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Journal articles on the topic 'Light Naphtha'

Author: Grafiati

Published: 4 June 2021

Last updated: 5 February 2022

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1

Lengyel, A., S. Magyar, D. Kalló, and J. Hancsók. "Catalytic Coprocessing of Delayed Coker Light Naphtha with Light Straight-run Naphtha/FCC Gasoline." Petroleum Science and Technology 28, no. 9 (2010): 946–54. http://dx.doi.org/10.1080/10916460902937059.

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2

Chuzlov, Viacheslav A., Emilia D. Ivanchina, Igor’ M. Dolganov, and Konstantin V. Molotov. "Simulation of Light Naphtha Isomerization Process." Procedia Chemistry 15 (2015): 282–87. http://dx.doi.org/10.1016/j.proche.2015.10.045.

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3

Li, Dadong, Mingfeng Li, Yang Chu, Hong Nie, and Yahua Shi. "Skeletal isomerization of light FCC naphtha." Catalysis Today 81, no. 1 (2003): 65–73. http://dx.doi.org/10.1016/s0920-5861(03)00103-2.

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4

Valavarasu, G., and B. Sairam. "Light Naphtha Isomerization Process: A Review." Petroleum Science and Technology 31, no. 6 (2013): 580–95. http://dx.doi.org/10.1080/10916466.2010.504931.

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5

Kozlov, I. T., V. A. Khavkin, and B. K. Nefedov. "Selective hydrocracking of light naphtha cuts." Chemistry and Technology of Fuels and Oils 21, no. 7 (1985): 346–49. http://dx.doi.org/10.1007/bf00723841.

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6

M. Hussain, Halah, and Abdulhaleem A.K. Mohammed. "Experimental Study of Iraqi Light Naphtha Isomerization over Ni-Pt/H-Mordenite." Iraqi Journal of Chemical and Petroleum Engineering 20, no. 4 (2019): 61–66. http://dx.doi.org/10.31699/ijcpe.2019.4.10.

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Hydroisomerization of Iraqi light naphtha was studied on prepared Ni-Pt/H-mordenite catalyst at a temperature range of 220-300°C, hydrogen to hydrocarbon molar ratio of 3.7, liquid hourly space velocity (LHSV) 1 hr-1 and at atmospheric pressure. The result shows that the hydrisomerization of light naphtha increases with the increase in reaction temperature at constant LHSV. However, above 270 0C the isomers formation decreases and the reaction is shifted towards the hydrocracking reaction, a higher octane number of naphtha was formed at 270 °C.

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7

Cheng, Qi-tong, Ben-xian Shen, Hui Sun, Ji-gang Zhao, and Ji-chang Liu. "Methanol promoted naphtha catalytic pyrolysis to light olefins on Zn-modified high-silicon HZSM-5 zeolite catalysts." RSC Advances 9, no. 36 (2019): 20818–28. http://dx.doi.org/10.1039/c9ra02793a.

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Exploring the relationship between the properties and catalytic reactivity of the Zn-modified high-silicon ZSM-5 in the methanol/naphtha coupling reaction and achieving the efficient utilization of naphtha.

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8

Schmidt, Roland, M. Bruce Welch, and Bruce B. Randolph. "Oligomerization of C5Olefins in Light Catalytic Naphtha." Energy & Fuels 22, no. 2 (2008): 1148–55. http://dx.doi.org/10.1021/ef800005v.

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9

Vemot, E. H., R. T. Drew, and M. L. Kane. "Acute Toxicologic Evaluation of Light Alkyklate Naphtha." Journal of the American College of Toxicology 1, no. 2 (1990): 124. http://dx.doi.org/10.1177/109158189000100244.

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10

Hammadi, Ahmed Najeeb, and Ibtehal K. Shakir. "Adsorption Behavior of Light Naphtha Components on Zeolite (5A) and Activated Carbon." Iraqi Journal of Chemical and Petroleum Engineering 20, no. 4 (2019): 27–33. http://dx.doi.org/10.31699/ijcpe.2019.4.5.

