Conversion of higher n-alkanes under deep catalytic cracking conditions

Липин, П. В.; Доронин, В. П.; Gulyaeva, T. I.

doi:10.1134/s0965544110050075

Cited by 19 publications

(7 citation statements)

References 15 publications

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“…The fact that ZSM-5 zeolite had more acidic properties than Y-zeolite in the catalyst was found in [38]. The strong to weak acid sites ratio is similar to ZSM-5 zeolite, while the amount of weak acid sites in zeolite Y is lower in 2 times than the amount of average acid sites.…”

Section: T C a T C A T C A T C A T F S F S F S F S F S C A T C A Tmentioning

confidence: 85%

“…The strong to weak acid sites ratio is similar to ZSM-5 zeolite, while the amount of weak acid sites in zeolite Y is lower in 2 times than the amount of average acid sites. The total number of acid sites is 0.88 -for Y-zeolite and 1.30 -for ZSM-5 zeolite [38]. Along with that, the pore size of ZSM-5 zeolite is less than 0.7 nm.…”

Section: T C a T C A T C A T C A T F S F S F S F S F S C A T C A Tmentioning

confidence: 94%

“…The olefins in Y-zeolite pores are exposed to cyclization (k 14 =17.71 l·s -1 ·mol -1 ) and hydrogen transfer (k 15 = 36.3 l·s -1 ·mol -1 ) which leads to the formation of cycloalkanes, cycloalkenes and aromatics and the reduction of the olefins content in the products. [38]. These structures condense with a high reaction rate creating the coke precursor and the coke products.…”

Section: № Reactionsmentioning

confidence: 98%

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Mathematical modelling of catalytic cracking riser reactor

Иванчина

Ivashkina

Nazarova

2017

Chemical Engineering Journal

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Section: T C a T C A T C A T C A T F S F S F S F S F S C A T C A Tmentioning

confidence: 85%

Section: T C a T C A T C A T C A T F S F S F S F S F S C A T C A Tmentioning

confidence: 94%

Section: № Reactionsmentioning

confidence: 98%

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Mathematical modelling of catalytic cracking riser reactor

Иванчина

Ivashkina

Nazarova

2017

Chemical Engineering Journal

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“…The bizeolite deep catalytic cracking catalyst (whose composition we confirmed in [9]) and LUX catalyst (Gazprom Neft Omsk Oil Refinery) were selected for our study. The bizeolite catalyst incorpo rated a matrix, ZSM 5, and ultrastable Y zeolites in equivalent amounts.…”

Section: Methodsmentioning

confidence: 99%

Effect of process conditions on the composition of products in the conventional and deep catalytic cracking of oil fractions

2012

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With the purpose of increasing the yield of light C 2 −C 4 olefins in comparison with that in conven tional catalytic cracking, we experimentally study the effect of temperature and catalyst to oil ratio on the dis tribution of the basic products of oil catalytic cracking on the bizeolite and industrial LUX catalysts. The bizeolite catalyst contains ZSM 5 and ultrastable Y zeolites in equivalent amounts, while the LUX catalyst contains 18 wt % of Y zeolite in the HRE form. As shown by the results of our tests, the yield of C 2 -C 4 olefins and gasoline in the deep catalytic cracking of hydrotreated vacuum gasoil on the bizeolite catalyst within a range of catalyst to oil ratios of 5-7 and temperatures of 540-560°C reaches 32-36 and nearly 30 wt %, respectively. In cracking on the LUX catalyst under similar conditions, the yield of light olefins and gasoline is 12-16 and 37-45 wt %, respectively. The distribution of target products in the deep catalytic cracking of different hydrocarbon fractions (vacuum gasoil, gas condensate, its fraction distilled from the cut boiling below 216°C, and the hydrocracking heavy residue) on the bizeolite catalyst is studied. It is shown that the fractions of gas condensate and hydroc racking residue can serve as an additional source of hydrocarbon raw materials in the production of olefins.

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“…Another important characteristic of catalysts, which affects their activity, properties [23]. The results of TPD showed that subacid sites attend the catalysts the presence of one form of desorption of ammonia on the thermal desorption spe The temperatures of peak maximum are equal to 95-140 °C and 100-125 °C for re ated and spent catalysts [24], and the total amount of desorbed ammonia decrease regenerated to spent catalysts. Moreover, the specific surface area correlates with t number of acid sites on regenerated samples, for catalyst #4 these values are 141 and 232 μmol/g.…”

Section: Modellingmentioning

confidence: 99%

A Model of Catalytic Cracking: Catalyst Deactivation Induced by Feedstock and Process Variables

et al. 2022

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Changes in the quality of the feedstocks generated by involving various petroleum fractions in catalytic cracking significantly affect catalyst deactivation, which stems from coke formed on the catalyst surface. By conducting experimental studies on feedstocks and catalysts, as well as using industrial data, we studied how the content of saturates, aromatics and resins (SAR) in feedstock and the main process variables, including temperature, consumptions of the feedstock, catalyst and slops, influence the formation of catalytic coke. We also determined catalyst deactivation patterns using TG-DTA, N2 adsorption and TPD, which were further used as a basis for a kinetic model of catalytic cracking. This model helps predict the changes in reactions rates caused by coke formation and, also, evaluates quantitatively how group characteristics of the feedstock, the catalyst-to-oil ratio and slop flow influence the coke content on the catalyst and the degree of catalyst deactivation. We defined that a total loss of acidity changes from 8.6 to 30.4 wt% for spent catalysts, and this depends on SAR content in feedstock and process variables. The results show that despite enriching the feedstock by saturates, the highest coke yields (4.6–5.2 wt%) may be produced due to the high content of resins (2.1–3.5 wt%).

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Conversion of higher n-alkanes under deep catalytic cracking conditions

Cited by 19 publications

References 15 publications

Mathematical modelling of catalytic cracking riser reactor

Mathematical modelling of catalytic cracking riser reactor

Effect of process conditions on the composition of products in the conventional and deep catalytic cracking of oil fractions

A Model of Catalytic Cracking: Catalyst Deactivation Induced by Feedstock and Process Variables

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