Effect of Retorting Temperature on the Pyrolysis Characteristic of Longkou Oil Shale

Wang, Wei; Ma, Yue; Li, Shuyuan; Yue, Changtao; Gao, Jiancun

doi:https://doi.org/10.1155/2021/6442951

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Abstract Introduction Experimental Results and Discussion Conclusion Data Availability Conflicts of Interest Authors’ Contributions Acknowledgments References Copyright Related Articles

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Qualitative and Quantitative Characterization of Shale Oil Plays for Efficient Exploitation

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Research Article | Open Access

Volume 2021 | Article ID 6442951 | https://doi.org/10.1155/2021/6442951

Effect of Retorting Temperature on the Pyrolysis Characteristic of Longkou Oil Shale

Wei Wang,^1,2Yue Ma,³Shuyuan Li,³Changtao Yue,³and Jiancun Gao^1,2

Academic Editor: Bo Liu

Received17 Jun 2021

Revised25 Aug 2021

Accepted09 Sept 2021

Published07 Oct 2021

Abstract

Oil shale samples from Longkou City, Shandong Province, China, were pyrolyzed in a fixed bed reactor at retorting temperature varied from 400 to 550°C under nitrogen atmosphere with heating rate of 15°C/min. The influence of retorting temperature on the yield and characteristics of shale oil and retorting gases were determined. It was observed that the oil yield increased to the maximum value, 15.68 wt%, as the retorting temperature increased from 440 to 550°C. And increasing retorting temperature improved also gas yields, but reduced the char yield. The contents of H₂, CO₂, and CH₄ in the retorting gas increased with the rising of retorting temperature. The ratio of alkane/alkene hydrocarbon (C₁-C₅) decreased because of the secondary cracking reactions of gas phase in the high temperature. The carbon and nitrogen contents of shale oil increased with increasing retorting temperature, while those of hydrogen and oxygen decreased. The sulfur content was not significantly affected by the retorting temperature. In addition, the shale oil obtained from 550°C had the lowest aromatic content, 25.12 wt%, and the highest saturate content, 50.03 wt%, compared to the other retorting temperatures due to the cracking of aliphatic compounds. The alkanes with 8-34 carbons and alkenes with 8-27 carbons were detected in the shale oil. The concentration more than 20 mg/g_oil was C₂₃-C₃₀ in the range of 400-550°C. The total content of n-alkanes decreased to 369.25 mg g^-1_oil, and that of n-alkene reached the maximum value at 550°C, 181.62 mg/g_oil, with the rise of retorting temperature. It was demonstrated that the higher temperature was beneficial to promoting the reaction of aromatization, dehydrogenation, fraction, and other reactions in the pyrolysis process.

1. Introduction

The effective development of oil shale resources could alleviate the global energy crisis, of which the global resources amount to and the China’s reserves of approximately rank third among countries worldwide [1–4]. Containing 20-50% organic matter and 50-80% inorganic mineral, oil shale can be converted to shale oil, semicoke, water, and retorting gas by heating. Shale oil can be used as a component of marine fuels and light oils, such as gasoline and diesel oil. Hence, it is necessary to study the effect of pyrolysis factor on the pyrolysis characteristic of oil shale in order to increase the oil yield and upgrade its quality [5–7].