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Light naphtha one of the products from distillation column in oil refineries used as feedstock for gasoline production. The major constituents of light naphtha are (Normal Paraffin, Isoparaffin, Naphthene, and Aromatic). In this paper, we used zeolite (5A) with uniform pores size (5Aº) to separate normal paraffin from light naphtha, due to suitable pore size for this process and compare the behavior of adsorption with activated carbon which has a wide range of pores size (micropores and mesopores) and high surface area. The process is done in a continuous system - Fixed bed reactor- at the vapor phase with the constant conditions of flow rate 5 ml/min, temperature 180oC, pressure 1.6 bar and 100-gram weight of each adsorbents. We notice that the molecular sieve (5A) separated the normal paraffin (C4 – C8) from light naphtha feed until equilibrium (saturation). Activated carbon separated naphthene and aromatics, in addition, the other component of normal paraffin C6 (n-hexane), C7 (n-heptane) and C8 (n-octane). And there is increasing in weight percentage of C4 (n-butane), C5 (n-pentane) and the weight percentage of isoparaffin until equilibrium (Saturation). The study showed the difference in physical adsorption behavior and the effect of pore size on these processes.

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11

Knyazevaa, Tamar, and Tat'yana Raskulova. "TECHNOLOGY OF LIGHT NAPHTHA ISOMERIZATION IN PRACTICE PETROLEUM REFINING." Modern Technologies and Scientific and Technological Progress 2020, no. 1 (2020): 37–38. http://dx.doi.org/10.36629/2686-9896-2020-1-37-38.

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12

KATO, Koichi, and Satoshi FUKASE. "Light Naphtha Aromatization(LNA) Process for Aromatics Production." Journal of The Japan Petroleum Institute 37, no. 1 (1994): 77–83. http://dx.doi.org/10.1627/jpi1958.37.77.

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13

KATO, Koichi, Satoshi FUKASE, Toru AMAYA, and Yasukazu SATO. "Reaction Modeling of Light Naphtha Aromatization(LNA) Process." Journal of The Japan Petroleum Institute 38, no. 1 (1995): 9–18. http://dx.doi.org/10.1627/jpi1958.38.9.

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14

KATO, Koichi, Satoshi FUKASE, and Manabu YAMAMOTO. "Catalyst Regeneration in Light Naphtha Aromatization(LNA) Process." Journal of The Japan Petroleum Institute 39, no. 4 (1996): 290–95. http://dx.doi.org/10.1627/jpi1958.39.290.

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15

Vemot, E. H., R. T. Drew, and M. L. Kane. "Acute Toxicologic Evaluation of Light Catalytic Cracked Naphtha." Journal of the American College of Toxicology 1, no. 2 (1990): 117–18. http://dx.doi.org/10.1177/109158189000100237.

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16

Vemot, E. H., R. T. Drew, and M. L. Kane. "Acute Toxicologic Evaluation of Light Catalytic Cracked Naphtha." Journal of the American College of Toxicology 1, no. 2 (1990): 118–19. http://dx.doi.org/10.1177/109158189000100238.

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17

Vemot, E. H., R. T. Drew, and M. L. Kane. "Acute Toxicologic Evaluation of Light Catalytic Cracked Naphtha." Journal of the American College of Toxicology 1, no. 2 (1990): 119–20. http://dx.doi.org/10.1177/109158189000100239.

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18

Vemot, E. H., R. T. Drew, and M. L. Kane. "Acute Toxicologic Evaluation of Light Catalytic Reformed Naphtha." Journal of the American College of Toxicology 1, no. 2 (1990): 121. http://dx.doi.org/10.1177/109158189000100241.

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19

Abbas, Mohammmed Nsaif, and Suha Anwer Ibrahim. "Catalytic and thermal desulfurization of light naphtha fraction." Journal of King Saud University - Engineering Sciences 32, no. 4 (2020): 229–35. http://dx.doi.org/10.1016/j.jksues.2019.08.001.

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20

Akah, Aaron, Musaed Al-Ghrami, Mian Saeed, and M. Abdul Bari Siddiqui. "Reactivity of naphtha fractions for light olefins production." International Journal of Industrial Chemistry 8, no. 2 (2016): 221–33. http://dx.doi.org/10.1007/s40090-016-0106-8.

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21

Benallal, B., C. Roy, H. Pakdel, S. Chabot, and M. A. Poirier. "Characterization of pyrolytic light naphtha from vacuum pyrolysis of used tyres comparison with petroleum naphtha." Fuel 74, no. 11 (1995): 1589–94. http://dx.doi.org/10.1016/0016-2361(95)00165-2.

