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Journal articles on the topic 'Catalytic cracking'

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Published: 4 June 2021
Last updated: 1 March 2023

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1

Herbst, J. A., H. Owen, and P. H. Schipper. "Catalytic cracking process." Zeolites 11, no. 3 (March 1991): 299. http://dx.doi.org/10.1016/s0144-2449(05)80249-0.

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2

Adewuyi, Y. G., P. M. Adornato, and J. S. Buchanan. "Fluidized catalytic cracking." Zeolites 15, no. 1 (January 1995): 84. http://dx.doi.org/10.1016/0144-2449(95)90250-3.

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3

Istadi, I., Teguh Riyanto, Luqman Buchori, Didi D. Anggoro, Andre W. S. Pakpahan, and Agnes J. Pakpahan. "Biofuels Production from Catalytic Cracking of Palm Oil Using Modified HY Zeolite Catalysts over A Continuous Fixed Bed Catalytic Reactor." International Journal of Renewable Energy Development 10, no. 1 (November 6, 2020): 149–56. http://dx.doi.org/10.14710/ijred.2021.33281.

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The increase in energy demand led to the challenging of alternative fuel development. Biofuels from palm oil through catalytic cracking appear as a promising alternative fuel. In this study, biofuel was produced from palm oil through catalytic cracking using the modified HY zeolite catalysts. The Ni and Co metals were impregnated on the HY catalyst through the wet-impregnation method. The catalysts were characterized using X-ray fluorescence, X-ray diffraction, Brunauer–Emmett–Teller (BET), Pyridine-probed Fourier-transform infrared (FTIR) spectroscopy, and Scanning Electron Microscopy (SEM) methods. The biofuels product obtained was analyzed using a gas chromatography-mass spectrometry (GC-MS) method to determine its composition. The metal impregnation on the HY catalyst could modify the acid site composition (Lewis and Brønsted acid sites), which had significant roles in the palm oil cracking to biofuels. Ni impregnation on HY zeolite led to the high cracking activity, while the Co impregnation led to the high deoxygenation activity. Interestingly, the co-impregnation of Ni and Co on HY catalyst could increase the catalyst activity in cracking and deoxygenation reactions. The yield of biofuels could be increased from 37.32% to 40.00% by using the modified HY catalyst. Furthermore, the selectivity of gasoline could be achieved up to 11.79%. The Ni and Co metals impregnation on HY zeolite has a promising result on both the cracking and deoxygenation process of palm oil to biofuels due to the role of each metal. This finding is valuable for further catalyst development, especially on bifunctional catalyst development for palm oil conversion to biofuels.
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4

Ryabov, V. D., M. A. Silin, O. B. Chernova, and I. A. Bronzova. "Catalytic cracking of triphenylethylene." Petroleum Chemistry 49, no. 4 (July 2009): 297–300. http://dx.doi.org/10.1134/s0965544109040069.

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5

Camblor, M. A., A. Corma, A. Martínez, F. A. Mocholí, and J. Pérez Pariente. "Catalytic cracking of gasoil." Applied Catalysis 55, no. 1 (November 1989): 65–74. http://dx.doi.org/10.1016/s0166-9834(00)82317-9.

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6

Wojciechowski, Bohdan W. "Dichotomies in Catalytic Cracking." Industrial & Engineering Chemistry Research 36, no. 8 (August 1997): 3323–35. http://dx.doi.org/10.1021/ie960642o.

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7

Dwyer, John, and David J. Rawlence. "Fluid catalytic cracking: chemistry." Catalysis Today 18, no. 4 (December 1993): 487–507. http://dx.doi.org/10.1016/0920-5861(93)80065-9.

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8

GONG, Jian-hong, Jun LONG, and You-hao XU. "Protolytic cracking in Daqing VGO catalytic cracking process." Journal of Fuel Chemistry and Technology 36, no. 6 (December 2008): 691–95. http://dx.doi.org/10.1016/s1872-5813(09)60005-0.

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9

Mannanova, G. I., and I. M. Gubaydullin. "Development of fifteen component kinetic model of catalytic cracking process." Computational Mathematics and Information Technologies 3, no. 2 (2019): 104–17. http://dx.doi.org/10.23947/2587-8999-2019-2-2-104-117.