So far, there have been various studies for the efficient recovery of shale oil from oil shale [8–11]. Wang et al. [8, 9] investigated the influence of heating rate and retorting temperature on pyrolysis characteristics of Dachengzi oil shale pyrolysates. It was noticed that increasing temperature was beneficial to the yield and quality of shale oil, causing a drop of oil/gas yield ratio because of the secondary cracking reactions. Wang et al. [10] optimized the pyrolysis condition of Longkou oil shale, such as nitrogen flow rate, retorting temperature, particle size, and heating rate in order to reduce the secondary reactions. Oil yield reached the maximum value, 17.46%, higher than Fischer assay oil yield, at heating rate 15°C/min up to 550°C under 0.6 L/min nitrogen flow rate for 2 to 3 mm oil shale particles. TGA-MS was used to analyze the pyrolysis characteristics of Green River oil shale [11]. It was noted that the compositions of products were affected by the fundamental chemistry of the organic matter decomposition in oil shale and overall system or reactor configuration. Amounts of alkenes were produced during the pyrolysis process, in which the increase of alkenes to alkanes ratio as the heating rate rose. Dung [12] found out that the retorting temperature was the only factor to influence the H/C atomic and nitrogen content of shale oil derived from Stuart and Condor oil shale. Jaber and Probert [13] indicated that the main region of pyrolysis was in the range of 200-600°C. And the oil yield and the extent of any oil cracking were greatly influenced by the final retorting temperature. Al-Ayed et al. [14] pointed out that the oil yield decreased from 80% to 40% when heating rate was increasing from 0.2 to 13°C/min in fixed-bed retort, which was linked to the secondary cracking reactions. What is more, the oil yield and retorting gas were affected by the particle size. It was showed that shale oil yield firstly increased and then descended when the particle size increased from 10 to 40 mm [15]. It was attributed to the diffusion influence of large particle size. Besides, many studies focused on the thermogravimetric analyses for pyrolysis kinetics of oil shale. Li and Yue [16] studied the pyrolysis kinetics of different Chinese oil shale samples at a heating rate of 5 K/min using a special kinetic model involving 11 parallel first-order reactions. The parallel reactions with different apparent activation energy and frequency factors occurred simultaneously. It was found that the apparent activation energies were in the range of 120-240 kJ/mol. Abu-Qudais et al. [17] investigated the kinetics of pyrolysis of Attarat oil shale in Jordan using a thermogravimetric analyzer. Two kinetic expressions for each heating rate were proposed, standing for two steps of decomposition. Doǧan and Uysal [18] and Torrente and Galan [19] investigated the pyrolysis kinetics of Turkish and Spanish oil shale using first-order kinetics models including integral method, differential method, Friedman procedure, and maximum rate method. Mustafa Versan Kok and Senguler studied oil shale samples nonisothermally using thermogravimetry analysis [20]. In the combustion process, kinetic parameters of the samples were determined by Kissinger and KAS kinetic models. The results showed that the activation energy values were almost the same with each other in three different kinetic models studied. The differences were mainly contributed to the different equation parameters or the assumptions that those models are based on. However, few researches have investigated the effect of retorting temperature on the contents of alkanes and alkenes in the shale oil. Because the quality of shale oil recovered is eager to upgrade to improve its economic value [21], additional upgrading processes are required.

Therefore, not only yield but also properties of retorting gas should be considered. In this study, the effects of retorting temperature on the pyrolysates of Longkou oil shale were investigated in the range of 400-550°C. And the comparisons of characteristics of pyrolysates under different retorting temperatures, including the compositions of retorting gas, high-temperature simulated distillation, SARA fractions, and ultimate analysis of shale oil, were performed. The semiquantitative analysis of alkanes and alkenes in shale oil by GC-MS was also investigated. In other words, a uniform experimental design was rare to discuss effects of retorting temperature on different pyrolysis responses.

2. Experimental

2.1. Samples and Pretreatment

The oil shale used in this work was from Longkou City, located in Shandong Province of China. During the experiments, the samples were crushed to 0-6 mm particles according to the National Standards: GB/T 19494.2-2004 Mechanical sampling of coal-Part 2: Method for sample preparation. Fischer assay was carried out according to ASTM standards (ASTM D3904-90). The proximate analysis and ultimate analysis were conducted using a HTGF-3000 analyzer (Hebi Huatai Instrument Measuring Appliance Co. Ltd.) and a LECO CHN-2000(LECO, USA) and LECO S-144DR analyzer (LECO, USA), respectively. Samples were stored in sealed containers at room temperature, and there was no measurable change in its moisture content over the course of experiments. The basic properties of Longkou oil shale are presented in Table 1.