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22

Feng, Minchao, Xiaolong Zhou, Wei Hu, Wenyan Wang, and Chenglie Li. "Improved separation and utilization of light naphtha stock by adsorption process." Adsorption Science & Technology 36, no. 1-2 (2017): 732–42. http://dx.doi.org/10.1177/0263617417721571.

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An integrated process for separation and utilization of light naphtha stock in refineries is discussed in this paper. Normal paraffins present in light naphtha streams are first separated from nonnormal paraffins by adsorption technology. The adsorbed n-paraffins are recovered and can be used as an ideal feedstock for steam cracking, meanwhile iso-pentane or iso-pentane and iso-hexane blends are recovered by rectification of the nonadsorbed effluent and used as necessary components for modern gasoline or aviation gasoline products. From the results for a model feedstock, an isothermal adsorption and purging desorption approach is selected. Optimum parameters consist of adsorption and desorption duration of 30 min at 180℃ for each, nitrogen stream LHSV of 240 h−1 in the desorption step, the dynamic capacity of the adsorbent reaches 0.042 g/g.

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23

Zhang, Bin, Zhishan Bai, Bingjie Wang, and Huiqing Luo. "Highly efficient methyldiethanolamine (MDEA) removal and light naphtha purificationviasynergistic effect of molecular sieves and fixed adsorption bed." RSC Advances 9, no. 28 (2019): 15727–37. http://dx.doi.org/10.1039/c9ra00308h.

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24

Ali, Noha Muhsen, and Tariq Mohammed Naife. "Removal of Vanadium and Nickel Ions from Iraqi Atmospheric Residue by Using Solvent Extraction Method." Iraqi Journal of Chemical and Petroleum Engineering 22, no. 1 (2021): 15–20. http://dx.doi.org/10.31699/ijcpe.2021.1.2.

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Iraqi crude Atmospheric residual fraction supplied from al-Dura refinery was treated to remove metals contaminants by solvent extraction method, with various hydrocarbon solvents and concentrations. The extraction method using three different type solvent (n-hexane, n-heptane, and light naphtha) were found to be effective for removal of oil-soluble metals from heavy atmospheric residual fraction. Different solvents with using three different hydrocarbon solvents (n-hexane, n-heptane, and light naphtha) .different variables were studied solvent/oil ratios (4/1, 8/1, 10/1, 12/1, and 15/1), different intervals of perceptual (15, 30-60, 90 and 120 min) and different temperature (30, 45, 60 and 90 °C) were used. The metals removal percent were found depending on the yield of asphaltene. The solvent-oil ratio had important effects on the amount of metal removal. The metals removal was increased at increasing temperatures from 30 to 90 0C increases the metal ion precipitated. The highest Ni precipitated was 79.23 ppm using heptane at 90 0C while for V the highest value was 64.51 ppm using also heptane at 90 0C, while the mixing time decreased metals removal. With increasing asphalt yield, the removal of metal was more selective. Among the solvents used in the extraction treatment method, the highest Ni precipitated was 76 ppm using hexane at 150 ml solvent and showed the most promising results. Increasing mixing time increases metals removal for V, the highest value was 65.51 ppm using either heptane or light naphtha. The highest Ni precipitated was 78 ppm using heptane at 120 min while for V the highest value was 67 ppm using either heptane or light naphtha after 120 min.

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25

Pérez-Romo, Patricia, Candido Aguilar-Barrera, Juan Navarrete-Bolaños, Luis M. Rodríguez-Otal, Francisco Hernández Beltrán, and José Fripiat. "Silica poisoning in HDT catalysts by light coker naphtha." Applied Catalysis A: General 449 (December 2012): 183–87. http://dx.doi.org/10.1016/j.apcata.2012.10.001.

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26

Chekantsev, Nikita V., Maria S. Gyngazova, and Emilia D. Ivanchina. "Mathematical modeling of light naphtha (C5, C6) isomerization process." Chemical Engineering Journal 238 (February 2014): 120–28. http://dx.doi.org/10.1016/j.cej.2013.08.088.

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27

Panfilov, Nikita, and Ivan Semenov. "PROBLEM POINTS OF LIGHT-NAPHTHA RECTIFICATION PROCESS OF ISOMERIZATION TECHNOLOGY." Modern Technologies and Scientific and Technological Progress 2020, no. 1 (2020): 57–58. http://dx.doi.org/10.36629/2686-9896-2020-1-57-58.