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10

Wang, Yulong, Ruifang Zhao, Chun Zhang, Guanlong Li, Jing Zhang, and Fan Li. "The Investigation of Reducing PAHs Emission from Coal Pyrolysis by Gaseous Catalytic Cracking." Scientific World Journal 2014 (2014): 1–6. http://dx.doi.org/10.1155/2014/528413.

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The catalytic cracking method of PAHs for the pyrolysis gaseous products is proposed to control their pollution to the environment. In this study, the Py-GC-MS is used to investigate in situ the catalytic effect of CaO and Fe2O3on the 16 PAHs from Pingshuo coal pyrolysis under different catalytic temperatures and catalyst particle sizes. The results demonstrate that Fe2O3is effective than that of CaO for catalytic cracking of 16 PAHs and that their catalytic temperature corresponding to the maximum PAHs cracking rates is different. The PAHs cracking rate is up to 60.59% for Fe2O3at 600°C and is 52.88% at 700°C for CaO. The catalytic temperature and particle size of the catalysts have a significant effect on PAHs cracking rate and CaO will lose the capability of decreasing 16 PAHs when the temperature is higher than 900°C. The possible cracking process of 16 PAHs is deduced by elaborately analyzing the cracking effect of the two catalysts on 16 different species of PAHs.
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11

SA, Hosseini. "CFD Simulation of Catalytic Cracking of n-Heptane in a Fixed Bed Reactor." Petroleum & Petrochemical Engineering Journal 4, no. 2 (2020): 1–8. http://dx.doi.org/10.23880/ppej-16000220.

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This work aims to three-dimension computational fluid dynamics (CFD) simulation of n-heptane catalytic cracking in fixed bed reactor (L=0.80 m) and to promote the cracking model of n-heptane using CFD. The catalyst granules were located in middle section of the reactor. The reaction scheme of n-heptane catalytic cracking was involved one primary reaction and 24 secondary reactions. Catalytic cracking process with a model of 25 molecular reactions was simulated by Fluent 6.0 software. The ratio of tube-to-particle diameter was considered N=2. The contours of coke deposition rate, vorticity, velocity and coke precursors and their relations along the reactor were predicted and discussed.
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12

Naik, Desavath V., K. K. Singh, Vimal Kumar, Basheshar Prasad, B. Behera, D. P. Bangwal, Neeraj Atheya, and M. O. Garg. "Catalytic Cracking of Glycerol to Fine Chemicals over Equilibrium Fluid Catalytic Cracking Catalyst." Energy Procedia 54 (2014): 593–98. http://dx.doi.org/10.1016/j.egypro.2014.07.300.

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13

Istadi, I., Teguh Riyanto, Luqman Buchori, Didi Dwi Anggoro, Roni Ade Saputra, and Theobroma Guntur Muhamad. "Effect of Temperature on Plasma-Assisted Catalytic Cracking of Palm Oil into Biofuels." International Journal of Renewable Energy Development 9, no. 1 (February 4, 2020): 107–12. http://dx.doi.org/10.14710/ijred.9.1.107-112.

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Plasma-assisted catalytic cracking is an attractive method for producing biofuels from vegetable oil. This paper studied the effect of reactor temperature on the performance of plasma-assisted catalytic cracking of palm oil into biofuels. The cracking process was conducted in a Dielectric Barrier Discharge (DBD)-type plasma reactor with the presence of spent RFCC catalyst. The reactor temperature was varied at 400, 450, and 500 ºC. The liquid fuel product was analyzed using a gas chromatography-mass spectrometry (GC-MS) to determine the compositions. Result showed that the presenceof plasma and catalytic role can enhance the reactor performance so that the selectivity of the short-chain hydrocarbon produced increases. The selectivity of gasoline, kerosene, and diesel range fuels over the plasma-catalytic reactor were 16.43%, 52.74% and 21.25%, respectively, while the selectivity of gasoline, kerosene and diesel range fuels over a conventional fixed bed reactor was 12.07%, 39.07%, and 45.11%, respectively. The increasing reactor temperature led to enhanced catalytic role of cracking reaction,particularly directing the reaction to the shorter hydrocarbon range. The reactor temperature dependence on the liquid product components distribution over the plasma-catalytic reactor was also studied. The aromatic and oxygenated compounds increased with the reactor temperature.©2020. CBIORE-IJRED. All rights reserved
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14

Rabeeah Taj, Rabeeah Taj, Erum Pervaiz Erum Pervaiz, and Arshad Hussain Arshad Hussain. "Synthesis and Catalytic Activity of IM-5 Zeolite as Naphtha Cracking Catalyst for Light Olefins: A Review." Journal of the chemical society of pakistan 42, no. 2 (2020): 305. http://dx.doi.org/10.52568/000637.

