Process of hydroconversion-distillation of heavy and/or extra-heavy crude oils

Patent metadata

Field	Value
Publication number	US-9920264-B2
Application number	US-201213598684-A
Country	US
Kind code	B2
Filing date	Aug 30, 2012
Priority date	Aug 31, 2011
Publication date	Mar 20, 2018
Grant date	Mar 20, 2018

Abstract

A process for hydroconversion-distillation of heavy and/or extra-heavy crude oils, which comprises four stages:
1) desalting and separation of the feedstock; 2) catalytic hydrotreating of light fraction (optional); 3) catalytic hydroconversion of heavy fraction, and 4) distillation of hydrotreated products

to provide products that can be processed in conventional refining schemes designed to operate with light and intermediate crude oils.

First claim

What is claimed is:

1. A process for the hydroconversion-distillation of heavy and extra heavy crude oils to obtain an upgraded crude oil, which comprises
desalting a feedstock comprising heavy and/or extra heavy crude oil at atmospheric pressure and at a temperature of 280° C. to 420° C. to obtain a desalted feedstock,
passing said desalted feedstock directly to a distillation zone where said desalted feedstock is subjected to a temperature in the range of from 280 to 420° C. at atmospheric pressure to obtain a light fraction and a heavy fraction, said light fraction containing light gas oil, naphtha and middle distillates having a boiling point of below 360° C., said heavy fraction containing asphaltenes and having a boiling point greater than 360° C.;
subjecting said light fraction to catalytic hydrotreatment in the presence of hydrogen to obtain a hydrotreated fraction and to remove sulfur and nitrogen compounds;
subjecting said heavy fraction to catalytic hydroconversion in the presence of hydrogen to obtain a hydroconverted fraction having a reduced the viscosity and increased the API gravity; and
feeding said hydrotreated fraction and said hydroconverted fraction to an atmospheric distillation apparatus to obtain a distilled light and medium fraction containing naphtha and middle distillates for processing in a process for light and medium crude oils and an atmospheric residue, separating said atmospheric residue and feeding to a vacuum distillation column and recovering a light as oil fraction, a heavy gas oil fraction, and a vacuum residue.

2. The process of claim 1 , wherein said feedstock comprises crude oil having 3 to 30 API gravity units.

3. The process of claim 2 , wherein said feedstock comprises crude oil having 3 to 10 API gravity units.

4. The process of claim 1 , wherein said catalytic hydrotreatment of said light fraction is carried out with catalysts of nickel-molybdenum (Ni—Mo) or cobalt-molybdenum (Co—Mo), in extruded or spherical shape.

5. The process of claim 1 , wherein said catalytic hydrotreatment of said light fraction is carried out at a pressure of 10 to 80 kg/cm 2 , hydrogen to hydrocarbon ratio of 350 to 3,000 ft 3 /bbl, temperature of 280 to 380° C. and the volumetric feed flow related to catalyst volume (LHSV) of 0.5 to 3 h −1 .

6. The process of claim 1 , wherein said heavy fraction has an initial boiling point above 360° C. and said catalytic hydroconversion of said heavy fraction is carried out in two or more fixed-bed reactors connected in series.

7. The process of claim 6 , wherein said fixed-bed reactor comprise three sequential zones having an increased catalyst concentration than a preceding fixed bed.

8. The process of claim 6 , wherein the catalysts of the fixed-bed reactors comprise metals selected from the group consisting of Pt, Pd, Ni, Mo and Co, at concentrations of 2 to 15 weight % of each one in the fresh catalysts.

9. The process of claim 8 , wherein said metals are selected from the group consisting of Ni, Mo and Co.

10. The process of claim 8 , wherein said catalysts are supported on aluminum oxides, silica, titanium, and mixtures thereof, and where said reactor has a first bed having a catalyst concentration of 0.1-3 wt %, Ni and 1-5 wt % Mo, a second bed having a catalyst concentration greater than said first bed and having catalyst concentration of 0.5-5 wt % Ni and 2-8 wt % Mo, and a third bed having a catalyst concentration greater than said second bed and having a catalyst concentration of 1-5 wt % Ni and 5-12 wt % Mo.

11. The process of claim 10 , wherein said support is aluminum oxide in its gamma phase and particle sizes ranging from 1 to 3 mm diameter in cylindrical or extruded with different profiles, tablets or lobular shapes.

12. The process of claim 7 , wherein a first zone of said three zones is loaded with a hydrodemetallization catalyst in concentrations of 0.1 to 3 weight % of nickel and from 1 to 5 weight % of molybdenum, supported on gamma alumina.