2.2. Pyrolysis Equipment

Figure 1 shows the schematic diagram of the fixed bed apparatus in laboratory scale. The fixed-bed reactor placed with 50 g sample was electrically heated at 15°C/min heating rates under 0.6 L/min N₂ atmosphere to different final temperatures with the range of 400-550°C. In order to minimize secondary reaction, nitrogen was introduced from the bottom of pyrolysis reactor to evenly sweep the generated products toward the side outlet of reactor. The liquid condenser was consisted of a glass liner contained within a series of cold traps, maintained at -22°C and connected to the reactor outlet. Serpentine condenser pipe was used to ensure that all the pyrolysis products had enough time to cool and collect the pyrolysis products uncooled in the condenser bottle although it was few. The reactor was cooled to the room temperature after the experiment ceased. The weight of semicoke was collected and weighted. The weight of the mixture of shale oil and water was the difference between the gross weight of bottles with condensate and empty bottles. The water content was determined by solvent extraction. The weight of shale oil was the difference between mixture and water. The noncondensable outlet gas was collected using gas bag from condenser pipe and analyzed by Agilent-6890 gas chromatograph.

In order to assess the reproducibility, each pyrolysis experiment was performed twice under identical conditions.

2.3. SARA Fractions

The collected shale oil was separated into four fractions (saturates (S), aromatics (A), resins (R), and asphaltenes (A)) by a column chromatography on activated alumina using the National Standards: GB/SH/T 0509-2010. At first, shale oil was mixed with 50 mL of heptane for 12 h. As the fraction of bitumen insoluble in heptane, the asphaltenes was collected after the mixture was filtered through a funnel covered with cotton wool. The separated soluble fractions were directed to column chromatography to obtain the saturates, aromatics, and resins, respectively. It was eluted sequentially by heptane, methylbenzene, and methylbenzene-ethanol to obtain. A glass column () was packed with 40 g of aluminum oxide (80-100 mesh, activated at 500°C for 6 h). Cotton wool was inserted at the bottom of the column. After the hexane-soluble matter was poured through the packed column, 80 mL of heptane was added to elute the saturate fraction. The aromatic fraction was obtained by eluting the column with 80 mL methylbenzene. And then, the mixture of methylbenzene-ethanol (1 : 1, ) was added to obtain the resin fraction.

2.4. High-Temperature Simulated Distillation

High-temperature simulated distillation was analyzed using the ASTM method HT 750 (AC Analytical Controls Method; Analytical Controls, Inc., USA) and performed an Agilent 6890 N gas chromatograph (Agilent Technologies, Inc., USA), which was equipped with an automatic injector. The carrier gas was helium (99.999% purity) with a constant flow rate of 5 mL min^-1. The GC contained a capillary column (DB-1, Agilent Technologies, Inc., USA) with a cool on-column injector. Temperature programming for the column was 10°C/min from 50°C to 450°C (maintain for 5 min). The injector and flame ionization detector (FID) were held at 300 and 350°C, respectively. About 10 mg of shale oil sample was completely dissolved in 1 mL of carbon disulfide to analyze.

2.5. GC-MS Analysis

GC-MS analysis of shale oil was performed using Thermo Trace DSQ GC-MS equipped with a HP-5 MS column (). The GC oven was held at 50°C for 3 min, increased to 300°C with heating rate of 5°C/min, and then held isothermal for 10 min. The injector and transfer line temperatures were held at 300 and 250°C, respectively. Helium was used as the carrier gas with 1 mL min^-1 flow rate. Ion source temperature was maintained at 250°C, and ionizing voltage was 70 eV.

About 10 mg of shale oil sample was completely dissolved in 1 mL of dichloromethane. And 10 mg mL^-1 standard N-tetracosane-D50 diluted with 1 mL N-hexane was added to the shale oil to semiquantitatively analyze the compositions of alkanes and alkenes.

