Studying the mechanism and kinetics of fuel desulfurization using CexOy/NiOx piezo

Scientific Reports volume 13,

Scientific Reports volume 13, Article number: 7574 (2023) Cite this article

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In order to advance desulfurization technology, a new method for excellent oxidative desulfurization of fuel at room temperature will be of paramount importance. As a novel desulfurization method, we developed piezo-catalysts that do not require adding any oxidants and can be performed at room temperature. A microwave method was used to prepare CeO2/Ce2O3/NiOx nanocomposites. Model and real fuel desulfurization rates were examined as a function of synthesis parameters, such as microwave power and time, and operation conditions, such as pH and ultrasonic power. The results showed that CeO2/Ce2O3/NiOx nanocomposites demonstrated outstanding piezo-desulfurization at room temperature for both model and real fuels. Furthermore, CeO2/Ce2O3/NiOx nanocomposites exhibited remarkable reusability, maintaining 79% of their piezo-catalytic activity even after 17 repetitions for desulfurization of real fuel. An investigation of the mechanism of sulfur oxidation revealed that superoxide radicals and holes played a major role. Additionally, the kinetic study revealed that sulfur removal by piezo-catalyst follows a second-order reaction kinetic model.

Low-frequency vibration energy is everywhere in the environment and has a bright prospect for resolving the energy crisis and pollution issues. There has, however, been no effective utilization of this low-frequency energy1,2. Low-frequency vibration energy can be converted into energy in two ways: piezoelectric energy harvesting and piezoelectric catalysis3,4,5. As a result of piezoelectric catalysis, mechanical vibrations can be converted into free charges at the surface of piezoelectric materials in a wide range of environments (e.g. water and air). As a result of the local micro-electrolysis of water, piezo-catalytic materials can produce a number of reactive oxygen species (ROS) such as ·OH, ·O2–, ·HO2 and H2O2. In the textile, chemical, pharmaceutical, and food industries, ROS are used to catalytically oxidize and degrade toxic and carcinogenic dyes in water6,7,8.

The purpose of this work is to suggest a new application for piezocatalysts; we used nickel oxide/cerium oxide nanocomposites as piezocatalysts for the desulfurization of models and real fuels. Using Piezo-catalysis has several advantages compared to existing catalysis for desulfurization processes. They can operate in dark conditions, show a high desulfurization rate, and low cost, and can harvest low-frequency vibrations present in the environment to drive desulfurization reactions.

In spite of the adoption of new energy strategies in recent years, the use of conventional fuels remains dominant. As a result of the combustion of sulfur-containing fuels, SOx is produced, which contributes to acid rain and fine particulate matter (PM 2.5), as well as corrosion of engines and catalytic converters8,9,10,11. Globally, strict regulations have been enacted to limit fuels with low sulfur content12,13. By utilizing hydrodesulfurization (HDS), which has been widely used in industry for decades, aliphatic sulfur can be easily removed from fuel oil in industrial production. Due to the steric hindrance, it is difficult to eliminate aromatic sulfur compounds from fuel, such as dibenzothiophene (DBTP). High temperatures and pressures, as well as large amounts of hydrogen, are required for HDS to remove thiophene derivatives, resulting in high operating costs and loss of octane14,15,16,17,18,19,20. We present here a piezocatalyst that eliminates sulfur compounds from the model and real fuel without adding any oxidants and by only applying mechanical force. In contrast, previous techniques for desulfurization required to add oxidants, such as H2O221,22,23,24,25,26,27. Recently, an modified the oxidative desulfurization process by using single-atom catalysts with earth-abundant metal cores and robust nanoporous supports, as well as mixed transition metal oxides28,29,30. As a result of using single-atom catalysts or mixed transition metal oxides, the efficiency and stability of the catalyst were improved.

Different parameters, including synthesis parameters and operation parameters, were examined in order to determine how they affected the desulfurization rate. At room temperature, desulfurization rates of up to 92.7% for TP and 94.1% for DBTP could be achieved within 30 min of mechanical force is applied. The results showed that microwave pulses and calcination times had a dramatic impact on desulfurization rates in the synthesis step, whereas ultrasonic power and extraction time play a significant role in the operation step. In addition to its advantages, such as its oxidant-free nature and low reaction temperature, this method can be applied to basic, natural, and acidic environments.