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Approaches of problem points estimation for increasing productivity and increasing the accuracy of isolating the C5-C6 fraction in light naphtha isomerization technology are considered. It is shown that the elimination of these problem points is possible by increasing the efficiency of existing internal contact devices of the distillation column, or by increasing the efficiency of the furnace. The final solution to the problem should be determined on the basis of mathematical modeling of the process.

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28

Ji, Xiang, Qing Sheng Zhang, Qun Cui, and Hai Yan Wang. "The Adsorption/Desorption Dynamics Properties of N-Alkanes in Light Naphtha on 5A Zeolites." Advanced Materials Research 807-809 (September 2013): 2643–46. http://dx.doi.org/10.4028/www.scientific.net/amr.807-809.2643.

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Self-made JH4 zeoite was characterized by BET, mercury and other methods. The dynamic adsorption capacity of nC5/nC6 in light naphtha on JH4 zeolite fixed bed was investigated. The effect of cyclic purge exhaust composition, which simulate different condensation conditions, on desorption performance of JH4 zeolite bed was studied. The results shows that, the microporous BET specific surface area and pore volume of JH4 zeolite is 710.05 m2/g and 0.32 cm3/g; macropore specific surface area and pore volume is 3.64 m2/g and 0.29 cm3/g, respectively. Under the adsorption conditions of 0.1 MPa, 165 °C, adsorption capacity of n-pentane and n-hexane in light naphtha on JH4 zeolite reaches, 7.24 g/100gadsand 3.11 g/100gadsrespectively.If the content of pentane and hexane achieves 3.68% and 0.21% in nitrogen purge gas, total desorption amount of JH4 zeolite is 2.07 g/100gads, falling 60.19% than that of pure N2purge.

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29

Knyazeva, Tamara, and Tat'yana Raskulova. "THE OPERATION OF THE CONDENSING EQUIPMENT OF THE ISOMERIZATION UNITS OF LIGHT RIGHT NAPTHA." Modern Technologies and Scientific and Technological Progress 1, no. 1 (2021): 31–32. http://dx.doi.org/10.36629/2686-9896-2021-1-1-31-32.

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the analysis of the operation of the condensation equipment of the units for the pre liminary fractionation of raw materials for the isomerization of straight-run naphtha. Variants of ar rangement of condensing devices of rectification columns are considered, their efficiency is e

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30

KATO, Koichi, Satoshi FUKASE, Yasushi ISHIBASHI, and Manabu YAMAMOTO. "Development of Light Naphtha Aromatization(LNA) Process-Demonstration Plant Work." Journal of The Japan Petroleum Institute 40, no. 6 (1997): 529–33. http://dx.doi.org/10.1627/jpi1958.40.529.

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31

Kimura, Takao, Toshio Shimizu, and Tetsuya Imai. "Platinum-loaded Sulfated Zirconia Catalyst for Isomerization of Light Naphtha." Journal of the Japan Petroleum Institute 47, no. 3 (2004): 179–89. http://dx.doi.org/10.1627/jpi.47.179.

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32

Rovenskaja, Svetlana, and Nikolaj Ostrovski. "Aromatization of light naphtha fractions on zeolites 1: Kinetic model." Chemical Industry 57, no. 9 (2003): 399–403. http://dx.doi.org/10.2298/hemind0309399r.

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On the basis of analyzing kinetic experimental data performed in laboratory integral reactors a lumping kinetic model of the "Zeoforming" process was developed. A reaction scheme of the lumped components was proposed, that was adapted to the technological requirements. The reaction rate constants and activation energies were estimated, that are valid for certain feed compositions. The model is intended for further modeling and optimization of the process.

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33

Al-Kandari, H., S. Al-Kandari, F. Al-Kharafi, and A. Katrib. "Molybdenum-Based Catalysts for Upgrading Light Naphtha Linear Hydrocarbon Compounds." Energy & Fuels 23, no. 12 (2009): 5737–42. http://dx.doi.org/10.1021/ef900617d.

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34

Kriván, Eszter, and Jenő Hancsók. "Oligomerization of Light FCC Naphtha with Ion Exchange Resin Catalyst." Topics in Catalysis 58, no. 14-17 (2015): 939–47. http://dx.doi.org/10.1007/s11244-015-0462-1.

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35

Mohamed, M. F., W. M. Shehata, A. A. Abdel Halim, and F. K. Gad. "Improving gasoline quality produced from MIDOR light naphtha isomerization unit." Egyptian Journal of Petroleum 26, no. 1 (2017): 111–24. http://dx.doi.org/10.1016/j.ejpe.2016.02.009.