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Light olefins are the backbone of modern industrialization. Olefins are used as feedstock for production of various industrial products such as synthetic fibers, construction materials, textiles, rubber and other chemicals in the petrochemical industry. For more than a half-century, steam/thermal hydrocarbon cracking is considered as the main route and conventional process for light olefins yield. Few drawbacks of conventional steam cracking such as extensive energy consumption, requirements of high temperature and pressure conditions, the difficult selectivity of particular light olefins and excess emission of CO2 relate to this technology, which cannot accommodate further needs regarding the chemical process industry. Steam cracking also poses a threat to uncontrolled heat. Catalytic cracking of hydrocarbons is highly appreciated as it is a less energy consuming (low temperature and pressure conditions) and an environment-friendly process for light olefins production. Catalytic cracking has been under consideration as a favorable alternative but still depends upon catalyst, its activity, and selectivity for a particular product. Catalytic cracking is quite beneficial for industrial scale. The present proficiency of refining and petro-chemistry to a great extent is based on highly active, selective, and durable catalysts. Various catalysts possess compositional diversity, surface area, and surface energy and hence provide a different pathway for the reaction to occur. Petroleum-extracted naphtha cracking technique now a days is the main process for light olefins yield. This review highlights the use of IM-5 zeoliteas an emerging catalyst for naphtha cracking process as compared to conventional catalysts in the last few decades. Structure, synthesis techniques and catalytic activity of IM-5 zeolite is reviewed. Different zeolites which can be used in naphtha cracking reactor and their applications in the catalytic cracking of hydrocarbons have been studied. This review provides a significant insight into catalytic activity comparison between conventional zeolites and IM-5 zeolite.
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15

Rabeeah Taj, Rabeeah Taj, Erum Pervaiz Erum Pervaiz, and Arshad Hussain Arshad Hussain. "Synthesis and Catalytic Activity of IM-5 Zeolite as Naphtha Cracking Catalyst for Light Olefins: A Review." Journal of the chemical society of pakistan 42, no. 2 (2020): 305. http://dx.doi.org/10.52568/000637/jcsp/42.02.2020.

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Light olefins are the backbone of modern industrialization. Olefins are used as feedstock for production of various industrial products such as synthetic fibers, construction materials, textiles, rubber and other chemicals in the petrochemical industry. For more than a half-century, steam/thermal hydrocarbon cracking is considered as the main route and conventional process for light olefins yield. Few drawbacks of conventional steam cracking such as extensive energy consumption, requirements of high temperature and pressure conditions, the difficult selectivity of particular light olefins and excess emission of CO2 relate to this technology, which cannot accommodate further needs regarding the chemical process industry. Steam cracking also poses a threat to uncontrolled heat. Catalytic cracking of hydrocarbons is highly appreciated as it is a less energy consuming (low temperature and pressure conditions) and an environment-friendly process for light olefins production. Catalytic cracking has been under consideration as a favorable alternative but still depends upon catalyst, its activity, and selectivity for a particular product. Catalytic cracking is quite beneficial for industrial scale. The present proficiency of refining and petro-chemistry to a great extent is based on highly active, selective, and durable catalysts. Various catalysts possess compositional diversity, surface area, and surface energy and hence provide a different pathway for the reaction to occur. Petroleum-extracted naphtha cracking technique now a days is the main process for light olefins yield. This review highlights the use of IM-5 zeoliteas an emerging catalyst for naphtha cracking process as compared to conventional catalysts in the last few decades. Structure, synthesis techniques and catalytic activity of IM-5 zeolite is reviewed. Different zeolites which can be used in naphtha cracking reactor and their applications in the catalytic cracking of hydrocarbons have been studied. This review provides a significant insight into catalytic activity comparison between conventional zeolites and IM-5 zeolite.
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16

Patel, Rajesh, Dawei Wang, Chao Zhu, and Teh C. Ho. "Effect of injection zone cracking on fluid catalytic cracking." AIChE Journal 59, no. 4 (September 26, 2012): 1226–35. http://dx.doi.org/10.1002/aic.13902.

