Kinetic and decay cracking model for a MicroDowner unit

Corma, Avelino; Melo, Francisco Vicente Sales; Sauvanaud, Laurent

doi:10.1016/j.apcata.2005.03.032

Cited by 25 publications

(18 citation statements)

References 35 publications

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“…We are thinking of the FCC technology that makes use of catalysts with ZSM-5 additives to produce higher light olefins [24][25][26]. In fact, with the development of efficient feed injection systems (multiple injectors), it would be relatively easy to inject methanol along with the usual FCC hydrocarbon feed [27].…”

Section: Resultsmentioning

confidence: 99%

Mixed Naphtha/Methanol Feed Used in the Thermal Catalytic/Steam Cracking (TCSC) Process for the Production of Propylene and Ethylene

Yan

Mao

2010

Catal Lett

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The addition of some methanol to petroleum light naphtha used as feed in the Thermal Catalytic/Steam Cracking(TCSC) process significantly increases the product yield of C 2 -C 4 olefins, particularly that of ethylene ? propylene. However, over 20-25 wt% of methanol content in the naphtha feed, the beneficial effect is attenuated. At relatively high values of contact time, the (Zn-Pd) co-catalyst of the hybrid catalyst exerts noticeably its coke cleaning effect on the zeolite acid sites, particularly when methanol is present in the feed. The product weight ratio (propylene/ethylene) is not affected by such ''moderate'' addition of methanol and remains higher than 1.3.

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Section: Resultsmentioning

confidence: 99%

Mixed Naphtha/Methanol Feed Used in the Thermal Catalytic/Steam Cracking (TCSC) Process for the Production of Propylene and Ethylene

Yan

Mao

2010

Catal Lett

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“…The peak that appears at 600ºC (4000s, Figure 4) is due to methane and is correlated with a peak for hydrogen. The hydrogen and methane emissions from coked catalyst have already been observed during stripping [20] or preheating of coked catalysts at temperatures above 600ºC before further processing [21]. The emissions of methane and hydrogen from coke have nearly stopped when the second emissions begin at 700ºC and represent only a tiny fraction of the total coke on catalyst (<3%).…”

Section: Tpd-ms Results and Influence Of The Temperature On Fcc Equilmentioning

confidence: 99%

Coke steam reforming in FCC regenerator: A new mastery over high coking feeds

Corma

Sauvanaud

Doskocil³

et al. 2011

Journal of Catalysis

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One of the crucial problems of processing residual feeds in the FCC is their high coking tendency, which limits their use in the FCC and requires them to be mixed with lighter feeds to be processed in conventional FCC units. A step-out improvement of the FCC process to use in processing heavy feeds is presented, where the heat balance in the unit is maintained by removing the high coke on catalyst by a combination of coke combustion and reforming, i.e. Coke Steam Reforming (CSR) in the regenerator. This option enables using feeds with more than 10% Conradson Carbon while still maintaining the possibility to control the heat balance in the unit without using partial combustion or catalyst coolers. Although the Equilibrium catalyst has little CSR activity, we have found that hydrotalcite materials, besides having an excellent catalytic cracking selectivity for heavy feeds, also have significant CSR activity. We have demonstrated that CSR can be performed together with combustion at conditions found in the FCC regenerator so that the regenerator temperature remains within traditional limits despite higher coke on catalyst and the coke on the catalyst is nearly completely removed. While the reaction rate at higher temperatures seems to obey first order, steam reforming coke removal kinetics at lower (750ºC) temperatures seem more complex due to the heterogeneous nature of coke.

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“…Hardware and detailed operation of the MD have been described previously [8,9]. Main features of the unit comprise a catalyst preheated where the catalyst is stored before the test, a once-through tubular reactor, where the feed and the preheated catalyst are contacted continuously at a short residence time (0.3-2 s), and a disengaged in which catalyst is separated from hydrocarbons before regeneration.…”

Section: Reaction Schemesmentioning

confidence: 99%

“…Products are recovered by known methods (cold traps for liquids and a burette for gases) and catalyst is regenerated after the stripping step with an air flow of 500 ml/min during 3 h. Nitrogen is injected for catalyst smooth transport and feed dispersion. The unit can work in a fully automatic way, and an option for testing different catalysts is available [9]. The MAT unit is an automated unit that can perform in a continuous way up to eight experiments without personal assistance; details are given elsewhere [10,11].…”

Section: Reaction Schemesmentioning

confidence: 99%

Different process schemes for converting light straight run and fluid catalytic cracking naphthas in a FCC unit for maximum propylene production

Corma¹

2004

Applied Catalysis A: General

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Kinetic and decay cracking model for a MicroDowner unit

Cited by 25 publications

References 35 publications

Mixed Naphtha/Methanol Feed Used in the Thermal Catalytic/Steam Cracking (TCSC) Process for the Production of Propylene and Ethylene

Mixed Naphtha/Methanol Feed Used in the Thermal Catalytic/Steam Cracking (TCSC) Process for the Production of Propylene and Ethylene

Coke steam reforming in FCC regenerator: A new mastery over high coking feeds

Different process schemes for converting light straight run and fluid catalytic cracking naphthas in a FCC unit for maximum propylene production

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