Process for the treatment of heavy oils using light hydrocarbon components as a diluent

Patent metadata

Field	Value
Publication number	US-9260671-B2
Application number	US-50235709-A
Country	US
Kind code	B2
Filing date	Jul 14, 2009
Priority date	Jul 14, 2008
Publication date	Feb 16, 2016
Grant date	Feb 16, 2016

Abstract

The present invention relates to a process for the treatment of heavy oils using a catalytic hydrotreating process. More specifically, the invention relates to the presence of light hydrocarbon components in conjunction with the heavy oils for improved treatment of the heavy oils utilizing moderate temperature and pressure.

First claim

What is claimed is:

1. A process for upgrading of heavy oils comprising the steps of:
feeding a heavy oil feed stream to a hydrodemetalization reaction vessel, the hydrodemetalization reaction vessel containing a hydrodemetalization catalyst, the hydrodemetalization catalyst being operable to remove a substantial quantity of metal compounds from the heavy oil feed stream;
feeding a hydrogen source to the hydrodemetalization reaction vessel, the hydrogen source having a hydrogen pressure in the range of 50 to 150 bar; and
feeding a light hydrocarbon diluent to the hydrodemetalization reaction vessel, the light hydrocarbon diluent being substantially in liquid phase,
wherein the feeding of the heavy oil feed stream and the hydrogen source and the light hydrocarbon diluent to the hydrodemetalization reaction vessel defines a feed rate, the feed rate further defining a total liquid hourly space velocity within a predetermined liquid hourly space velocity range of 0.1 hr −1 to 5 hr −1 such that a combined effluent stream is produced and removed from the hydrodemetalization reaction vessel;
the process further comprising;
feeding the combined effluent stream to a hydrodesulfurization reaction vessel, the hydrodesulfurization reaction vessel containing a hydrodesulfurization catalyst operable to remove a substantial amount of sulfur from the combined effluent such that a hydrodesulfurization catalyst effluent is produced;
feeding the hydrodesulfurization catalyst effluent to a hydroconversion reaction vessel, the hydroconversion reaction vessel containing a hydroconversion catalyst, the hydroconversion catalyst being operable to convert the hydrodesulfurization catalyst effluent to a hydroconverted product, the hydroconverted product having, an increased API gravity as compared to the heavy oil feed stream;
feeding the hydroconverted product to a separation unit, the separation unit operable to separate the hydroconverted product into a process gas component stream and a liquid product;
feeding the liquid product to a flash vessel to separate a light hydrocarbon fraction and a final liquid product, the final liquid product having a reduced sulfur content, reduced metal content and increased API gravity in comparison to the heavy oil feed stream;
recycling at least a portion of the light hydrocarbon fraction to the hydrodemetalization reaction vessel; and
combining the recycled light hydrocarbon fraction with a fresh light hydrocarbon diluent to form the light hydrocarbon diluent and to thereby recycle the light hydrocarbon diluent to the hydrodemetalization reaction vessel to reduce coke formation.

2. The process of claim 1 , further comprising the step of:
recycling at least a portion of the process gas component stream to the hydrodemetalization reaction vessel.

3. The process of claim 1 wherein the separation unit is operable to remove sulfur components from the hydroconverted product.

4. The process of claim 1 wherein the sulphur removed, from the heavy feed oil stream in the hydrodesulfurization reaction vessel is at least 30 wt % of sulphur found in the heavy oil feed stream.

5. The process of claim 1 wherein
the light hydrocarbon diluent is a mixture of hydrocarbons derived from crude oil and defining a final boiling point,
the heavy oil feed stream further defines an initial boiling point, and
the final boiling point of the light hydrocarbon diluent does not exceed the initial boiling point of the heavy oil feed stream.

6. The process of claim 1 wherein at least a portion of the light hydrocarbon fraction is added to the heavy oil feed stream.

7. The process of claim 1 wherein the light hydrocarbon diluent is present at a ratio of at least 5 wt % compared to the heavy oil feed stream.

8. The process of claim 1 wherein the light hydrocarbon diluent comprises light hydrocarbons selected from the group consisting of C 15 -C 25 alkyl hydrocarbons.

9. The process of claim 1 wherein the light hydrocarbon diluent comprises less than about 30 wt % aromatics and has a final boiling point less than about 335° C.

10. The process of claim 1 wherein a ratio of the light hydrocarbon diluent to heavy crude oil in the heavy oil feed stream, while the process is at steady state, is 10 wt %, and a circulation rate of the light hydrocarbon diluent is between 5 wt % to 20 wt % of a feed of the fresh light hydrocarbon diluent for reduced crudes.

11. The process of claim 1 , wherein an average deactivation rate of hydroprocessing catalysts for the production of reduced sulfur crude oil is 1° C. per month.

12. A process for upgrading of heavy oils to increase diesel comprising the steps of:
feeding a heavy oil feed stream to a hydrodemetalization reaction vessel, the hydrodemetalization reaction vessel containing a hydrodemetalization catalyst, the hydrodemetalization catalyst being operable to remove a substantial quantity of metal compounds from the heavy oil feed stream;
feeding a hydrogen source to the hydrodemetalization reaction vessel, the hydrogen source having a hydrogen pressure in the range of 50 to 150 bar; and
feeding a light hydrocarbon diluent to the hydrodemetalization reaction vessel
wherein the feeding of the heavy oil feed stream and the hydrogen source and the light hydrocarbon diluent to the hydrodemetalization reaction vessel defines a feed rate, the feed rate further defining a total liquid hourly space velocity within a predetermined liquid hourly space velocity range of 0.1 hr −1 to 5 hr −1 that a combined, effluent stream is produced and removed from the hydrodemetalization reaction vessel;
the method further comprising:
feeding the combined effluent stream to a hydrodesulfurization reaction vessel, the hydrodesulfurization reaction vessel containing a hydrodesulfurization catalyst operable to remove a substantial amount of sulfur from the combined effluent such that a hydrodesulfurization catalyst effluent is produced;
feeding the hydrodesulfurization catalyst effluent to a separation unit, the separation unit operable to separate the hydrodesulfurization catalyst effluent into a process gas component stream and a liquid product;
recycling at least a portion of the gas component stream to the hydrodemetalization reaction vessel;
feeding the liquid product to a flash vessel to separate a light hydrocarbon fraction and a final liquid product, the final liquid product having a higher diesel content as compared to the heavy oil feed stream;
recycling at least a portion of the light hydrocarbon fraction to the hydrodemetalization reaction vessel; and
combining the recycled light hydrocarbon fraction with a fresh light hydrocarbon diluent to form the light hydrocarbon diluent and to thereby recycle the light hydrocarbon diluent to the hydrodemetalization reaction vessel to reduce coke formation.

Assignees

• Shafi Raheel
• Hamad Esam Z
• Kressmann Stephane Cyrille
• Alzaid Ali Hussain
• Saudi Arabian Oil Co

Inventors

• Shafi Raheel
• Hamad Esam Z
• Kressmann Stephane Cyrille
• Alzaid Ali Hussain

Classifications

• C10G2300/205

  Metal content · CPC title

• C10G65/12 Primary

  including cracking steps and other hydrotreatment steps · CPC title

• C10G2300/202

  Heteroatoms content, i.e. S, N, O, P · CPC title

• C10G2300/802

  Diluents · CPC title