US 4,180,453 AGranted

Process for the steam-cracking of heavy feedstocks

AssigneeInstitut Francais du Petrole

InventorsJean-Pierre Franck, Edouard Freund, Jean-Francois Le Page, Jean Miquel

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Abstract

A fresh charge containing aromatic hydrocarbons is hydrotreated in admixture with a recycle fraction, in the presence of a bifunctional catalyst, a portion of the effluent is subjected to steam-cracking, thereby recovering a gas oil fraction which is subjected to hydrogenation and forms said recycle fraction. The mixture of recycle fraction and charge is advantageously treated with hydrogen in the presence of a monofunctional catalyst to hydrogenate olefins, at a lower temperature than the hydrotreatment, and then passed to the hydrotreatment zone.

Claims5

Dependent claims

A process for treating a hydrocarbon charge of initial boiling point higher than about 150.degree. C., selected from the atmospheric gas oils, vacuum gas oils and deasphalted residues, the charge containing at least 10% by weight selected from monocyclic and polycyclic aromatic hydrocarbons, comprising the steps of:

(a) passing a mixture of said hydrocarbon charge with a recycle fraction as hereinafter defined through a catalyst bed in the presence of hydrogen to hydrogenate olefins present in said mixture, at a temperature between 280.degree. and 400.degree. C., said temperature being lower than the hydrotreating of step (b), said catalyst bed containing at least one sulfide of a metal from group VI B and at least one sulfide of a metal from group VIII of the periodic classification of the elements, and a carrier having an acidity corresponding to a heat of ammonia absorption lower than .DELTA.H=0.06, measured at a pressure of 10.sup.-4 mm Hg;
(b) subjecting resultant effluent from step (a) to a hydrotreatment to separate nitrogen and sulfur and to hydrogenate the monocyclic and polycyclic aromatic hydrocarbons therein, at 340.degree.-420.degree. C., in the presence of hydrogen gas and a catalyst comprising 1-30% by weight of at least one sulfide of a metal selected from tungsten and molybdenum, and at least one sulfide of a metal selected from cobalt and nickel, and an acidic carrier selected from aluminas, alumina-silicas, boron-aluminas, fluorinated aluminas and magnesia-silicas;
(c) subjecting at least a portion of resultant effluent from the hydrotreatment of step (b) to a steam-cracking step;
(d) withdrawing from the steam-cracking step a gas oil fraction distilling at about 150.degree.-400.degree. C., light hydrocarbons and a gasoline fraction;
(e) subjecting at least a portion of said gas oil fraction from step (d) to hydrogenation at 150.degree.-260.degree. C. under a pressure of 30 to 130 bars, at a L.H.S.V. of from 1 to 5, in the presence of a catalyst selected from a platinum group metal or at least one sulfided metal from group VI B and VIII of the periodic classification of elements, and a carrier selected from the group consisting of alumina and silica having a specific surface of between 10 and 100 m.sup.2 /g, said hydrogenation effecting a decrease of the total content of alkenylaromatic hydrocarbons and indenes in said gas oil fraction to less than 1% by weight;
and
(f) admixing resultant effluent from step (e) as said recycle fraction with said hydrocarbon charge to form said mixture which is passed through said catalyst bed of step (a), the amount of said admixed recycle fraction being at least 10% by weight of said hydrocarbon charge.

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Dependencies are inferred from the claim text.

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Abstract

(a) passing a mixture of said hydrocarbon charge with a recycle fraction as hereinafter defined through a catalyst bed in the presence of hydrogen to hydrogenate olefins present in said mixture, at a temperature between 280.degree. and 400.degree. C., said temperature being lower than the hydrotreating of step (b), said catalyst bed containing at least one sulfide of a metal from group VI B and at least one sulfide of a metal from group VIII of the periodic classification of the elements, and a carrier having an acidity corresponding to a heat of ammonia absorption lower than .DELTA.H=0.06, measured at a pressure of 10.sup.-4 mm Hg;
(b) subjecting resultant effluent from step (a) to a hydrotreatment to separate nitrogen and sulfur and to hydrogenate the monocyclic and polycyclic aromatic hydrocarbons therein, at 340.degree.-420.degree. C., in the presence of hydrogen gas and a catalyst comprising 1-30% by weight of at least one sulfide of a metal selected from tungsten and molybdenum, and at least one sulfide of a metal selected from cobalt and nickel, and an acidic carrier selected from aluminas, alumina-silicas, boron-aluminas, fluorinated aluminas and magnesia-silicas;
(c) subjecting at least a portion of resultant effluent from the hydrotreatment of step (b) to a steam-cracking step;
(d) withdrawing from the steam-cracking step a gas oil fraction distilling at about 150.degree.-400.degree. C., light hydrocarbons and a gasoline fraction;
(e) subjecting at least a portion of said gas oil fraction from step (d) to hydrogenation at 150.degree.-260.degree. C. under a pressure of 30 to 130 bars, at a L.H.S.V. of from 1 to 5, in the presence of a catalyst selected from a platinum group metal or at least one sulfided metal from group VI B and VIII of the periodic classification of elements, and a carrier selected from the group consisting of alumina and silica having a specific surface of between 10 and 100 m.sup.2 /g, said hydrogenation effecting a decrease of the total content of alkenylaromatic hydrocarbons and indenes in said gas oil fraction to less than 1% by weight;
and
(f) admixing resultant effluent from step (e) as said recycle fraction with said hydrocarbon charge to form said mixture which is passed through said catalyst bed of step (a), the amount of said admixed recycle fraction being at least 10% by weight of said hydrocarbon charge.

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