2.6. GC Analysis

GC analysis of retorting gas was performed an Agilent 6890N gas chromatograph (Agilent Technologies, Inc., USA). The gas analyzer was consisted of a Hayesep-Q 5A column () with thermal conductivity detector (TCD) detector and a HP-PLOT S column () with FID detector. The GC oven was held at 50°C for 10 min, increased to 190°C with heating rate of 15°C/min, and then held isothermal for 15 min. The injector and detector temperatures were held at 150 and 250°C, respectively. Helium was used as the carrier gas with 38 mL/min flow rate. The GC was recorded for the following components: CH₄, C₂H₆, C₂H₄, C₃H₈, C₃H₆, C₄H₁₀, C₄H₈, C₅H₁₂, C₅H₁₀, CO, CO₂, and H₂.

3. Results and Discussion

3.1. Products Yield

The oil yield of Longkou oil shale affected by final retorting temperature is showed in Figure 2. It was obvious that the semicoke content decreased from 81.83% to 71.04% as the final retorting temperature increased from 400°C to 550°C. It means that the shale oil and retorting gas of oil shale can be increased by about 10% by increasing the retorting temperature. Hence, the retorting temperature was the main factor affecting the pyrolysis process of oil shale. When the retorting temperature increased from 400°C to 520°C, the oil yield increased from 6.02% to 15.68 wt% due to the split of strong chemical bonds in aromatic rings and heterocyclic and alicyclic compounds. So, the main pyrolysis reaction zone of oil shale was in the range of 400-520°C. After then, the oil yield continued to increase slowly from 520°C to 550°C as the incomplete pyrolysis at low retorting temperature occurred. It was indicated the end of conversion of high molecular organic compounds to oil [22–24]. Above it, the shale oil yield may reduce due to the polycondensation and aromatization reactions of oil [23, 24]. During the whole temperature-rising stage, the content of water and retort gas increased slowly as they were released with the formation of shale oil during pyrolysis process. So, 550°C was selected as the optimal temperature.

3.2. Compositions of Retorting Gas

Figure 3 shows the influence of final retorting temperature of oil shale on the composition of retorting gas. Obviously, the retorting gases were mainly CH₄, CO₂, and H₂ in the initial pyrolysis process. As the temperature rose, the organic matter in the oil shale began to decompose, and many small molecular gases and volatile products were generated. So, the retorting gas products mainly included inorganic gases and small molecular hydrocarbons of C₁-C₅. The light compounds (C₁-C₅) were mainly generated from the cracking of macromolecule or some side chains, containing methane, ethane, propane, butane, pentane, ethene, propene, butene, and pentene. In the range of 350-400°C, the increase of CO₂ and CO content was ascribed to the decarboxylation reaction of the oxygen-containing functional groups. But in the higher temperature range, the rise of their contents possibly caused by the break of the carbonyl group [25].

Besides, the ratio of alkanes (C₁-C₅)/alkenes (C₂-C₄) decreases with the rise of the final temperature. The change of ratio is linked to the secondary cracking reaction. The higher the retorting temperature, the more the gas cracking and secondary gas phase reactions [26, 27].

When the retorting temperature reached 490°C, the content of H₂ increased rapidly. The generation of H₂ mainly came from two reactions: one was the condensation polymerization reaction between free radicals and the other was the condensation and aromatization reaction of pyrolysis products. At higher temperatures, alkanes were prone to decomposition and dehydrogenation due to lower bond energy, leading to higher olefin and H₂ content. With the increase of temperature, the ratio of alkanes to alkenes in the retorting gas decreased, indicating that high temperature intensifies the secondary cracking reaction of gas.

3.3. SARA Fractions

Figure 4 provides the results of SARA fractions of shale oil obtained from different retorting temperatures. It was obvious that the aromatics, resins, and asphaltenes in shale oil increase as the retorting temperature rose from 400 to 550°C. The increase of aromatic fraction may be caused by the increase of aromatization at high temperature. It has been reported that aromatic compounds were generated from the cracking of aliphatic compounds or Diels-Alder type reactions [28, 29]. The cracking reaction was dominant in the high temperature, and the long-chain aliphatic hydrocarbons were fractured to generate more aromatic components, decreasing the content of saturates’ fraction from 54.12 wt% to 50.03 wt%. In addition, the strong thermodynamic stability of aromatic fraction was also another reason for the increase of aromatic fraction.

