Effect of HZSM-5 Zeolite Addition to a Fluid Catalytic Cracking Catalyst. Study in a Laboratory Reactor Operating under Industrial Conditions

Arandes, José M.; Abajo, Iñaki; Fernández, Inmaculada; Azkoiti, Miren J.; Bilbao, Javier

doi:10.1021/ie990335t

Cited by 63 publications

(63 citation statements)

References 19 publications

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“…Furthermore, the conversion of isoolefins to isoparaffins by hydrogen transfer is severely hindered by shape selectivity and the low acid sites density of the tested samples. The results are consistent with those obtained in the cracking of VGO by several authors [41,42,44,45].…”

Section: Conversion and Yieldssupporting

confidence: 93%

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Effect of HZSM-5 catalyst addition on the cracking of polyolefin pyrolysis waxes under FCC conditions

Arandes

Azkoiti

Torre

et al. 2007

Chemical Engineering Journal

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Section: Conversion and Yieldssupporting

confidence: 93%

“…The consequence is a decrease in the yield of gasoline and an increase in the yield of LPG compared to the base catalyst [40][41][42]44]. This apparently different role of the zeolite is explained by the difference in the feeds.…”

Section: Conversion and Yieldsmentioning

confidence: 99%

Effect of HZSM-5 catalyst addition on the cracking of polyolefin pyrolysis waxes under FCC conditions

Arandes

Azkoiti

Torre

et al. 2007

Chemical Engineering Journal

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“…The naphtha stream can be reprocessed either in the same riser or in a parallel, dedicated riser, taking advantage of customized operating conditions. Studies in Riser Simulator [48], Microriser [37] and Microdowner [40][41] have been realized, giving similar results. As expected, olefins, especially longer olefins (7 or more carbons) are considerably reduced in the remaining gasoline.…”

Section: Naphtha Cracking and High Severity Crackingmentioning

confidence: 63%

FCC testing at bench scale: New units, new processes, new feeds

Corma

Sauvanaud

2013

Catalysis Today

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As the FCC process has evolved over decades, several laboratory scale equipment have appeared to maintain a proper assessment of catalysts activity. Several laboratory equipments are available for simulating the FCC process, from the well known fixed bed, MicroActivity Test to newer, fluid bed or transported bed units. As well, a number of units have been created to simulate other parts of the process such as regenerator or stripper, The increased pressure for treating non-conventional feeds, from reprocessing gasoline to extra-heavy feeds or oils produced from biomass containing large amounts of heteroatoms, increase the needs to have a laboratory test which is as close as possible to the process so that data extraction from the laboratory test are simplified, thus less prone to errors or misunderstanding. KeywordsLaboratory testing, catalytic cracking, naphtha cracking, coked catalyst, biooil cracking Highlights• FCC process is adapting to new feeds and new processes• Heavy resid feeds and biomass-derived feeds are being extensively tested • Significant operation and process changes are contemplated to squeeze maximum value from feeds: naphtha reprocessing, use of partially coked catalysts, several independent risers. 3

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“…The Riser Simulator is a novel bench scale, invented by de Lasa (1992). This unit overcomes the technical problems of the standard micro-activity test (MAT) and is becoming a most valuable experimental tool for testing and developing new FCC catalysts (Arandes et al, 2000;Arandes et al, 1997;Bidabehere and Sedran, 2000;Sedran, 1994). …”

Section: -Reaction Evaluationmentioning

confidence: 99%

Diffusion and catalytic cracking of 1,3,5 tri-iso-propyl-benzene in FCC catalysts

Al-Khattaf

Atias

Jarosch

et al. 2002

Chemical Engineering Science

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The present study describes catalytic cracking experiments developed in a novel CREC Riser Simulator using 1,3,5-Tri-iso-propyl-benzene and two FCC catalysts with different crystal sizes (0.4-μm and 0.9-μm diameter). The experiments are modeled using an unsteady state model for both gas and catalyst phases. It is found that a quasi-steady state approximation can be used for the catalyst and changes in the gas phase can be accounted, under the allowed model simplifications, with a relatively simple unsteady state equation. The model is completed using two catalytic decay models, with one of them involving a decay function based on "reactant converted". Experimental and modeling observations point towards an overall cracking reaction rate controlled by diffusion at 350°C -450°C with this rate shifting to one being controlled by the intrinsic cracking reaction at 500°C -550°C.(*) Author to whom correspondence may be addressed 2 1-IntroductionThe oil refining industry has experienced in recent years, a dramatic increase in the price and availability of crude oil. In this respect, new catalyst technology is needed to process heavier feedstocks and to produce more environmentally friendly products.The currently available 60-μm commercial FCC catalysts are manufactured with 1-2-μm Y-zeolite crystals dispersed in an amorphous silicaalumina matrix . The majority of the active sites are located within the zeolite pore structure. In order for the reaction to proceed, molecules have to diffuse through the large matrix pores into the zeolite crystals.As a result, only certain hydrocarbon species with a kinetic diameter smaller than 10.2 Å can penetrate the zeolite pores (Leiby, 1992). Hence the relationship between catalytic cracking reaction and diffusional processes can determine the extent of cracking and greatly influence the product selectivity. Such phenomena are complex and theoretical models to describe such systems are needed (Bidabehere and Sedran, 2000).Diffusion in catalysts belongs in many cases to the Knudsen regime.However, diffusion in zeolites falls more in a so-called "configurational regime", since the size of the hydrocarbon molecule is nearly the size of the zeolite inner channels (Karger and Ruthven, 1992; Gates et al,1979). As a result, diffusion of the hydrocarbon molecules is governed by an almost continuous interaction between the zeolite crystal and the diffusing molecules (Karger and Ruthven,1992;Gates et al,1979). In addition, there may be compounded effects 3 with larger hydrocarbon molecules hindering the diffusion of smaller molecules.As a result, lighter product molecules may be trapped or delayed in a zeolite pore network already filled with sorbed heavier molecules (Gates et al, 1979). The 1,3,5-TIPB is a relatively bulky molecule with a critical molecular diameter of about 9.5 Å (Bhatai, 1991). Due to its large size, it has been used to simulate the diffusional constrains expected in the catalytic cracking of gas oil (Aguiar et al, 1995). For instance, the cracking of 1,3,5-TIPB ...

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Effect of HZSM-5 Zeolite Addition to a Fluid Catalytic Cracking Catalyst. Study in a Laboratory Reactor Operating under Industrial Conditions

Cited by 63 publications

References 19 publications

Effect of HZSM-5 catalyst addition on the cracking of polyolefin pyrolysis waxes under FCC conditions

Effect of HZSM-5 catalyst addition on the cracking of polyolefin pyrolysis waxes under FCC conditions

FCC testing at bench scale: New units, new processes, new feeds

Diffusion and catalytic cracking of 1,3,5 tri-iso-propyl-benzene in FCC catalysts

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