There was no further purification of any of the chemicals used in the study since all of them were of analytical grade. Ce(NO3)3.6 H2O and Ni(NO3)2. 6 H2O were purchased from Fluka. Ethylenediaminetetraacetic acid disodium (EDTA-2Na) and ethanol were purchased from BDH Chemicals (England). 1, 4-benzoquinone (BQ), and Isopropanol (IPA) were purchased from Scharlau (Spain). Cetyltrimethylammonium Bromide (CTAB) and Ammonium hydroxide were purchased from Sigma-Aldrich and Merch, respectively.

First, 30 mL of 0.06 mM Ce(NO3)3.6 H2O and Ni(NO3)2. 6 H2O was prepared, and the solvent was the mixture of distilled water and methanol with a ratio of 2:1, respectively. As a next step, the above solutions were mixed. An aqueous solution containing 0.016 mM CTAB was gradually added to the metal solution under stirring. By adding 1 M ammonia, the pH was adjusted to 11. Following this, the mixture was placed in a microwave and heated for four minutes (30 s on, 60 s off). The products were then washed, dried, and calcined at 500 °C for five hours. A series of catalysts were prepared under different parameters using the same procedure, as shown in Table 1. D1–D3 show the effect of microwave power, whereas d4 and d5 show the effect of microwave pulse. Lastly, d6–d11 illustrate the effects of microwave time, calcination temperature, and time.

In a Pyrex cell, 50 mg of piezocatalyst was used to oxidative desulfurize the model fuel and 25 mL of model fuel (TP or dibenzothiophene (DBTP)/n-hexane solution containing 500 ppm or real fuel (kerosene containing 2273 ppm) under the ultrasonic device. The samples were stirred in the dark for 30 min prior to ultrasonication. As a result of this step, equilibrium between adsorption and desorption is established. At certain intervals, desulfurized samples were withdrawn and centrifuged in a volume of 10 mL. The oxidized sulfur compounds were extracted with a 1:1 vol ratio of DMF under magnetic stirring for 15 min at room temperature after the precipitate was discarded. As a final step, two phases of DMF and hexane were separated and the model fuel in the upper phase was analyzed by an X-ray sulfur meter. The pH value of the solution was adjusted by adding drops of 0.1 M NaOH or 0.1 M H2SO4 in the pH range of 4–10 while stirring the solution. In order to measure the pH of solutions containing n-hexane solvent, a water extraction process is used. The sample is thoroughly mixed with water before being added (1:1). As soon as equilibrium has been reached, the solvent phase is separated, and the pH of the water phase is determined.

Based on the following formula, the desulfurization efficiency (DS) of fuel was calculated:

During the initial and t-time periods, S and St represent the sulfur concentrations in the fuel solution, respectively.

In addition, radical trapping experiments were performed in order to identify the primary active species during piezo desulfurization. There were a number of scavengers added to the fuel system, including Na2-EDTA (to quench h +), IPA (to quench OH radical), and BQ (to quench ·O2−).

An X-ray diffractometer (Philips X'pert Pro MPD, The Netherlands) was used to examine the crystal structure of the samples with Ni-filtered Cu Kα radiation (λ = 1.54 Å). Sonochemical reactions were carried out in an ultrasonic bath with a 20 kHz ultrasonic device with a maximum output power of 360 watts. An EDS (energy dispersion spectroscopy) analysis was performed with an X-Max Oxford, England. A FESEM image was recorded using IGMa/VP-ZEISS, Germany. Zeiss transmission electron microscopy was used to acquire TEM images.

