Method for cracking residual oils

Claim 2

In a method for converting hydrocarbons comprising residual oils which comprises charging hot particles of catalyst at a temperature above 1400° F. and at least equal to the pseudo-critical temperature of a hydrocarbon feed comprising residual oils to the lower portion of a riser conversion zone for flow upwardly therethrough, charging the hydrocarbon feed comprising residual oils to said riser conversion zone as a multiplicity of separate streams so as to substantially completely vaporize vaporizable components of the feed whereby thermal and catalytic cracking of the feed is accomplished and recovering a hydrocarbon product of said thermal and catalytic cracking of the feed separate from catalyst particles the improvement comprising employing a catalyst comprising a zeolitic aluminosilicate selected from the group consisting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 3

In a method for cracking a heavy oil comprising polycyclic aromatics, asphaltenes and metal contaminants which comprises, contacting the heavy oil with catalyst particles to form a suspension at a temperature above the heavy oil pseudo-critical temperature and contact conditions to obtain substantially complete vaporization of the heavy oil in combination with thermal and catalytic cracking thereof, and recovering hydrocarbon products of said thermal and catalytic cracking separate from catalyst particles, the improvement comprising employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 4

In a method for cracking a heavy oil comprising polycyclic aromatics, asphaltenes and metal contaminants which comprises, contacting the heavy oil with catalyst particles to form a suspension at a temperature above the heavy oil pseudo-critical temperature and contact conditions to obtain substantially complete vaporization of the heavy oil in combination with thermal and catalytic cracking thereof, and recovering hydrocarbon products of said thermal and catalytic cracking separate from catalyst particles, the improvement comprising employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 5

In a method for converting crude oil boiling above 400° F. which comprises mixing a sufficient amount of catalyst particles at a temperature above 1400° F. and at least equal to the crude oil pseudo-critical temperature charged as a plurality of separate oil streams and admixed with a diluent material to obtain substantially instantaneous vaporization of the charged crude oil by catalyst substantially concomitantly with thermal and catalytic cracking thereof, and recovering products of said cracking separate from catalyst particles, the improvement which comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 6

In a method for converting crude oil boiling above 400° F. which comprises mixing a sufficient amount of catalyst particles at a temperature above 1400° F. and at least equal to the crude oil pseudo-critical temperature charged as a plurality of separate oil streams and admixed with a diluent material to obtain substantially instantaneous vaporization of the charged crude oil by catalyst substantially concomitantly with thermal and catalytic cracking thereof, and recovering products of said cracking separate from catalyst particles, the improvement which comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 7

In a method for effecting conversion of a residual oil by mixing a residual oil preheated to a temperature up to about 800° F. with a sufficient amount of catalyst particles at an elevated temperature above the residual oil pseudo-critical temperature to obtain substantially instantaneous vaporization of the residual oil feed along with thermal and catalytic cracking thereof and recovering products of said cracking comprising gasoline, higher and lower boiling hydrocarbon products separate from catalyst particles, the improvement comprising employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 8

In a method for effecting conversion of a residual oil by mixing a residual oil preheated to a temperature up to about 800° F. with a sufficient amount of catalyst particles at an elevated temperature above the residual oil pseudo-critical temperature to obtain substantially instantaneous vaporization of the residual oil feed along with thermal and catalytic cracking thereof and recovering products of said cracking comprising gasoline, higher and lower boiling hydrocarbon products separate from catalyst particles, the improvement comprising employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 9

In a method for catalytically converting high boiling hydrocarbons comprising topped crudes, atmospheric tower bottoms, residual oils, tar sands, shale oils and gas oils comprising one or more of asphaltenes, polycyclic aromatics and metal contaminants which comprises, catalytically cracking said high boiling hydrocarbons initially mixed in a cracking zone with hot regenerated catalyst at a temperature at least equal to the pseudo-critical temperature of the hydrocarbon feed, separating catalyst particles comprising hydrocarbonaceous deposits from hydrocarbon conversion products and separately recovering each, partially regenerating separated catalyst particles comprising hydrocarbonaceous deposits in a first catalyst regeneration zone under conditions of oxygen concentration and temperature selected to burn particularly hydrogen associated with hydrocarbonaceous material thereby leaving residual carbon on the catalyst and produce a CO rich flue gas thereafter recovered from said catalyst partial regeneration operation, passing catalyst particles thus partially regenerated and comprising residual carbon deposits to a second separate catalyst regeneration zone, further regenerating the partially regenerated catalyst in the second regeneration zone at a temperature above 1500° F. in the presence of sufficient oxygen to substantially completely burn residual carbon deposits and CO and produce a CO 2 rich flue gas, recovering regenerated catalyst substantially free of residual carbon thereon at a temperature above the psuedo-critical temperature of said hydrocarbon feed to be catalytically converted by the catalyst, and passing catalyst thus regenerated from said second regeneration zone to said cracking zone to form a mix temperature at least equal to said psuedo-critical temperature of charged hydrocarbon feed, the improvement which comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 10

