Recent advances in the deactivation of FCC catalysts by cyclic propylene steaming (CPS) in the presence and absence of contaminant metals

Wallenstein, D.; Harding, Robert H.; Nee, J. R. D.; Boock, Lori T.

doi:10.1016/s0926-860x(00)00504-4

Cited by 43 publications

(16 citation statements)

References 9 publications

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“…E-CATs were characterized and subjected to a catalytic cracking testing at the bench scale and pilot scale at the same operating conditions than those used for CD-CATs. A summary of E-CAT1 and E-CAT2 properties is displayed in Table 2, showing that the average concentration of metals was 499 and 562 ppm Ni as well as 2,015 and 2,494 ppm V, respectively, corresponding to a low-moderate metals level [1,15].…”

Section: Equilibrium Catalystsmentioning

confidence: 99%

“…Methods aimed at simulating, artificially and rapidly, the irreversible deactivation of the catalyst in the FCC unit due to (hydro)thermal and metallic effects have been developed [14][15][16]. This has been demanding as the scene complicates by the fact that the catalyst circulating in the unit, denoted as equilibrium catalyst, is a mixture of various age particles.…”

Section: Introductionmentioning

confidence: 99%

“…Though CMD mimics relatively well metals distribution in the catalyst particle, it is not very reproducible and flexible. The cyclic propylene steaming (CPS) is a flexible and reproducible method wherein a presteamed catalyst is impregnated with metals via incipient wetness and next subjected to a set of reduction-purge-oxidation-purge cycles in the presence of steam [15,16]. In CPS, propylene is used as reducing gas to modulate the oxidation state of V.…”

Section: Introductionmentioning

confidence: 99%

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Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

et al. 2011

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Besides offering an adequate product distributions, a cracking catalyst must exhibit a reasonable resistance to the combined effect of high temperature, steam and metals. Two commercial catalysts, poisoned with Ni ? V (*2,500 ppm), are subjected to a large scale cyclic deactivation with steam, then characterized using mostly basic techniques and finally tested via bench scale and pilot scale cracking experiments. As examples of industrial deactivation, corresponding equilibrium catalysts (E-CATs) are investigated in parallel. Depending on their specific formulation, catalysts deactivate differently due to the exposition to high temperature steam and metals. The intrinsic deviations in the catalytic properties of cyclic deactivated catalysts (CD-CATs) related to E-CATs are further biases by the particular history of the latter and the particular reactor configuration and hydrodynamics, such deviations being magnified in the bench scale testing. Relative differences in activity and product yields (except for coke and hydrogen) of CD-CATs referred to E-CATs are below 10% at the pilot scale, and within 23% at the bench scale. Relative biases in hydrogen and coke yield of may be as high as 75 and 26% in the pilot plant and as much as 150 and 32% at the bench scale.

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Section: Equilibrium Catalystsmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

et al. 2011

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“…Testing of the 650 fractions from Cases 1-3 and 5 of Table 1 was conducted in an ACE fluidized bed pilot plant reactor after deactivation by the cyclic propylene steaming (CPS) protocol 10) . Feed metals levels and theoretical catalyst addition rates were used to project equilibrium catalyst metals levels and simulate commercial operation.…”

Section: Rfcc Yields From Rds Productsmentioning

confidence: 99%

Increase Flexibility to Upgrade Residuum Using Recent Advances in RDS/VRDS-RFCC Process and Catalyst Technology

Threlkel

Dillon

Singh

et al. 2010

J. Jpn. Petrol. Inst.

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An overview of several refinery process options that convert high boiling point fractions of crude oil into more valuable distillates is presented. The combination of Residuum Desulfurization (RDS) with Residuum Fluid Catalyst Cracking (RFCC) produces high yields of transportation fuels and chemicals feedstock with minimal fuel oil by-product. This process scheme can present formidable technical challenges for the catalysts of each process to handle the increased levels of contaminants such as Microcarbon Residue (MCR), nickel and vanadium present in heavy oil. This paper presents the results of hydrotreating heavier Atmospheric Residuums (AR) in RDS pilot plants with Ni _ Mo supported catalysts. RDS pilot plant life tests are conducted and middle of run products are collected and distilled for analysis and further RFCC testing. Process condition variation and new catalyst development has been applied to improve RDS capability to handle heavier, more contaminated residuum. The RDS products are tested for RFCC reactivity using Advanced Cracking Evaluation (ACE) tests. The development of improved RFCC catalyst is applied to boost cracking catalyst tolerance of residuum metal contaminants. Judicious selection of newly developed RDS and RFCC catalysts enable production of higher yields of gasoline from heavier AR's. The coordinated application of new RDS and RFCC catalysts enables the conversion of dirtier residuum feedstock to produce greater yields of distillates.

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“…The production of excess coke and hydrogen is a result of dehydrogenation reactions catalyzed by the contaminant metals on equilibrium catalysts. It was reported that the oxidation state of contaminant-metals, especially vanadium, is very important factor that affects the dehydrogenation activity of a specific metal on FCC catalyst [2]. It is necessary to understand the relationship between the amount coke formed by contaminant metals and the oxidation states of these metals.…”

Section: Introductionmentioning

confidence: 99%

Temperature-programmed oxidation of equilibrium fluid catalytic cracking catalysts

Bayraktar

Kugler

2004

Journal of Thermal Analysis and Calorimetry

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Characterization of coke on equilibrium, fluid catalytic cracking (FCC) catalysts contaminated with metals was investigated using temperature-programmed oxidation (TPO). TPO spectra of spent equilibrium catalysts from cracking of sour imported heavy gas oil (SIHGO) were deconvoluted into four peaks (Peak K, L, M and N). The four peaks were assigned to different types of coke on the catalyst. Peak L in the TPO spectrum was assigned to the 'contaminant' coke in the vicinity of metals. The amount of contaminant coke (Peak L) correlates with metal-contaminant concentration. The size of Peak L which is related to amount of contaminant coke decreased significantly for the spent highly contaminated catalyst pretreated with hydrogen and methane prior to cracking reactions as compared to the non-pretreated catalysts. Since both hydrogen and methane pretreatment can reduce oxidation state of the vanadium that present at high concentrations on the equilibrium catalysts the decrease in the amount of contaminant-coke represented by Peak L was explained by the reduction of the oxidation state of vanadium. Less contaminant coke was produced after the equilibrium catalysts were pretreated using hydrogen and methane gases since reduced vanadium has lower dehydrogenation activity compared to oxidized vanadium.

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Recent advances in the deactivation of FCC catalysts by cyclic propylene steaming (CPS) in the presence and absence of contaminant metals

Cited by 43 publications

References 9 publications

Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

Increase Flexibility to Upgrade Residuum Using Recent Advances in RDS/VRDS-RFCC Process and Catalyst Technology

Temperature-programmed oxidation of equilibrium fluid catalytic cracking catalysts

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