In order to determine the nature and phase structure of the as-synthesized samples, XRD analysis was conducted, as illustrated in Fig. 1. XRD pattern of d1-d3 indicated the effect of microwave power on crystallinity and compound of products. The CeO2/Ce2O3/NiOx nanocomposite was formed under microwave power of 600 W. CeO2 and Ce2O3 showed good agreement with JCPDS 96-900-9009 with cubic phase and JCPDS 96-101-0280 with hexagonal phase. XRD patterns of nickel oxide with hexagonal phase were in good agreement with JCPDS 96-901-2317. Based on the Scherrer equation, an average crystal size of 17.9 nm was determined. A composite consisting of CeO2/Ce2O3/NiOx with an average crystal size of 22.4 nm was obtained by increasing microwave power to 700 W. When microwave power is increased to 900 W (d3), however, CeO2 nanoparticles with an average crystal size of 4.9 nm are almost formed. Our previous research indicated that microwave pulses are an important parameter affecting the crystallinity and morphology of the final product31,32,33. The synthesis of catalysts was carried out under three different pulse conditions (30 s on, 60 s off, and 30 s on, 30 s off). An increase in the ratio of on to off in each cycle resulted in a decrease in the NiOx ratio as shown in the XRD patterns. It appears that NiOx requires more relaxation time in order to crystallize.

(a) XRD patterns of catalysts d1-d6 and (b) XRD patterns of catalyst d7-d11.

To investigate the effect of microwave time on the crystallinity and structure of final products, the catalyst was prepared at three different microwave times: 3 min (d6), 4 min (d2), and 6 min (d7). In accordance with the results of the XRD analysis, the intensity of the peak associated with nickel oxide decreased with increasing microwave time. Nickel oxide can be formed more efficiently by using less microwave energy. Calcination temperature and time are two other parameters in the synthesis of a catalyst. For the purpose of studying the effects of calcination temperature on the products, three different calcination temperatures were used: 400 °C (d8), 500 °C (d2), and 700 °C (d9). Based on our findings, Ce2O3 disappeared with increasing calcination temperature, leading to the formation of a composite composed of CeO2 and NiO. Increasing the calcination temperature also resulted in an increase in crystal size. The XRD patterns of d10, d2, and d11 illustrate the effect of calcination time on crystallinity. The results of this study showed that calcination time did not affect the composition of the composite. Ce2O3/CeO2/NiOx nanocomposites were formed at three calcination temperatures of 3, 5 and 7 h. However, crystallinity improved with time.

An illustration of the SEM images of the d1-d7 catalysts is provided in Fig. 2a–i. The SEM images in Fig. 2a–e illustrate the effects of microwave power on the morphology of the products. The formation of micro-sized spheres made of particles 20–100 nm in diameter was observed using microwave power of 600 W (Fig. 2a and b). Increasing microwave power to 700 W led to the formation of micro-sized plates containing nanoparticles of 20–90 nm in diameter (Fig. 2c and d). The microwave power of 900 W resulted in rod-like structures made by nanoparticles with a diameter of 30–150 nm (Fig. 2e). In this study, it was demonstrated that microwave power can be used to control the morphology of a piezo-catalyst. Increasing microwave power resulted in changes in the morphology from microspheres to rods, as can be seen in the figure. Due to increasing power, the penetration depth of the solvent would increase, which would facilitate the formation of oriented structures like rods34.

SEM images of : (a,b) catalyst d1, (c,d) catalyst d2, (e) catalyst d3, (f) catalyst d4, (g) catalyst d5, (h) catalyst d6, (i) catalyst d7.