The increase of asphaltene fraction could be interpreted by the pyrolysis mechanism of bitumen as the intermediate product [30]. The bitumen was converted into asphaltenes and other products during the pyrolysis process.

3.4. High-Temperature Simulated Distillation

Figure 5 shows the simulation distillation curves of shale oil obtained at different pyrolysis final temperatures (400-550°C). It can be seen from the figure that there was little difference in the distillate distribution of shale oil at different final temperatures. The curve of simulation distillation moved upward slightly as the final temperature of pyrolysis increased, indicating that the final temperature of pyrolysis has hardly affected on the distillation range distribution of shale oil.

3.5. Ultimate Analysis of Shale Oil

The ultimate results of shale oil are depicted in Figure 6. Obviously, the C content in shale oil increased by about 3 wt%, and the H content decreased slightly when the final retorting temperature rose from 400 to 550°C. It means that the H/C ratio decreased with the increase of the final retorting temperature, which may be caused by aromatization, dehydrogenation, and coking reactions. The result was the same with that of SARA.

The O content decreased from 7.59 wt% at 400°C to 6.02 wt% at 550°C due to the oxygen-containing functional groups decompose rapidly due to thermodynamic instability in the high temperature. The higher the temperature, the easier it was to generate small molecular oxides, resulting in the decrease of oxygen content in shale oil. The N content increased slightly with the increase of temperature, which was attributed to the aromatization reaction to form polycyclic aromatic nitrogenous compounds in the high temperature. However, the increase of temperature had little effect on the content of S element. S compounds can stably exist in shale oil due to their strong thermodynamic stability.

3.6. GC-MS Analysis for Shale Oil

Figure 7 describes the effect of the final retorting temperature on the total ion chromatogram of shale oil. It was observed that the ion distribution of shale oil obtained from different retorting temperatures was similar, indicating the molecular components of shale oil were unchanged by changing the retorting temperature. N-alkanes with 8-34 carbons and n-alkenes with 8-27 carbons were detected. Most of compounds were concentrated on the heavier compounds of shale oil. In addition, the difference of peak area and height of standard N-tetracosane-D₅₀ is less than 5% to eliminate the systematic errors. The relative intensity of the MS spectrum was estimated according to the area ratio of a peak to the peak of n-C₂₄D₅₀. And the concentration (mg/g_oil) of alkene and alkane compounds is depicted in Figures 8 and 9, respectively. The concentration more than 20 mg/g_oil was C₂₃-C₃₀ in the range of 400-550°C. The maximum concentration in the range of 400-550°C was C₂₇ to C₂₉, especially the concentration of C₂₇ at 460°C reached to the maximum value with 30 mg/g_oil because of the rapidly cracking of macromolecular components in oil shale [9]. What is more, the main contents of shale oil were C₁₆-C₃₀ in the range of 400-460°C, but C₂₂-C₂₉ ranging from 460°C to 550°C. And when the retorting temperature increased from 400°C to 550°C, the content of n-alkanes with C₈-C₁₅ in shale oil gradually increased, especially the content of C₈-C₁₂ n-alkanes with an increase of about 2-4 mg/g_oil. But the content of C₁₆-C₃₄ n-alkanes decreased as the secondary fracture reaction of long-chain alkanes occurred in the higher temperature. Although the secondary cracking of long-chain alkanes in shale oil was demonstrated to take place, the generating rate of shale oil was faster than the cracking rate as the oil yield reached to the maximum value.

Figure 10 shows the effect of the retorting temperature on the content of C₈-C₂₇ n-alkenes in shale oil. The content of C₈-C₂₀ n-alkenes increased with the rise of retorting temperature, while that of C₂₁-C₂₇ n-alkenes decreased. The larger the carbon number of an alkane, the smaller the bond energy between its C-C bond and C-H bond, and the worse its stability. Therefore, long-chain n-alkanes were easy to crack or dehydrogenize at high temperatures to generate short-chain alkanes and alkenes. Therefore, the higher the temperature, the higher the content of C₈-C₁₅ alkanes and C₈-C₂₀ alkenes, and the lower the content of long-chain alkanes. Besides, long-chain alkenes may undergo fracture, dehydrogenation, and aromatization reactions at high temperature, resulting in a decrease in its content and an increase in the content of short-chain alkenes [10].