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17

Olaremu, Abimbola G., Williams R. Adedoyin, Odunayo T. Ore, and Adedapo O. Adeola. "Sustainable development and enhancement of cracking processes using metallic composites." Applied Petrochemical Research 11, no. 1 (January 23, 2021): 1–18. http://dx.doi.org/10.1007/s13203-021-00263-1.

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AbstractMetallic composites represent a vital class of materials that has gained increased attention in crude oil processing as well as the production of biofuel from other sources in recent times. Several catalytic materials have been reported in the literature for catalytic cracking, particularly, of crude oil. This review seeks to provide a comprehensive overview of existing and emerging methods/technologies such as metal–organic frameworks (MOFs), metal–matrix composites (MMCs), and catalytic support materials, to bridge information gaps toward sustainable advancement in catalysis for petrochemical processes. There is an increase in industrial and environmental concern emanating from the sulphur levels of oils, hence the need to develop more efficient catalysts in the hydrotreatment (HDS and HDN) processes, and combating the challenge of catalyst poisoning and deactivation; in a bid to improving the overall quality of oils and sustainable use of catalyst. Structural improvement, high thermal stability, enhanced cracking potential, and environmental sustainability represent the various benefits accrued to the use of metallic composites as opposed to conventional catalysts employed in catalytic cracking processes.
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18

Nurmukhametova, E. R., A. F. Akhmetov, and A. R. Rakhmatullin. "Research of catalytic cracking gasoline." Oil and Gas Business, no. 2 (April 2014): 181–93. http://dx.doi.org/10.17122/ogbus-2014-2-181-193.

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19

Gómez, Maria Elizabeth, Clemencia Vargas, and Javier Lizcano. "PETROCHEMICAL PROMOTERS IN CATALYTIC CRACKING." CT&F - Ciencia, Tecnología y Futuro 3, no. 5 (December 31, 2009): 143–58. http://dx.doi.org/10.29047/01225383.454.

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This study is based on the current scheme followed by a refinery with available Catalytic Cracking capacity to process new feedstocks such as Straight Run Naphtha and Naphthas from FCC. These feedstocks are of petrochemical interest to produce Ethane, Ethylene, Propylene, i-Butane, Toluene and Xylene. To evaluate the potential of these new streams versus the Cracking-charged Residues, it was performed a detailed chemical analysis on the structural groups in carbons [C1-C12] at the reactor product obtained in pilot plant. A catalyst with and without Propylene - Promoter Additive was used. This study analyzes the differences in the chemical composition of the feedstocks, relating them to the yield of each petrochemical product. Straight Run Naphthas with a high content of Naphthenes, and Paraffines n[C5-C12] and i[C7-C12] are selective to the production of i-Butane and Propane, while Naphthas from FCC with a high content of n[C5-C12]Olefins, i-Olefins, and Aromatics are more selective to Propylene, Toluene, and Xylene. Concerning Catalytic Cracking of Naphthas, the Additive has similar selectivity for all the petrochemical products, their yields increase by about one point with 4%wt of Additive, while in cracking of Residues, the Additive increases in three points Propylene yield, corresponding to a selectivity of 50% (ΔC3= / ΔLPG).
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20

Corma, A., and B. W. Wojciechowski. "The Chemistry of Catalytic Cracking." Catalysis Reviews 27, no. 1 (January 1985): 29–150. http://dx.doi.org/10.1080/01614948509342358.

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21

CHENG, W. C., G. KIM, A. W. PETERS, X. ZHAO, K. RAJAGOPALAN, M. S. ZIEBARTH, and C. J. PEREIRA. "Environmental Fluid Catalytic Cracking Technology." Catalysis Reviews 40, no. 1-2 (February 1998): 39–79. http://dx.doi.org/10.1080/01614949808007105.