Changing the microwave pulse while keeping other parameters constant allowed a study of the effect of the microwave pulse on the morphology of piezo-catalysts. During the first series of products, microsphere structures were formed when the pulse was on for 30 s and off for 60 s (Fig. 2a and b). In Fig. 2f and Fig. S1 in SI, microwave pulses of 30 s on and 30 s off resulted in nanoplatelets with 40–120 nm in thickness that was adherent to each other. The thick plates with a thickness of 200–800 nm were formed when the pulse was 30 s on and 10 s off (Fig. 2g and Fig. S2 in SI). As a result of increasing the running time in each cycle, nanoparticles became more adherent. Increasing the running time in each cycle prevented nanoparticles from rearranging and assembling themselves. In addition, increasing the running time leads to a greater penetration depth, providing conditions for the formation of oriented structures34. Another parameter that might affect the morphology of the piezo-catalyst is microwave time. In Fig. 2a,b,h,i, SEM images demonstrate that nanoparticle sizes increased with increasing microwave time. In addition to calcination temperature, calcination time was another parameter that affected the morphology of final products. Nanoparticles with an average diameter of 18–80 nm were formed at a calcination temperature of 400 °C (Fig. 3a). It is shown in Figs. 2a and b that nanoparticles of 20–100 nm were obtained by increasing the calcination temperature to 500 °C. A subsequent increase in calcination temperature to 700 °C resulted in nanoparticles with a diameter of 30 to 150 nm (Fig. 3b). The results showed that nanoparticle size increased with increasing calcination temperature. To determine the effect of calcination time on the morphology of the piezo-catalyst, the piezo-catalyst was calcined for 3, 5, and 7 h. Nanoparticles with a diameter of 15–90 nm were formed after 3 h of calcination (Fig. 3c). During calcination time periods of 5 (Fig. 2a) and 7 h (Fig. 3d), piezo catalyst nanoparticles were enlarged to 20–100 nm and 50–200 nm, respectively.

SEM images of: (a) catalyst d8, (b) catalyst d9, (c) catalyst d10, and (d) catalyst d11.

Figure 4 and Table 2 illustrate the effect of synthesis parameters and the ratio of Ce, Ce, and O in the piezo-catalysts. Based on EDX results shown in Fig. 4, peaks related to Ce, Ni, O, and Au have been detected, which confirms the purity of the final products. In order to improve the conductivity of samples and prevent charge accumulation during EDX measurements, Au was used. According to EDX results, increasing the microwave power from 600 W (d1) to 700 W (d2) increased the ratio of Ce, while decreasing the ratio of Ni, while maintaining an almost constant level of oxygen. When the microwave power is raised to 900 W (d3), the ratio of Ce remains nearly constant, whereas the ratio of Ni increases and the ratio of O decreases. As a result of comparing the EDS of d2, d4, and d5, we can conclude that increasing microwave running time in each cycle results in a higher Ce ratio while decreasing the O ratio. The Ce ratio in piezo-catalysts increased with an increase in microwave time from 3 min (d6) to 4 min (d2) and 6 min (d7). Increased calcination temperatures from 400 °C (d8) to 500 °C (d2) and 700 °C (d9) resulted in a decrease in Ce ratios and an increase in O ratios. As a result of the EDS of d10, d2, and d11, the element ratio in the piezocatalyst was affected by the calcination time. Extending the calcination time from 3 h (d10) to 5 h (d2) and 7 h (d10), the Ce ratio went up and the Ni ratio decreased. In Fig. 5a–d, TEM images of d2 are presented as a champion catalyst. On the basis of TEM results, d2 is almost uniform in diameter, ranging from 10 to 15 nm.

EDX results for catalyst d1-d11 with WT % for each element. Au was used to coat samples to prevent charge accumulation during taking EDX.

(a–d) shows the TEM images of d2 as the best piezo-catalyst in desulfurization of model and real fuel.

Synthesis of parameters such as microwave power, microwave pulse, microwave time, calcination temperature, and time has a profound effect on desulfurization rats. In order to investigate these effects, piezo-desulfurization was carried out under ultrasonic power of 320 W for 30 min at pH = 7 and 50 mg of the catalyst. As can be seen in Fig. 6a, microwave pulses have a significant impact on the rate of desulfurization when piezo catalysts are prepared. Increasing microwave running time in each cycle significantly reduced desulfurization rates, as shown in the figure. The microwave running time during the synthesis of the catalyst was 30 s on and 60 s off in each cycle. This meant that 92.7 and 94.1% of the TP and DBTP were removed from the model fuel after only 30 min of ultrasonic processing. During the synthesis of the catalyst, the microwave pulse was changed to 30 s on and 30 s off. This resulted in a reduction in the desulfurization rate from 81.1 to 82.1% for TP and DBTP, respectively. In model fuel, TP and DBTP desulfurization rates were decreased to 72.4 and 74.6%, respectively, by changing the pulse duration to 30 s on and 10 s off during catalyst synthesis. The reason for this is that the d2 piezo catalyst has a smaller nanoparticle size compared to the d4 and d5. According to Kim et al.35, piezoelectricity increases non-linearly with decreasing nanostructure size.