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36

Corma, A., F. V. Melo, L. Sauvanaud, and F. Ortega. "Light cracked naphtha processing: Controlling chemistry for maximum propylene production." Catalysis Today 107-108 (October 2005): 699–706. http://dx.doi.org/10.1016/j.cattod.2005.07.109.

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37

Uçar, Suat, and Selhan Karagöz. "Co-processing of olive bagasse with crude rapeseed oil via pyrolysis." Waste Management & Research: The Journal for a Sustainable Circular Economy 35, no. 5 (2017): 480–90. http://dx.doi.org/10.1177/0734242x16680729.

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The co-pyrolysis of olive bagasse with crude rapeseed oil at different blend ratios was investigated at 500ºC in a fixed bed reactor. The effect of olive bagasse to crude rapeseed oil ratio on the product distributions and properties of the pyrolysis products were comparatively investigated. The addition of crude rapeseed oil into olive bagasse in the co-pyrolysis led to formation of upgraded biofuels in terms of liquid yields and properties. While the pyrolysis of olive bagasse produced a liquid yield of 52.5 wt %, the highest liquid yield of 73.5 wt % was obtained from the co-pyrolysis of olive bagasse with crude rapeseed oil at a blend ratio of 1:4. The bio-oil derived from olive bagasse contained 5% naphtha, 10% heavy naphtha, 30% gas oil, and 55% heavy gas oil. In the case of bio-oil obtained from the co-pyrolysis of olive bagasse with crude rapeseed oil at a blend ratio of 1:4, the light naphtha, heavy naphtha, and light gas oil content increased. This is an indication of the improved characteristics of the bio-oil obtained from the co-processing. The heating value of bio-oil from the pyrolysis of olive bagasse alone was 34.6 MJ kg−1 and the heating values of bio-oils obtained from the co-pyrolysis of olive bagasse with crude rapeseed oil ranged from 37.6 to 41.6 MJ kg−1. It was demonstrated that the co-processing of waste biomass with crude plant oil is a good alternative to improve bio-oil yields and properties.

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38

Han, Lei, Chuan Qin Ding, and Huie Lui. "Studies on Olefin Production by Steam Cracking of Waste Oil Blended with Naphtha." Applied Mechanics and Materials 291-294 (February 2013): 738–43. http://dx.doi.org/10.4028/www.scientific.net/amm.291-294.738.

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Waste oil is an important part of the renewable energy, the main component is triglyceride that can be used to generate light olefins by steam cracking. The steam cracking feedstock is naphtha mixed with different proportions of waste oil, mainly in order to study the effect of different mixing ratio on the yield of ethylene, propylene and butadiene. In the case of the mixing ratio of naphtha and waste oil is 1:1, the optimum operating conditions are obtained: the steam cracking temperature is 775°C, the water- oil ratio is 0.65, the residence time is 0.4s.

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39

Hissa, Michaela, Seppo Niemi, Katriina Sirviö, Antti Niemi, and Teemu Ovaska. "Combustion Studies of a Non-Road Diesel Engine with Several Alternative Liquid Fuels." Energies 12, no. 12 (2019): 2447. http://dx.doi.org/10.3390/en12122447.

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Sustainable liquid fuels will be needed for decades to fulfil the world’s growing energy demands. Combustion systems must be able to operate with a variety of renewable and sustainable fuels. This study focused on how the use of various alternative fuels affects combustion, especially in-cylinder combustion. The study investigated light fuel oil (LFO) and six alternative liquid fuels in a high-speed, compression-ignition (CI) engine to understand their combustion properties. The fuels were LFO (baseline), marine gas oil (MGO), kerosene, rapeseed methyl ester (RME), renewable diesel (HVO), renewable wood-based naphtha and its blend with LFO. The heat release rate (HRR), mass fraction burned (MFB) and combustion duration (CD) were determined at an intermediate speed at three loads. The combustion parameters seemed to be very similar with all studied fuels. The HRR curve was slightly delayed with RME at the highest load. The combustion duration of neat naphtha decreased compared to LFO as the engine load was reduced. The MFB values of 50% and 90% occurred earlier with neat renewable naphtha than with other fuels. It was concluded that with the exception of renewable naphtha, all investigated alternative fuels can be used in the non-road engine without modifications.