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22

Billaud, F., A. K. Tran Minh, P. Lozano, and D. Pioch. "Catalytic cracking of octanoic acid." Journal of Analytical and Applied Pyrolysis 58-59 (April 2001): 605–16. http://dx.doi.org/10.1016/s0165-2370(00)00144-3.

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23

Lee, Fu Ming. "Catalytic cracking under hydrogen fluidization." Industrial & Engineering Chemistry Research 28, no. 7 (July 1989): 920–25. http://dx.doi.org/10.1021/ie00091a006.

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24

Parris, G. E., and J. N. Armor. "Catalytic cracking of organic amides." Applied Catalysis 78, no. 1 (October 1991): 45–64. http://dx.doi.org/10.1016/0166-9834(91)80088-e.

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25

Parris, G. E., and J. N. Armor. "Catalytic cracking of organic amides." Applied Catalysis 78, no. 1 (October 1991): 65–78. http://dx.doi.org/10.1016/0166-9834(91)80089-f.

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26

Li, Zekun, Gang Wang, Yindong Liu, Hao Wang, Yongmei Liang, Chunming Xu, and Jinsen Gao. "Catalytic Cracking Constraints Analysis and Divisional Fluid Catalytic Cracking Process for Coker Gas Oil." Energy & Fuels 26, no. 4 (March 21, 2012): 2281–91. http://dx.doi.org/10.1021/ef201893s.

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27

Pujro, Richard, Marisa Falco, and Ulises Sedran. "Catalytic Cracking of Heavy Aromatics and Polycyclic Aromatic Hydrocarbons over Fluidized Catalytic Cracking Catalysts." Energy & Fuels 29, no. 3 (March 2, 2015): 1543–49. http://dx.doi.org/10.1021/ef502707w.

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28

Hafnee Lateh, Juntakan Taweekun, Kittinan Maliwan, Zainal Alimuddin Zainal Alauddin, and Sukritthira Rattanawilai. "The Removal of Biomass Tar Derived Producer Gas by Means of Thermal and Catalytic Cracking Methods." Journal of Advanced Research in Fluid Mechanics and Thermal Sciences 88, no. 2 (November 1, 2021): 147–56. http://dx.doi.org/10.37934/arfmts.88.2.147156.

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Tar derived from biomass gasification system needs to be eliminated before applying biomass producer gas for avoiding equipment and its gas problems. In this study, thermal and catalytic cracking methods of biomass tar along with microwave assistance in heat transfer were experimented at various temperatures during 650-1,200 °C and residence at 0.24-0.5 s. The results present that high tar removal efficiency by approximately 90 % under thermal cracking treatment and about 98 % with catalytic cracking method. It also shows that the catalytic cracking especially modified catalyst could be lowered carbon deposition on catalyst surface.
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29

Wang, Chuansheng, Xiaolong Tian, Baishun Zhao, Lin Zhu, and Shaoming Li. "Experimental Study on Spent FCC Catalysts for the Catalytic Cracking Process of Waste Tires." Processes 7, no. 6 (June 1, 2019): 335. http://dx.doi.org/10.3390/pr7060335.

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Research on the synergistic high-value reuse of waste tires and used catalysts in spent fluid catalytic cracking (FCC) catalysts was carried out in this study to address the serious ecological and environmental problems caused by waste tires and spent FCC catalysts. The experiment, in which a spent FCC catalyst was applied to the catalytic cracking of waste tires, fully utilized the residual activity of the spent FCC catalyst and was compared with a waste tire pyrolysis experiment. The comparative experimental results indicated that the spent FCC catalyst could improve the cracking efficiency of waste tires, increase the output of light oil in pyrolysis products, and improve the quality of pyrolysis oil. It could also be used for the conversion of sulfur compounds during cracking. The content of 2-methyl-1-propylene in catalytic cracking gas was found to be up to 65.59%, so a new method for producing high-value chemical raw materials by the catalytic cracking of waste tires with spent FCC catalysts is proposed.
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30

Istadi, Istadi, Luqman Buchori, Didi Dwi Anggoro, Teguh Riyanto, Anindita Indriana, Chusnul Khotimah, and Fachmy Adji Pangestu Setiawan. "Effects of Ion Exchange Process on Catalyst Activity and Plasma-Assisted Reactor Toward Cracking of Palm Oil into Biofuels." Bulletin of Chemical Reaction Engineering & Catalysis 14, no. 2 (August 1, 2019): 459. http://dx.doi.org/10.9767/bcrec.14.2.4257.459-467.