Figure 11 shows the variation of n-alkane and n-alkene contents at different retorting temperatures. With the increase of the retorting temperature, the content of n-alkanes decreased from 402.91 to 369.25 mg/g_oil, a decrease of about 43 mg/g_oil. The total amount of n-alkene reached the maximum value at 550°C, 181.62 mg/g_oil. The change trend of n-alkane and n-alkene contents was opposite with the increase of the retorting temperature. But the increase number of n-alkanes was about half of the decrease number of n-alkanes, indicating that the n-alkanes may participate in the reaction of aromatization, dehydrogenation, fracture, and other reactions in the pyrolysis process.

4. Conclusion

In this study, the yield of pyrolysates and characteristics of shale oil and retorting gas were obviously affected by retorting temperature carried out in laboratory-scale fixed-bed reactor for Longkou oil shale. The main results were the following: (1)As the retorting temperature increased from 430 to 520°C, the yield of shale oil and retorting gas increased while that of shale char decreased significantly. And retorting temperature with 550°C was optimal at 15°C/min heating rate, ensuring maximum value of shale oil yield, 17.46%(2)As the retorting temperature increases, there were increases in CH₄, H₂, and CO₂ while a decline of the ratio of alkanes/alkenes (C₁-C₅) because of the gas secondary cracking reaction. At higher temperatures, alkanes were prone to decomposition and dehydrogenation due to lower bond energy, leading to higher olefin and H₂ content(3)Increasing the retorting temperature from 400 to 550°C caused aromatic fractions to slightly increase because of the cracking of aliphatic compounds or Diels-Alder type reactions at higher temperature. In addition, the decrease of saturate fraction can be also explained by the cracking of aliphatic compounds. The increase of asphaltene fraction could be interpreted by the pyrolysis mechanism of bitumen as the intermediate product, in which the higher temperature, the more asphaltene produced. It was worth noting that the retorting temperature had little effect on the distillation range distribution of shale oil(4)Increasing retorting temperature increased the carbon and nitrogen content, while decreased that of hydrogen and oxygen, and the atomic H/C ratio in the derived shale oil. This decrease of the atomic H/C ratio was caused by the aromatization, dehydrogenation, and coking reactions in the higher temperature. The decrease of oxygen was also reflected by the decomposition of the oxygen-containing functional groups. The increase of the nitrogen content was linked to the aromatization reaction, which was converted to form the polycyclic aromatic nitrogenous compounds in the high temperature. The sulfur content was not significantly affected by increasing retorting temperature due to its stability(5)The concentration more than 20 mg/g_oil was C₂₃-C₃₀ in the range of 400-550°C. The concentration of alkanes (C₈-C₁₅) and alkenes (C₈-C₁₂) increased, whereas the total content of n-alkanes (C₈-₃₄) decreased from 402.91 mg/g_oil to 369.25 mg/g_oil and that of n-alkene reached the maximum value at 550°C, 181.62 mg/g_oil with the rise of final retorting temperature, indicating that the n-alkanes may participate in the reaction of aromatization, dehydrogenation, fraction, and other reactions in the pyrolysis process

Data Availability

The data used to support the findings of this study are available from the corresponding author (Pro. Jiancun Gao) upon request.

Conflicts of Interest

The authors declare that they have no conflicts of interest.

Authors’ Contributions

Wei Wang and Yue Ma contributed equally to this work.

Acknowledgments

The project was supported by the Natural Science Foundation of Beijing, China (General Program, No. 2214071). We are grateful to Pro. Q. Shi from China University of Petroleum-Beijing for GC-MS analysis support.

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Copyright © 2021 Wei Wang et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

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