In a method for catalytically converting high boiling hydrocarbons comprising topped crudes, atmospheric tower bottoms, residual oils, tar sands, shale oils and gas oils comprising one or more of asphaltenes, polycyclic aromatics and metal contaminants which comprises, catalytically cracking said high boiling hydrocarbons initially mixed in a cracking zone with hot regenerated catalyst at a temperature at least equal to the pseudo-critical temperature of the hydrocarbon feed, separating catalyst particles comprising hydrocarbonaceous deposits from hydrocarbon conversion products and separately recovering each, partially regenerating separated catalyst particles comprising hydrocarbonaceous deposits in a first catalyst regeneration zone under conditions of oxygen concentration and temperature selected to burn particularly hydrogen associated with hydrocarbonaceous material thereby leaving residual carbon on the catalyst and produce a CO rich flue gas thereafter recovered from said catalyst partial regeneration operation, passing catalyst particles thus partially regenerated and comprising residual carbon deposits to a second separate catalyst regeneration zone, further regenerating the partially regenerated catalyst in the second regeneration zone at a temperature above 1500° F. in the presence of sufficient oxygen to substantially completely burn residual carbon deposits and CO and produce a CO 2 rich flue gas, recovering regenerated catalyst substantially free of residual carbon thereon at a temperature above the psuedo-critical temperature of said hydrocarbon feed to be catalytically converted by the catalyst, and passing catalyst thus regenerated from said second regeneration zone to said cracking zone to form a mix temperature at least equal to said psuedo-critical temperature of charged hydrocarbon feed, the improvement which comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consiting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 11

The process of claims 1,2,3,4 or 5 wherein said zeolitic aluminosilicate is LZ-210 having a SiO 2 to Al 2 O 3 ratio greater than 8.0.

Claim 12

The process of claims 1,2,3,4 or 5 wherein said zeolitic aluminosilicate is LZ-210-T having a SiO 2 to Al 2 O 3 ratio greater than 8.0.

Claim 13

The process of claims 1,2,3,4 or 5 wherein said zeolitic aluminosilicate is LZ-210-M having a SiO 2 to Al 2 O 3 ratio greater than 6.0 and less than 8.0.

Claim 14

The process of claims 1,2,3,4 or 5 wherein said zeolitic aluminosilicate is LZ-210-A having a SiO 2 to Al 2 O 3 ratio greater than 7.0.

Claim 15

The process of claim 4 or claim 5 wherein the regenerated catalyst is at a temperature within the range of 1400° F. to 1800° F.

Claim 16

The method of claim 5 wherein the second stage catalyst regeneration operation is effected at a higher temperature than said first stage regeneration.

Claim 17

The method of claim 5 wherein said hydrocarbon conversion products comprise gasoline.

Claim 18

The method of claim 5 wherein the catalyst employed is spherical.

Claim 19

The process of claims 1,2,3,4 or 5 wherein the zeolitic aluminosilicate is defined as having a chemical composition expressed in terms of mole fractions of framework tetrahedra as: [Al.sub.(a-N) Si.sub.b+(N-Δz) □.sub.z ]O.sub.2 wherein; ##EQU4## has a value greater than 3, the change in defect structure factor Δz is less than 0.08; an increased silicon content in the framework, (N-Δz)/N, of at least 0.5; and a cation equivalent expressed as a monovalent cation species, N + /Al, from 0.85 to 1.1 and the characteristic crystal structure of zeolite Y as indicated by an X-ray powder diffraction pattern having at least the d-spacings set forth broadly in Table A.

Claim 20

The process of claim 14 wherein the change in defect structure Δz is less than 0.05.

Claim 21

The process of claim 14 wherein the cation equivalent expresses a multivalent cation species, M +n /Al, where n is 2 or 3.

Claim 22

The process of claim 14 wherein ##EQU5## is greater than 3.5.

Claim 23

The process of claim 17 wherein ##EQU6## is greater than 4.0.