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Biofuels can be produced through a conventional catalytic cracking system and/or a hybrid catalytic-plasma cracking system. This paper was focused on studying effect of Na+ ion exchange to HY-Zeolite catalyst on catalyst performance to convert palm oil into biofuels over a conventional continuous fixed bed catalytic cracking reactor and comparing the catalytic cracking performance when carried out in a continuous hybrid catalytic-plasma reactor. The catalysts were characterized by X-ray Diffraction (XRD) and Bruneuer-Emmet-Teller (BET) surface area methods. The biofuels product were analyzed using Gas Chromatography-Mass Spectrometry (GC-MS) to determine the hydrocarbons composition of biofuels product. From the results, ion exchange process of Na+ into HY-Zeolite catalyst decreases the catalyst activity due to decreasing the number of active sites caused by blocking of Na+ ion. The selectivity to gasoline ranges achieved 34.25% with 99.11% total conversion when using HY catalyst over conventional continuous fixed bed reactor system. Unfortunately, the selectivity to gasoline ranges decreased to 13.96% and the total conversion decrease slightly to 98.06% when using NaY-Zeolite catalyst. As comparison when the cracking reaction was carried out in a hybrid catalytic-plasma reactor using a spent residual catalytic cracking (RCC) catalyst, the high energetics electron from plasma can improve the reactor performance, where the conversion and yield were increased and the selectivity to lower ranges of hydrocarbons was increased. However, the last results were potential to be intensively studied with respect to relation between reactor temperature and plasma-assisted catalytic reactor parameters. Copyright © 2019 BCREC Group. All rights reserved
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31

Han, Yueyang, Lingyin Du, Yuan Zhu, Youhao Xu, Xuhui Bai, Ying Ouyang, Yibin Luo, and Xingtian Shu. "High-Temperature Cracking of Pentene to Ethylene and Propylene over H-ZSM-5 Zeolites: Effect of Reaction Conditions and Mechanistic Insights." Catalysts 13, no. 1 (December 30, 2022): 73. http://dx.doi.org/10.3390/catal13010073.

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The effects of reaction conditions on the yield of ethylene and propylene from pentene cracking were investigated in a fixed-bed reactor at 500–750 °C and for a weight hourly space velocity (WHSV) of 15–83 h−1. The total yield of ethylene and propylene reached a maximum (67.8 wt%) at 700 °C and 57 h−1. In order to explore the reaction mechanism at high temperatures, a thermal/catalytic cracking proportion model was established. It was found that the proportion of pentene feed chemically adsorbed with the acid sites and cracked through catalytic cracking was above 88.4%, even at 750 °C. Ethylene and propylene in the products were mainly derived from catalytic cracking rather than thermal cracking at 650–750 °C. In addition, the suitable reaction network for pentene catalytic cracking was deduced and estimated. The results showed that the monomolecular cracking proportion increased from 1% at 500 °C to 95% at 750 °C. The high selectivity of ethylene and propylene at high temperatures was mainly due to the intensification of the monomolecular cracking reaction. After 20 times of regeneration, the acidity and pore structure of the zeolite had hardly changed, and the conversion of pentene remained above 80% at 650 °C.
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32

Ulfiati, Ratu. "CATALYTIC PERFORMANCE OF ZSM-5 ZEOLITE IN HEAVY HYDROCARBON CATALYTIC CRACKING: A REVIEW." Scientific Contributions Oil and Gas 42, no. 1 (August 6, 2020): 29–34. http://dx.doi.org/10.29017/scog.42.1.384.