(a) Effect of microwave pulse during synthesis of catalyst on removal of TP and DBTP, (b) effect of microwave time during synthesis of catalyst on removal of TP and DBTP, (c) effect of calcination temperature during synthesis of catalyst on removal of TP and DBTP, (d) effect of calcination time during synthesis of catalyst on removal of TP and DBTP, (e) effect of microwave power during synthesis of catalyst on removal of TP, DBTP, kerosene.

Figure 6b illustrates the effect of microwave time during the synthesis of the catalyst on sulfur removal yield. According to the results, microwave time had no significant effect on desulfurization rates. As a result of using d6 (3-min microwaves) as a catalyst, TP and DBTP desulfurization rates were 91.0 and 91.2%, respectively. As a result of substituting the catalyst with d2, which was prepared by microwave irradiation for 4 min, 92.7 and 94.1% of TP and DBTP were removed from the fuel. Finally, when the catalyst prepared under 6 min microwave irradiation was used, the desulfurization rate for TP and DBTP was changed to 89.3 and 89.2% for TP and DBTP, respectively. As a result of the fact that microwave time did not significantly affect catalyst size, it did not appear to have a significant effect on desulfurization rates. For the same reason, the calcination temperature did not significantly affect desulfurization (Fig. 6c). The Piezo catalytic activity of products is influenced by the calcination time. As shown in Fig. 6d, the desulfurization rate is influenced by the calcination time during the synthesis stage. In the case of TP and DBTP, the removal rates were 74.0% and 75.9%, respectively, when the calcination time was 3 h (d10). As calcination time increased to 5 h (d2) and 7 h (d11), desulfurization rates increased to 92.7 and 91.5% for TP and 94.1 and 92.0% for DBTP, respectively. This could be attributed to the fact that the crystallinity of the catalyst increased with increasing calcination time. Last but not least, microwave power is considered to be an invaluable parameter in the synthesis of the catalyst that can influence the desulfurization rates of the model and real fuel (Fig. 6e). In Fig. 6e, it is shown that the optimum microwave power in desulfurizing TP, DBTP, and kerosene is 700 W. Using a piezo-catalyst synthesized at 600 W (d1) as the catalyst, 81.7, 82.4 and 50.6% of TP, DBTP in model fuel, and sulfur compounds in kerosene as real fuel were removed under 30 min ultrasonic treatment. When the catalyst was changed to d2, which was prepared at 700 W, desulfurization rates for TP, DBTP, and sulfur compounds in kerosene as real fuel increased by 92.7, 94.1 and 56.7%, respectively. Increasing the microwave power to 900 W, however, resulted in a decrease in the sulfur removal percentage to 87.4, 86.9 and 53.9%, respectively. In this case, smaller particles also demonstrated better piezo catalytic activity.

As operation parameters that may influence desulfurization rates during piezo-desulfurization of fuel, we considered PH, ultrasonic power (US power), ultrasonic time (US time), and extracting time. Primary studies were conducted to identify optimum initial pH conditions for piezo-desulfurization of fuel. TP, DBTP, and sulfur compounds were desulfurized using d2 as the champion catalyst at pH 4, 7, and 10 (Fig. 7a and Table 3). During 30 min of ultrasonic treatment, 98.6 and 99.5% removal yields of TP and DBTP were achieved when the pH was initially adjusted to 4 using H2SO4. A pH of 7 resulted in a decrease in sulfur removal yields of 97.1 and 97.8% for TP and DBTP, respectively. When the pH was raised to 10 with NaOH, the desulfurization rate decreased even more. A pH adjustment to 10 resulted in the removal of 92.7 and 94.1% of TP and DBTP, respectively. Based on the results, it has been determined that acidic media are preferable for the piezo desulfurization of fuels. The reason for this is that H2SO4 can act as an oxidant and facilitate the oxidation of TP and DBTP. Alternatively, the basic environment decreases piezo-desulfurization since OH radicals played a negligible role in piezo-desulfurization and when we add more OH anions, more OH radicals are generated. We will discuss this in more detail in the section devoted to mechanisms. To test the effect of ultrasonic power on desulfurization rates, three power including 240 W, 320 W, and 360 W were used in piezo-desulfurization of TP and DBTP while pH was adjusted at 10 and 75 mg of d2 was used. Figure 7b and Table 3 showed that desulfurization rates increased by increasing ultrasonic power because piezo-electricity increased by increasing mechanical force and more free radical produced by increasing mechanical force.

