Effect of steam during catalytic cracking of n-hexane using P-ZSM-5 catalyst

Yamaguchi, Aritomo; Jin, Dingfeng; Ikeda, Takuji; Sato, Koichi; Hiyoshi, Norihito; Hanaoka, Toshiaki; Mizukami, Fujio; Shirai, Masayuki

doi:10.1016/j.catcom.2015.05.015

Cited by 27 publications

(9 citation statements)

References 32 publications

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“…It was summarized by Yamaguchi et al (2013) that phosphorus modification for improving the resistance against dealuminization of zeolite in many studies was not sufficient to keep the zeolite structure in SCC. For example, irreversible dealuminization of P-modified zeolite would still occur under a steam/naphtha ratio greater than 0.5 . Also, P-modification could decrease the catalytic activity of zeolite .…”

Section: Processes and Technologies Of Catalytic Cracking Over Basic ...mentioning

confidence: 99%

Research Progress of Basic Catalyst Used in Catalytic Cracking for Olefin Production and Heavy Oil Utilization

Gao

Zhang

Zhao

et al. 2023

Ind. Eng. Chem. Res.

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As the demand for light olefins increases and the oil becomes heavier, higher requirements for catalytic activity, anticoking performance, and stability of catalyst have been brought forward. Basic catalyst has attracted much more attention in recent years due to its excellent performance in heavy oil utilization. This review highlights the research progress of catalytic cracking over basic catalyst for olefin production and heavy oil utilization. The catalytic mechanism along with attractive functions of basic catalyst are summarized. The optimized condition of operation is discussed as well. Several processes and technologies of catalytic cracking over basic catalyst are introduced to advance future development. This review attempts to benefit new researchers in this field by helping them to understand basic-catalyzed cracking characteristics for preparing a suitable catalyst.

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Section: Processes and Technologies Of Catalytic Cracking Over Basic ...mentioning

confidence: 99%

Research Progress of Basic Catalyst Used in Catalytic Cracking for Olefin Production and Heavy Oil Utilization

Gao

Zhang

Zhao

et al. 2023

Ind. Eng. Chem. Res.

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“…A BEA zeolite has been synthesized with different recipes under static conditions with the reaction temperature in the range of 150–170 °C and crystallization time of up to 96 h. 39,42–44 Also, post-modification techniques have been employed to change the BEA catalyst surface to maximize the product yield of the catalytic cracking reaction. The post-modification techniques that have been used include desilication, 38,44–46 dealumination, 6,15,44,47–50 or the combination of both, followed by ion-exchange with several metals. 16,44 The desilication process is done to create mesoporosity by removing silica using an alkaline solution such as sodium hydroxide (NaOH) or potassium hydroxide (KOH), whereas dealumination is carried out to strip alumina from the zeolite crystal framework using an acid solution such as nitric acid.…”

Section: Introductionmentioning

confidence: 99%

Nano BEA zeolite catalysts for the selective catalytic cracking of n-dodecane to light olefins

et al. 2021

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“…Thus, different types of inhibitor additives are used commercially and/or under study. These inhibitors are categorized as sulfur based compounds, i.e., dimethyl sulfide (DMS), dimethyl disulfide (DMDS), hydrogen sulfide (H 2 S), benzothiophenes, bibenzyl sulfide, organo-phosphorus chemicals like Nalco’s trademarked COKE-LESS, sulfur–silicon based additive liquids like the CLX family, , and tin-based additives such as Chevron Phillips CCA500. , Among the additives, the traditional approach to coke elimination in the thermal cracking process is the purposeful addition of sulfur-based compounds, i.e., DMS or DMDS to the feedstocks. , Influence of sulfur compounds to prevent coke formation is highly dependent on the metal composition, application method, concentration, , as well as the chemical nature of the sulfur compounds …”

Section: Introductionmentioning

confidence: 99%

New Design and Optimization for Replacing Dimethyl Disulfide with Wasted Disulfide Oil in Olefin Furnaces

2018

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This paper is aimed to examine and understand the feasibility of replacing dimethyl disulfide (DMDS) with disulfide oil (DSO) in olefin units of the Amir Kabir Petrochemical Refinery (Khuzestan, Iran). This substitution not only provides a very low-priced supply for replacing DMDS in olefin plants, but also it restrains emitting poisonous sulfur gas to the environment. Considering the fact that the conversion of DSO to hydrogen sulfide required a longer residence time related to DMDS, the DSO pilot was built to examine this alteration. Comparing the results with those of DMDS revealed that this pilot allowed for complete replacement. The polynuclear aromatics mechanism was the predominant mechanism, and optimization results showed that three selected parameters (temperature, retention time, and DSO injection rate) affected the CO production. The rate of CO formation was very similar for using both cases. The total sulfur content, which is an environmental pollutant and a component of gasoline, was also controlled. With DMDS, the total sulfur content varied from 20 to 130 ppm, while with DSO it varied from 20 to 100 ppm, which was acceptable. As a result of this process, approximately 221 000 EUR would be saved per year in an olefin unit with an ethylene production capacity of 520 000 tons.

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Effect of steam during catalytic cracking of n-hexane using P-ZSM-5 catalyst

Cited by 27 publications

References 32 publications

Research Progress of Basic Catalyst Used in Catalytic Cracking for Olefin Production and Heavy Oil Utilization

Research Progress of Basic Catalyst Used in Catalytic Cracking for Olefin Production and Heavy Oil Utilization

Nano BEA zeolite catalysts for the selective catalytic cracking of n-dodecane to light olefins

New Design and Optimization for Replacing Dimethyl Disulfide with Wasted Disulfide Oil in Olefin Furnaces

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