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Low quality heavy oils and residues, which are subsequently obtained by processing heavy crudes, are considered as alternate suitable source for transportation fuels, energy and petrochemicals. ZSM-5 zeolite with high Si/Al ratio and modified with phosphorous and La has showed not only high selectivity to light olefins but also high hydrothermal stability for the steam catalytic cracking of naphtha. Kaolin is promising natural resource as raw material to synthesis of ZSM-5 zeolite. The utilization of acid catalysts with large pore size or hierarchically structured and high hydrothermal stability to resist the severity of the steam catalytic cracking (or thermal and catalytic cracking) operation conditions to maximize the olefin production.
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33

Tang, Shanshan, Yan He, Xingfa Deng, and Xuemin Cui. "Thermal Catalytic-Cracking Low-Density Polyethylene Waste by Metakaolin-Based Geopolymer NaA Microsphere." Molecules 27, no. 8 (April 15, 2022): 2557. http://dx.doi.org/10.3390/molecules27082557.

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Metakaolin-based geopolymer microspheres (MGM) with hierarchical pore structures were prepared by suspension dispersion method in dimethicone at 80 °C. The hydrothermal modification of MGM was carried out at a lower temperature of 80 °C, and a NaA molecular sieve converted from metakaolin-based geopolymer (NMGM) with good crystal structure was prepared and applied in thermal catalytic cracking of low-density polyethylene (LDPE) reaction. The one-pot two-stage thermal catalytic cracking of LDPE was carried out in a 100 mL micro-autoclave under normal pressure. In this work, the optimal proportions and optimal reaction conditions of catalysts for NMGM thermal catalytic cracking of LDPE waste to fuel oil were investigated. The NMGM catalyst showed high selectivity to the liquid product of thermal catalytic cracking of waste LDPE. Under the reaction conditions of reaction time of 1 h and reaction temperature of 400 °C, the liquid-phase yield of thermal catalytic cracking of LDPE reached a high of 88.45%, of which the content of gasoline components was 10.14% and the content of diesel components was 80.97%.
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34

Castellanos, E. steban, Hans Neumann, and Ing Jose Prieto. "THERMAL CRACKING, THERMAL HYDROCRACKIKG AND CATALYTIC CRACKING OF DEASPHALTED OILS." Petroleum Science and Technology 11, no. 12 (1993): 1731–58. http://dx.doi.org/10.1080/08843759308916156.

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35

Khongprom, Parinya, Supawadee Ratchasombat, Waritnan Wanchan, Panut Bumphenkiattikul, and Sunun Limtrakul. "Scaling of catalytic cracking fluidized bed downer reactor based on CFD simulations—Part II: effect of reactor scale." RSC Advances 12, no. 33 (2022): 21394–405. http://dx.doi.org/10.1039/d2ra03448d.

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The modified scaling law based on the similitude method for a catalytic cracking downer reactor was proposed for various reactor scales. An excellent similarity of chemical performance of complex catalytic cracking was obtained.
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36

Mansur, Dieni, Aminuddin Aminuddin, and Verina J. Wargadalam. "Production of Bio-hydrocarbon from Refined-Bleach-Deodorized Palm Oil using Micro Activity Test Reactor." Reaktor 20, no. 2 (June 30, 2020): 75–80. http://dx.doi.org/10.14710/reaktor.20.2.75-80.

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Catalytic cracking of vegetable oil for the production of bio-hydrocarbons had been developed. In this study, the catalytic cracking of Refined-Bleach-Deodorized Palm Oil (RBDPO) had carried out over Fluid Catalytic Cracking Unit (FCCU) equilibrium catalyst in a micro activity test reactor at 510°C under various catalyst to oil (CTO) ratio of 1.20 - 2.01 g/g. The catalytic cracking of RBDPO had produced the organic liquid product (OLP) containing bio-hydrocarbon, water, gas, and coke on the catalyst converted to CO2 during the catalyst regeneration process. The increase in CTO ratio from 1.20 to 2.01, OLP yield decreased from 80.48% to 70.12%. The OLP was separated into gasoline, light cycle oil (LCO), and heavy cycle oil (HCO) based on boiling point difference by a simulated distillation gas chromatography (SimDis GC). High gasoline fraction as 31.56% was produced at CTO of 2.01 g/g. The gasoline fraction contained olefins, aromatics, paraffin, iso-paraffins, and a small amount of naphthenes and oxygenates. The presence of chemicals in the gasoline fraction influenced the research octane number (RON) of the fuel.Keyword: bio-hydrocarbon; catalytic cracking; micro activity test reactor; RBDPO
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37

KITAZATO, Hajime, Sachio ASAOKA, and Hiroaki IWAMOTO. "Catalytic cracking of hydrocarbons from microalgae." Journal of The Japan Petroleum Institute 32, no. 1 (1989): 28–34. http://dx.doi.org/10.1627/jpi1958.32.28.