(a) Effect of pH of reaction in yield of piezo-desulfurization of TP and DBTP, (b) effect of ultrasonic power on desulfurization rate during piezo-desulfurization of TP and DBTP, (c) effect of ultrasonic time on desulfurization rate during piezo-desulfurization of TP and DBTP, (d) effect of extraction time on desulfurization rates of TP and DBTP.

Table 3 and Fig. 7c illustrate the effect of ultrasonic time. Results indicated that the removal of sulfur was increased by increasing ultrasonic time. After 5 min, approximately 75.4 and 76.44% of the TP and DBTP had been removed, indicating that the reaction was progressing at a rapid rate. The results showed that the reaction had almost reached equilibrium after 30 min.

During the desulfurization process, extracting time refers to the period during which oxidized sulfur compounds are extracted by a polar solvent while being shaken. A summary of the results is presented in Fig. 7d. The results indicated that extraction was completed within 15 min of shaking. When the extract time was 1 min, the desulfurization rate for TP and DBTP was 50.7 and 57.1%, respectively. As a result of increasing the extraction time to 5 min, the desulfurization rate for TP and DBTP increased to 68.7 and 71.4%, respectively. As a result of 15 min of extraction, the removal yield for TP and TBTP was 97.1 and 97.8%, respectively. After 15 min of extraction, desulfurization rates are almost constant, which is why we consider 15 min to be the optimal extraction time. The effects of catalyst dosage and sulfur content on desulfurization rates were demonstrated in Fig. 8 and Table 3. When the catalyst dosage was increased from 10 to 75 mg, removal yield increased, and then decreased slightly when the piezo-catalyst dosage was increased to 100 mg. When 75 mg catalyst was used to desulfurize model fuel, the removal yield was 97.1 and 97.8%, respectively. The removal yield decreased to 95.0 and 95.2% when a 100 mg catalyst was employed to desulfurize model fuel. As a result of high catalyst dosages, catalyst accumulation may occur which led to reduced desulfurization rates. When 10 ppm sulfur content was used in model fuel, 99.1 and 99.2% of TP and DBTP were eliminated. The sulfur content was increased to 250 ppm, resulting in the removal of 98.9 and 99.0% of TP and DBTP, respectively. A further increase in sulfur content to 500 ppm resulted in a slight decrease in the desulfurization rate, with the desulfurization rate for TP and DBTP changing to 97.1 and 97.8%, respectively. Furthermore, when sulfur content was increased to 750 ppm and 1000 ppm, desulfurization rates changed from 78.4 and 64.2% for TP to 80.1 and 63.4% for DBTP during 30 min ultrasonication.

Effect of piezo-catalyst dosage (a) and sulfur content (b) on desulfurization rates of TP and DBTP.

When considering the use of catalysts in large-scale industrial applications, recovering and reusing the catalyst is an imperative factor. We investigated the reusability of CeO2/Ce2O3/NiOx piezo-catalyst, as shown in Fig. 9 and summarized in Table 4. Separating the used CeO2/Ce2O3/NiOx piezo-catalyst from the reactant medium allowed it to be reused without prior treatment for the subsequent batch reaction. Reaction batches were conducted under the same conditions: reaction temperature of 30 °C, catalyst dosage of 75 mg, and pH value of 7. There was remarkable reusability of the piezocatalyst as determined by the results. In the first run, desulfurization rates for TP and DBTP were 97.1 and 97.8%, respectively. After 11 reuses of the catalyst, these rates decreased to 79.4 and 78.2%, respectively. Even after 11 times of re-use, it retained almost 82% of its piezo-catalytic activity. A prepared piezo-catalyst demonstrated even greater reusability when it was used to desulfurize real fuel (kerosene). Despite being run 17 times, it maintained almost 79% of its piezo-catalytic activity.