Claim 24

In a method for improving the operation with respect to feeds processed, catalyst regeneration and providing a high temperature operation for processing high boiling heavy residual oils in a riser cracking zone of a process comprising: providing a riser cracking zone in combination with an added second regeneration zone, said second regeneration zone adjacent to but above a restricted temperature regeneration zone, passing a suspension of hydrocarbon product vapor and catalyst flowing traverse of the riser cracking zone into a suspension breaking zone which promotes the downward flow of separated catalyst particles from product vapors entraining catalyst particles, passing the product vapors through a passageway immediately adjacent the suspension breaking zone in open communication with a cyclone separation zone, separating hydrocarbon product vapors from catalyst in said cyclone separation zone and recovering said hydrocarbon product vapors separately from cyclone separated catalyst, stripping catalyst separated from hydrocarbon vapors before downward passage thereof to a lower portion of a dense fluid bed of catalyst in said temperature restricted regeneration zone; effecting a partial regeneration of the catalyst in a dense fluid catalyst bed in said temperature restricted regenerating zone up to 1400° F. with an amount of oxygen sufficient to effect from 10 to 90 wt% removal of carbonaceous material and produce a flue gas rich in CO and provide catalyst particles with a residual carbon thereon, passing the partially regenerated catalyst through an external stripping zone and thence through a confined transfer zone to a bottom portion of the upper regeneration zone; further regenerating the partially regenerated catalyst comprising residual carbon in a dense fluid catalyst bed in the second regeneration zone at a temperature greater than 1500° F., and passing high temperature regenerated catalyst from said second regeneration zone through an external stripping zone before passage to said riser cracking zone for admixture with said high boiling heavy feed oil charged thereto; wherein the improvement comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consisting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 25

In a method for improving the operation with respect to feeds processed, catalyst regeneration and providing a high temperature operation for processing high boiling heavy residual oils in a riser cracking zone of a process comprising: providing a riser cracking zone in combination with an added second regeneration zone, said second regeneration zone adjacent to but above a restricted temperature regeneration zone, passing a suspension of hydrocarbon product vapor and catalyst flowing traverse of the riser cracking zone into a suspension breaking zone which promotes the downward flow of separated catalyst particles from product vapors entraining catalyst particles, passing the product vapors through a passageway immediately adjacent the suspension breaking zone in open communication with a cyclone separation zone, separating hydrocarbon product vapors from catalyst in said cyclone separation zone and recovering said hydrocarbon product vapors separately from cyclone separated catalyst, stripping catalyst separated from hydrocarbon vapors before downward passage thereof to a lower portion of a dense fluid bed of catalyst in said temperature restricted regeneration zone; effecting a partial regeneration of the catalyst in a dense fluid catalyst bed in said temperature restricted regenerating zone up to 1400° F. with an amount of oxygen sufficient to effect from 10 to 90 wt% removal of carbonaceous material and produce a flue gas rich in CO and provide catalyst particles with a residual carbon thereon, passing the partially regenerated catalyst through an external stripping zone and thence through a confined transfer zone to a bottom portion of the upper regeneration zone; further regenerating the partially regenerated catalyst comprising residual carbon in a dense fluid catalyst bed in the second regeneration zone at a temperature greater than 1500° F., and passing high temperature regenerated catalyst from said second regeneration zone through an external stripping zone before passage to said riser cracking zone for admixture with said high boiling heavy feed oil charged thereto; wherein the improvement comprises employing a catalyst comprising a zeolitic aluminosilicate selected from the group consisting of LZ-210, LZ-210-M, LZ-210-T, LZ-210-A and mixtures thereof.

Claim 26

The method of claim 19 wherein the said partial regeneration and further regeneration are carried out at a temperature above 1600° F.

Claim 29

The process of claim 21 wherein the zeolitic aluminosilicate is defined as having a chemical composition expressed in terms of mole fractions of framework tetrahedra as: [Al.sub.(a-N) Si.sub.b+(N-Δz) □.sub.z ]O.sub.2 wherein; ##EQU7## has a value greater than 6.0 the change in defect structure factor Δz is less than 0.08; an increased silicon content in the framework, (N-Δz)/N, of at least 0.5; and a cation equivalent expressed as a monovalent cation species, M + /Al, from 0.85 to 1.1 and the characteristic crystal structure of zeolite Y as indicated by an X-ray powder diffraction pattern having at least the d-spacings set forth broadly in Table A.

Claim 30

The process of claim 22 wherein "Δz" is less than 0.05.

Claim 31

The process of claim 22 wherein ##EQU8## has a value greater than 3.5.

Claim 32

The process of claim 24 wherein ##EQU9## has a value greater than 4.0.

Claim 33

The process of claim 21 wherein said regeneration is carried out in the presence of steam.