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Moore, Howard F., Sharon L. Mayo, and Terry L. Goolsby. "CATALYTIC CRACKING OF RESIDUAL PETROLEUM FRACTIONS." Fuel Science and Technology International 9, no. 3 (April 1991): 283–303. http://dx.doi.org/10.1080/08843759108942266.

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39

Liu, Yu, and Thomas J. Pinnavaia. "Aluminosilicate Nanoparticles for Catalytic Hydrocarbon Cracking." Journal of the American Chemical Society 125, no. 9 (March 2003): 2376–77. http://dx.doi.org/10.1021/ja029336u.

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40

MONGE, J. J., and C. GEORGAKIS. "MULTIVARIABLE CONTROL OF CATALYTIC CRACKING PROCESSES." Chemical Engineering Communications 61, no. 1-6 (November 1987): 197–225. http://dx.doi.org/10.1080/00986448708912039.

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41

Feng, Wu, Erik Vynckier, and Gilbert F. Froment. "Single event kinetics of catalytic cracking." Industrial & Engineering Chemistry Research 32, no. 12 (December 1993): 2997–3005. http://dx.doi.org/10.1021/ie00024a007.

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42

Biswas, J., and I. E. Maxwell. "Octane enhancement in fluid catalytic cracking." Applied Catalysis 58, no. 1 (February 1990): 1–18. http://dx.doi.org/10.1016/s0166-9834(00)82274-5.

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43

Biswas, J., and I. E. Maxwell. "Octane enhancement in fluid catalytic cracking." Applied Catalysis 58, no. 1 (February 1990): 19–27. http://dx.doi.org/10.1016/s0166-9834(00)82275-7.

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44

Chen, Nai Y., and Stanley J. Lucki. "Nonregenerative catalytic cracking of gas oils." Industrial & Engineering Chemistry Process Design and Development 25, no. 3 (July 1986): 814–20. http://dx.doi.org/10.1021/i200034a038.

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Gaile, A. A., A. P. Khvorov, G. D. Zalishchevskii, O. M. Varshavskii, and L. V. Semenov. "Extraction treatment of catalytic cracking feedstock." Chemistry and Technology of Fuels and Oils 41, no. 1 (January 2005): 27–31. http://dx.doi.org/10.1007/s10553-005-0016-5.

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Rustamov, M. I., G. T. Farkhadova, S. A. Dorofeev, and N. S. Maiorova. "Model unit for continuous catalytic cracking." Chemistry and Technology of Fuels and Oils 27, no. 6 (June 1991): 293–96. http://dx.doi.org/10.1007/bf00718993.

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Farkhadova, G. T., M. I. Rustamov, A. A. Mkrtychev, A. M. Guseinov, N. S. Maiorova, and S. B. Guseinova. "Catalytic cracking of light coker gasoil." Chemistry and Technology of Fuels and Oils 21, no. 2 (February 1985): 57–62. http://dx.doi.org/10.1007/bf00719676.

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48

Farag, Ihab H., and Kun-Yung Tsai. "Simulation of fluid catalytic cracking operation." Mathematical Modelling 8 (1987): 311–16. http://dx.doi.org/10.1016/0270-0255(87)90596-3.

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Caldeira, Vinícius P. S., Anne G. D. Santos, Daniele S. Oliveira, Rafael B. Lima, Luiz D. Souza, and Sibele B. C. Pergher. "Polyethylene catalytic cracking by thermogravimetric analysis." Journal of Thermal Analysis and Calorimetry 130, no. 3 (July 3, 2017): 1939–51. http://dx.doi.org/10.1007/s10973-017-6551-6.

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50

Payá, J., J. Monzó, and M. V. Borrachero. "Fluid catalytic cracking catalyst residue (FC3R)." Cement and Concrete Research 29, no. 11 (November 1999): 1773–79. http://dx.doi.org/10.1016/s0008-8846(99)00164-7.

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