Reusability of piezo-catalyst in removing TP, DBTP and sulfur in kerosene. Catalyst was d2, catalyst dosage was 75 mg.

To figure out the mechanism behind the piezo-desulfurization of catalysts, free radical scavengers experiments were conducted by using BQ, Na2EDTA, and IPA as superoxide radical scavengers, h + scavengers, and OH radical scavengers5,36,37,38. In the following batch reactions, the following conditions were used: reaction temperature of 30 degrees Celsius, d2 as a catalyst, piezo-catalyst dosage of 50 mg, and pH = 7. A summary of the results is shown in Fig. 10. Under 30 min of ultrasonic treatment, 92.7% and 94.1% of TP and DBTP were removed when no scavenger was used in the reaction. As a result of the addition of BQ, which acts as a superoxide radical scavenger, the removal percentage for TP and DBTP decreased to 29.0 and 26.0%, respectively. The results presented in Fig. 10 demonstrate that when Na2EDTA is used as an h + scavenger, the desulfurization rate for TP and DBTP decreases to 32 and 29.0%, respectively. In order to determine the effect of OH free radicals on fuel desulfurization, IPA was added to the reaction, which resulted in decreased desulfurization rates of 81.0 and 85.0%. A piezo desulfurization process was initiated by applying mechanical force to the piezo. The application of mechanical force resulted in the production of electrons and holes. Electrons react with trace oxygen in fuel and produce superoxide radicals, whereas holes react directly with sulfur compounds. A reaction between superoxide free radicals and holes led to the oxidation of sulfur compounds, which were then extracted with DMF. As a result of the results obtained, it was found that OH free radicals did not have a crucial role to play in the piezo-desulfurization of fuels. Due to the fact that the model fuel does not contain H2O, OH radicals played no significant role in the piezo desulfurization of TP and DBTP. TP and DBTP, on the other hand, were oxidized by holes and superoxide radicals generated by the piezo catalyst. It was approved by Jiang et al. that DBTO2 would form following the ODS process29. As a result of their feasible oxidation state, mixed transition metal oxides have been found to exhibit higher catalytic performances than single-component oxides. Moreover, binary metal oxides demonstrated higher catalytic performance, which may be attributed to the synergistic effect of the two metals39.

Schematic of piezo desulfurization of fuel and results for free radical scavengers.

A series of experiments were conducted in order to study the kinetics of piezo-desulfurization by CeO2/Ce2O3/NiOx nanocomposite at different temperatures, including 298 K, 313 K, and 333 K. Figure 11a shows the rates of desulfurization at different temperatures for 500 ppm TP. As the reaction temperature was raised, the rate of sulfurization increased. The desulfurization rates for three different temperatures were close after 20 min of reactions and almost reached equilibrium after 20 min. Based on Fig. 11b, approximately 14.0% of the TP was removed after 60 min of ultrasonic treatment without a catalyst. There is evidence that CeO2/Ce2O3/NiOx nanocomposite plays an influential role in desulfurization. The kinetics of piezo-desulfurization and characteristic constants of sulfur removal by piezocatalyst can be studied through kinetic measurements using pseudo-first-order, pseudo-second-order, and intra-particle diffusion. The Lagergren pseudo-first-order model is given as follows26,40:

(a) piezo-desulfurization rates over time for 500 ppm TP in different temperatures in presence of d2 as catalyst, (b) piezo-desulfurization rates over time for 500 ppm TP without using catalyst, (c) Pseudo-first-order and pseudo-second-order fitting for piezo-removal of TP in different temperatures, (d) Activation energy for removal of TP by piezo catalyst based on Arrhenius equation.

The amounts of sulfur removed at equilibrium and at time t (min) are represented by qe and qt, respectively. k1 (min−1) is the rate constant.