13. The process of claim 12 , wherein an intermediate zone is loaded with a hydrogenation-hydrocracking catalyst in concentrations of 0.5 to 5 weight % of nickel and 2 to 8 weight % of molybdenum, supported on gamma alumina and where said catalyst concentration of said intermediate zone is greater than said first zone.

14. The process of claim 13 , wherein a third zone is loaded with a hydrogenating catalyst in concentrations of 1 to 5 weight % of nickel and from 5 to 12 weight % of molybdenum supported on gamma alumina, and where said catalyst concentration of said third zone is greater than said intermediate zone.

15. The process of claim 6 , wherein said catalytic hydroconversion of said heavy fraction is carried out at a pressure of 40 to 130 kg/cm 2 , a hydrogen to hydrocarbon ratio of from 2,000 to 7,000 feet 3 /bbl, a temperature of 320 to 450° C. and the volumetric feed flow related to catalyst volume (LHSV) of 0.2 to 3 h −1 .

16. The process of claim 1 , wherein said vacuum residue has an API gravity higher than 22 units.

17. The process of claim 1 , wherein said process increases the volumetric yield of the fractions obtained from a heavy and/or extra-heavy crude oils: light naphtha up to 1%, intermediate naphtha up to 2%, heavy naphtha up to 3%, light distillate up to 4%, heavy distillate up to 7%, straight-run gas oil up to 5%, light vacuum gas oil up to 12%, and heavy vacuum gas oil up to 5%; in addition to a decrease of the vacuum residue as high as 30%.

18. The process of claim 1 , wherein said process removes impurities contained in heavy and/or extra-heavy crude oils: hydrodemetallization up to 90%, hydrodesulfurization up to 90%, hydrodenitrogenation up to 70%, carbon removal up to 60%, and asphaltenes removal up to 70%.

19. A process for the hydroconversion-distillation of extra heavy crude oils to obtain an upgraded crude oil, which comprises
desalting a feedstock comprising an extra heavy crude oil at atmospheric pressure and at a temperature of 280° C. to 420° C. using fresh water to obtain a desalted extra heavy crude oil feedstock,
passing the desalted extra heavy crude oil feedstock directly to a distillation column to separate the desalted extra heavy crude oil feedstock into a light fraction and a heavy fraction, said light fraction containing light gas oil having a boiling point below 360° C. and said heavy fraction having an initial boiling point above 360° C.;
subjecting said light fraction to catalytic hydrotreatment in the presence of hydrogen to reduce the concentration of sulfur and nitrogen compounds and to obtain a hydrotreated light fraction;
subjecting said heavy fraction to catalytic hydroconversion in the presence of hydrogen in a fixed-bed reactor having a first bed, a second bed, and a third bed connected in series with hydrogen added to an inlet and along the catalyst beds of the second reactor, each of said fixed-bed reactors contains a Ni—Mo catalyst supported on gamma alumina and where said first bed comprises a catalyst having 0.1-3 wt % No and 1-5 wt % Mo, a second bed comprising a catalyst having 0.5 to 5 wt % Ni and 2-8 wt % Mo and has a catalyst concentration greater than said first bed, and a third bed comprising a catalyst having 1-5 wt % Ni and 5-12 wt % Mo and a catalyst concentration greater than said second bed, said catalytic hydroconversion being carried out to remove sulfur and nitrogen compounds from said heavy fraction and increase the API gravity; and
feeding said hydrotreated light fraction and said catalytic hydroconversion heavy fraction to an atmospheric distil

Assignees

• Ancheyta Juarez Jorge
• Munoz Moya Jose Antonio Domingo
• Castaneda Lopez Luis Carlos
• Ramirez Amador Sergio
• Marroquin Sanchez Gustavo Jesus
• Centeno Nolasco Guillermo
• Alonso Martinez Fernando
• Aguilar Escalante Rodolfo Antonio
• Mexicano Inst Petrol

Inventors

• Ancheyta Juarez Jorge
• Muñoz Moya Jose Antonio Domingo
• Castañeda Lopez Luis Carlos
• Ramirez Amador Sergio
• Marroquin Sanchez Gustavo Jesus
• Centeno Nolasco Guillermo
• Alonso Martinez Fernando
• Aguilar Escalante Rodolfo Antonio

Classifications

• C10G45/08

  in combination with chromium, molybdenum, or tungsten metals, or compounds thereof · CPC title

• C10G47/14

  the catalyst containing platinum group metals or compounds thereof · CPC title

• C10G67/00 Primary

  Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only · CPC title

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title

• C10G65/14

  plural parallel stages only · CPC title