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40

Panfilov, Nikita, and Ivan Semenov. "INCREASING THE COMPLETENESS OF PENTANE SEPARATION FROM NAPHTHA BY IMPROVING THE SEPARATION ACCURACY IN THE LIGHT NAPHTHA ISOMERIZATION TECHNOLOGY." Modern Technologies and Scientific and Technological Progress 1, no. 1 (2021): 66–67. http://dx.doi.org/10.36629/2686-9896-2021-1-1-66-67.

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The application of a dividing wall column for the separation of isomerization feed  was considered. It will increase the quality of separation of the raw mixture and the efficiency of the  plant.

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41

NISHIJIMA, Hiroaki, Shin-ichi AIKAWA, Tadami KONDOH, and Kazuo HIRABAYASHI. "Conversion of Light Naphtha to Aromatic Hydrocarbons on MFI-Type Zeolites." NIPPON KAGAKU KAISHI, no. 3 (1989): 591–94. http://dx.doi.org/10.1246/nikkashi.1989.591.

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42

Kimura, Takao. "Development of Pt/SO42−/ZrO2 catalyst for isomerization of light naphtha." Catalysis Today 81, no. 1 (2003): 57–63. http://dx.doi.org/10.1016/s0920-5861(03)00102-0.

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43

Redwan, D. S., and A. M. Y. Jaber. "DISTILLATION CHARACTERISTICS AND COMPOSITIONAL ANALYSIS OF ARABIAN LIGHT STRAIGHT RUN NAPHTHA." Petroleum Science and Technology 17, no. 9-10 (1999): 915–29. http://dx.doi.org/10.1080/10916469908949756.

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44

Tailleur, Roberto Galiasso, and Jose Bonilla Platin. "Role of Pt on PtGaZr/SiO2 catalyst in light naphtha isomerization." Journal of Catalysis 255, no. 1 (2008): 79–93. http://dx.doi.org/10.1016/j.jcat.2008.01.010.

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45

Viswanadham, Nagabhatla, Raviraj Kamble, Sandeep K. Saxena, and Madhulika Singh. "Enhanced octane boosting reactions of light naphtha on mesoporous ZSM-5." Catalysis Communications 9, no. 9 (2008): 1894–97. http://dx.doi.org/10.1016/j.catcom.2008.03.011.

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46

Finish, Qusay Ghanim, and Tariq Mohammed Naife. "Adsorption Desulfurization of Iraqi Light Naphtha Using Metals Modified Activated Carbon." Journal of Engineering 27, no. 7 (2021): 24–41. http://dx.doi.org/10.31026/j.eng.2021.07.03.

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The study aims to evaluate the removal of sulfur content from Iraqi light naphtha produced in Al-Dora refinery by adsorption desulfurization DS technique using modified activated carbon MAC loaded with nickel Ni and copper Cu as single binary metals. The experiments were carried in a batch unit with various operating parameters; MAC dosage, agitation speed, and a contact time of 300 min at constant initial sulfur concentration 155 ppm and temperature. The results showed higher DS% by AC/Ni-Cu (66.45)% at 500 rpm and 1 g dosage than DS (29.03)% by activated carbon AC, increasing MAC dosage, agitation speed, and contact time led to increasing DS% values. The adsorption capacity of MAC results was recorded (16, 15, and 20) mg sulfur/g MAC for AC/Ni, AC/Cu and, AC/Ni-Cu, respectively. Equilibrium isotherm study results show good fitting with Freundlich isotherm model with R2 value (0.95) for AC/Ni-Cu. The kinetic study results showed R2 value (0.974, 0.981, and 0.95) by pseudo first order and (0.96, 0.916 and, 0.909) by pseudo second order for AC/Ni, AC/Cu, and AC/Ni-Cu, respectively. The calculated qe(cal) (4.337-4.79) mg/g by first order model was the nearest to the obtained qe(exp) (5.125) mg/g by the experiments where no interparticle diffusion referring to more than one process is controlling the adsorption process of sulfur compounds by MAC.

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47

Натела Хецуриани, Есма Ушараули, Мадлена Чхаидзе, Тамар Шатакишвили та Мака Копалеишвили. "ИССЛЕДОВАНИЕ СКВАЖИН НОВЫХ МЕСТОРОЖДЕНИЙ МАНАВСКОЙ НЕФТИ". World Science 1, № 10(38) (2018): 46–52. http://dx.doi.org/10.31435/rsglobal_ws/31102018/6179.