Pseudo-second-order kinetic model assumes that the rate of degradation is second order26,41,42.

where k2 is the pseudo-second-order rate constant. According to nonlinear regression of the isotherm models, Fig. 11c and Table 5 show the kinetic parameters and their first and second order fitting at different temperatures (298 K, 313 K, and 333 K). It was estimated that Pseudo-First-Order fitting at 298 K had an R2 of 0.927, whereas Pseudo-Second-Order fitting had an R2 of 0.978. In the case of piezo-desulfurization of fuel at 313 K, R2 for pseudo-first and pseudo-second orders changed to 0.934 and 0.987, respectively. At 333 K, the R2 for pseudo-first order and pseudo-second order was 0.935 and 0.987, respectively. Clearly, the results indicated that the desulfurization process was governed by a second order kinetics for CeO2/Ce2O3/NiOx nanocomposite piezo-catalyst. This explains why the reaction rate is so high in the first ten minutes. The activation energy was 10.968 kJ/mol based on the liner Arrhenius equation for second order rate constant desulfurization of sulfur compound by CeO2/Ce2O3/NiOx nanocomposites (Fig. 11d).

We have developed a new method for desulfurizing real and model fuel by the use of CeO2/Ce2O3/NiOx nanocomposites with PIEZO-catalytic properties. Desulfurization was achieved here without adding any oxidant and at room temperature. The XRD, EDS, EDS, and TEM characterizations confirmed that the CeO2/Ce2O3/NiOx nanocomposites were successfully synthesized. In addition to its outstanding desulfurization activity, the PIEZO-catalyst achieves complete desulfurization within 20 min at room temperature without adding any oxidants. It was possible to remove up to 97.1 and 97.8% of 500 ppm of TP and DBTP, respectively, in 30 min without adding any oxidant. CeO2/Ce2O3/NiOx nanocomposite showed excellent reusability, maintaining 79% of its piezo-catalytic activity even after 17 cycles. In addition, the effect of synthesis parameters such as microwave time, microwave power, calcination temperature, and calcination time, and operation parameters such as pH, reaction temperature, ultrasonic power and time on sulfur compounds removal was examined. As a result of studying the mechanism behind the piezo-desulfurization reaction, it was found that superoxide radicals and holes played the primary roles in the oxidation of sulfur compounds. As well, the process of desulfurization by CeO2/Ce2O3/NiOx nanocomposites follows a second order reaction.

All data generated or analyzed during this study are included in this published article (and its Supplementary Information files).

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Authors are grateful to the council of University of Razi and University of Raparin to support this work.

Chemistry Department, College of Science, Salahaddin University, Kirkuk Road, 44001, Erbil, Kurdistan Region, Iraq

Sangar S. Ahmed, Karwan M. Rahman, Savana J. Ismael, Noor S. Rasul & Darya Mohammad

Chemistry Department, College of Science, University of Raparin, Rania, Kurdistan Region, Iraq

Omid Amiri & Karukh A. Babakr

Faculty of Chemistry, Razi University, Kermanshah, 67149, Iran

Omid Amiri

Department of Petroleum and Mining Engineering, Faculty of Engineering, Tishk International University, Erbil, Iraq

Nabaz A. Abdulrahman

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S.A. collected and analyzed the data. O.A. designed, supervise project and conceived the idea and wrote the paper. S.A., K.R., S.I., N.R., D.M, and N.A prepared the catalyst, performed most experiments, and collected and analyzed the data. K.B helped to study the kinetics of the reaction. All the authors contributed to discussing and commenting on the manuscript.

Correspondence to Omid Amiri.

The authors declare no competing interests.

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Ahmed, S.S., Amiri, O., Rahman, K.M. et al. Studying the mechanism and kinetics of fuel desulfurization using CexOy/NiOx piezo-catalysts as a new low-temperature method. Sci Rep 13, 7574 (2023). https://doi.org/10.1038/s41598-023-34329-y

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Received: 21 December 2022

Accepted: 27 April 2023

Published: 10 May 2023

DOI: https://doi.org/10.1038/s41598-023-34329-y

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Studying the mechanism and kinetics of fuel desulfurization using CexOy/NiOx piezo