# US 11,111,443 B2 · Process and zeolitic catalyst for the catalytic cracking of unconventional light crude oil type shale/tight oil and its blends with vacuum gas oil

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- Number: US 11,111,443 B2
- Document ID: US11111443B2
- Status: Granted
- Kind: B2
- Application number: 16/109,360
- Filed: 2018-08-22
- Published: 2019-02-28
- Granted: 2021-09-07
- Earliest claimed: 2017-08-23
- Assignees: Instituto Mexicano Del Petroleo
- Applicants: Instituto Mexicano Del Petroleo
- Inventors: Blanca Lucia Medellin Rivera; Maria del Rosario Socorro Luna Ramirez; Edith Meneses Ruiz; Rogelio Hernandez Suarez; Agapito Alberto Neri Gomez; Guadalupe Hayde Moreno Vasquez; Gonzalo Hernandez Tapia; Roberto Garcia De Leon
- Web page: https://patentgrep.com/patent/US11111443B2

## CPC

- C10G 11/05: Crystalline alumino-silicates, e.g. molecular sieves
- B01J 29/084: {Y-type faujasite}
- B01J 29/088: {Y-type faujasite}
- B01J 29/40: of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J 29/405: {containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead}
- B01J 29/80: Mixtures of different zeolites
- B01J 35/40: characterised by dimensions, e.g. grain size (in a colloidal state B01J35/23; crystallite size B01J35/77)
- B01J 35/615: {100-500 m2/g}
- B01J 35/633: {less than 0.5 ml/g}
- B01J 2229/20: to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
- B01J 2229/36: Steaming
- B01J 2235/15: X-ray diffraction
- B01J 2523/3706: Lanthanum
- B01J 2523/3712: Cerium
- C10G 2300/1059: Gasoil having a boiling range of about 330 - 427 °C
- C10G 2300/1074: Vacuum distillates
- C10G 2300/4006: Temperature
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

## Abstract

The present invention deals with a process for catalytic cracking of hydrocarbons comprising vacuum gas oil, hydrotreated vacuum gas oil, unconventional light crude oil, preferably unconventional light crude oil type shale/tight oil and its blends with conventional vacuum gas oil, in order to generate products of major commercial value in the field of fuels, getting improved gasoline and coke yield, as well as the procedure for the preparation of a catalyst with essential physical properties of density and particle size to uphold it in a fluidized bed under the operation conditions in the catalyst evaluation unit at micro level, wherein the catalyst particles achieve a catalytic performance similar to fluidized microspheres in a reactor, without appreciable generation of fine particles.

## Claims

### Claim 1

A catalytic system, comprising:
a heterogeneous solid acid catalyst based on a formulation with at least one active zeolite comprising Faujasite Y zeolite and a coke selective active matrix;
wherein the active matrix is selected from a group consisting of gamma phase alumina, silica-alumina or silicon oxide, kaolin, aluminum chlorohydrate, or mixtures thereof and avoids the use of phosphate; and
hydrocarbon feedstocks consisting of vacuum gas oil (VGO), conventional vacuum gas oil, hydrotreated vacuum gas oil, unconventional light crude oil, or unconventional light crude oil type shale/tight oil and its blends with conventional vacuum gas oil, in a percentage range of from 0 to 100% by volume of unconventional light crude oil,
wherein the hydrocarbon feedstocks are placed in contact with the heterogeneous solid acid catalyst.

### Claim 2

A catalytic system, comprising:
a heterogeneous solid acid catalyst based on a formulation with at least one active zeolite comprising Faujasite Y zeolite and a coke selective active matrix;
wherein the active matrix is selected from a group consisting of gamma phase alumina, silica-alumina or silicon oxide, kaolin, aluminum chlorohydrate, or mixtures thereof and avoids the use of phosphate; and
hydrocarbon feedstocks consisting of vacuum gas oil (VGO), conventional vacuum gas oil, hydrotreated vacuum gas oil, unconventional light crude oil, or unconventional light crude oil type shale/tight oil and its blends with conventional vacuum gas oil, in a percentage range of from 0 to 100% by volume of unconventional light crude oil, put in contact with the heterogeneous solid acid catalyst.

### Claim 3 (depends on 2)

The catalytic system of claim 2, wherein the active zeolite further comprises a REY zeolite and a ZSM-5 zeolite.

### Claim 4 (depends on 3)

The catalytic system of claim 3, further comprising a binder comprising a peptized alumina.

### Claim 5 (depends on 2)

The catalytic system of claim 2, wherein the total surface area of catalyst is in the range from 350 m2/g to 450 m2/g, the zeolite surface area is in the range from 280 m2/g to 350 m2/g, the matrix area is in the range from 60 m2/g to 75 m2/g and the pore volume in the range of from 0.25 cm3/g to 0.35 cm3/g obtained by the Nitrogen desorption method.

### Claim 6 (depends on 2)

The catalytic system of claim 2, wherein the active zeolite comprising Faujasite Y zeolite further comprising a stabilizing metal selected from a group consisting of lanthanum (La), Cerium (Ce), or its mixtures.

### Claim 7 (depends on 2)

The catalytic system of claim 2, wherein the active zeolite comprising Faujasite Y zeolite further comprising a stabilizing metal; wherein the stabilizing metal comprises from 2.5% to 5.1% by weight of the catalyst.