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    An investigation of oils from new wells of Manavi oil deposit was carried out. Physical and chemical and geochemical parameters, as well as functional groups were determined by IR spectrometry. Using simulative chromatographic distillation of oil from the #12 well naphtha 35-180 °C and diesel fractions were obtained. Individual paraffinic, naphthenic and aromatic hydrocarbons were identified in naphtha by gas chromatographic method and distribution of individual n-paraffinic hydrocarbons in urea concentrate was determined in diesel fraction. The results of the investigation show that due to low content of sulfur, tar- asphaltenic compounds and high yield of light fractions the Manavi oil can be recognized as a high quality paraffinic type of oil. Physical and chemical characteristics, chemical nature and high yield of light fractions outline a good perspective for usage of Manavi deposit oil as a raw material for production of commodity petroleum products like high quality organic solvents, aviation and diesel fuels and various petroleum oils.   

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48

INOUE, Masashi, Xinlin Tu, Sumito NH, and Tomoyuki INUI. "Upgrading of Naphtha Fractions of a Coal Liquid on H-Ga-sillicate. (II). Reactions of Representative Components of Light Naphtha." Journal of the Japan Institute of Energy 71, no. 12 (1992): 1178–83. http://dx.doi.org/10.3775/jie.71.1178.

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49

Ahmed zeki, Nada Sadoon, Sattar Jalil Hussein, Khalifa K. Aoyed, Saad Kareem Ibrahim та Ibtissam K. Mehawee. "Synthesis and Characterization of Co-Mo/γ-Alumina Catalyst from local Kaolin clay for Hydrodesulfurization of Iraqi Naphtha". Journal of Petroleum Research and Studies 11, № 1 (2021): 84–106. http://dx.doi.org/10.52716/jprs.v11i1.431.

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This work deals with the hydrodesulfurization of three types of naphtha feedstocks; mixednaphtha (WN), heavy naphtha (HN) & light naphtha (LN) with a sulfur content of 1642.1,1334.9 & 709 ppm respectively, obtained from Missan refinery using prepared Co-Mo/γ-Al2O3catalyst. The Iraqi white kaolin was used as a starting material for the preparation of γ-Al2O3support, transferring kaolin to meta-kaolin was studied through calcination at differenttemperatures and durations, kaolin structure was investigated using X-Ray diffractiontechniques.High purity 94.83%. Crystalline γ-Al2O3 with a surface area of 129.91 m2/gm, pore volume0.9002 cm3/g was synthesized by extraction of Iraqi kaolin with H2SO4 at different acid to clayweight ratios, acid concentrations & leaching time. Ethanol was used as precipitating agent; theresultant gel was dried and calcined at 70OC, 10 hrs & 900 OC, 2 hrs respectively.The effects of different parameters on the average crystallinity and extraction % ofsynthesized γ-Al2O3 were studied like; acid: clay ratio, sulfuric acid concentration, leachingtime, leaching temperature & kaolin conversion to metakaolin. Characterization of prepared γ-Al2O3 & Co-Mo catalyst were achieved by X-ray diffraction, FTIR-spectra, texture properties& BET surface area, BJH N2 adsorption porosity, AFM, SEM, crush strength & XRF tests. Co-Mo/ γ-Al2O3 catalyst with final loading 5.702 wt% and 21.45 wt% of Co and Mo oxidesrespectively was prepared by impregnation methods.The activity of prepared Co-Mo/γ-Al2O3 catalyst after moulding to be tested forhydrodesulfurization (HDS) of naphtha feedstock W.N, H.N & L.N was performed using apilot hydrotreating unit at petroleum research & development centre, at different operatingconditions. Effects of temperature, LHSV, pressure, time & pore size distribution were studied,the best percentage of sulfur removal is increased with decreasing LHSV to 2 hr-1 as a generaltrend to be 89.71, 99.72, 99.20 % at 310oC for the whole naphtha, heavy naphtha and lightnaphtha feedstocks respectively, at 34 bar pressure and 200/200 cm3/cm3 H2/HC ratio.

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50

FUKASE, Satoshi. "Deactivation of Catalyst for Aromatization of Light Naphtha by Deposition of Coke." Journal of The Japan Petroleum Institute 43, no. 1 (2000): 1–9. http://dx.doi.org/10.1627/jpi1958.43.1.

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