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Systems, methods, and catalysts for producing a crude product

a technology of crude feed and catalyst, applied in the direction of hydrocarbon oil treatment, hydrocarbon oil cracking, catalytic cracking, etc., can solve the problems of high tan, high cost of corrosion-resistant metal, and inability to use corrosion-resistant metal in existing equipment, etc., to achieve the effect of reducing the conten

Inactive Publication Date: 2005-06-23
SHELL OIL CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

The invention provides methods for converting a crude feed into a crude product that includes a liquid mixture. The methods involve using catalysts that have a specific pore size distribution and a specific molar ratio of metals. The catalysts are designed to have a specific pore size distribution that allows for optimal contact with the crude feed and the resulting crude product. The methods also involve controlling contacting conditions to achieve the desired pore size distribution and TAN (titanium dioxide activity) in the crude product. The invention also provides catalyst compositions that include specific metals and a support material with a specific pore size distribution. The technical effects of the invention include improved conversion of crude feed to crude product and improved quality of the resulting crude product.

Problems solved by technology

Disadvantaged crudes with a relatively high TAN may contribute to corrosion of metal components during transporting and / or processing of the disadvantaged crudes.
The use of corrosion-resistant metal often involves significant expense, and thus, the use of corrosion-resistant metal in existing equipment may not be desirable.
The use of corrosion inhibitors may negatively affect equipment used to process the crudes and / or the quality of products produced from the crudes.
Disadvantaged crudes often contain relatively high levels of residue.
Such high levels of residue tend to be difficult and expensive to transport and / or process using conventional facilities.
Organically bound heteroatoms may, in some situations, have an adverse effect on catalysts.
During processing of such crudes, metal contaminants and / or compounds of metal contaminants, may deposit on a surface of the catalyst or in the void volume of the catalyst.
Such deposits may cause a decline in the activity of the catalyst.
It may be costly to regenerate the catalytic activity of a catalyst contaminated with coke.
High temperatures used during regeneration may also diminish the activity of the catalyst and / or cause the catalyst to deteriorate.
Moreover, the metals in metal salts of organic acids may cause rapid deactivation of catalysts.
Treatment facilities that process disadvantaged crudes with an oxygen content of at least 0.002 grams of oxygen per gram of disadvantaged crude may encounter problems during processing.
Organic oxygen compounds, when heated during processing, may form higher oxidation compounds (for example, ketones and / or acids formed by oxidation of alcohols, and / or acids formed by oxidation of ethers) that are difficult to remove from the treated crude and / or may corrode / contaminate equipment during processing and cause plugging in transportation lines.
When processing of hydrogen deficient hydrocarbons, consistent quantities of hydrogen generally need to be added, particularly if unsaturated fragments resulting from cracking processes are produced.
Hydrogen is costly to produce and / or costly to transport to treatment facilities.
Disadvantaged crudes also tend to exhibit instability during processing in conventional facilities.
Crude instability tends to result in phase separation of components during processing and / or formation of undesirable by-products (for example, hydrogen sulfide, water, and carbon dioxide).
Conventional processes often lack the ability to change a selected property in a disadvantaged crude without also significantly changing other properties in the disadvantaged crude.
For example, conventional processes often lack the ability to significantly reduce TAN in a disadvantaged crude while, at the same time, only changing by a desired amount the content of certain components (such as sulfur or metal contaminants) in the disadvantaged crude.
Adding diluent, however, generally increases costs of treating disadvantaged crudes due to the costs of diluent and / or increased costs to handle the disadvantaged crudes.
Addition of diluent to a disadvantaged crude may, in some situations, decrease stability of such crude.
The processes, systems, and catalysts described in these patents, however, have limited applicability because of many of the technical problems set forth above.
In sum, disadvantaged crudes generally have undesirable properties (for example, relatively high TAN, a tendency to become unstable during treatment, and / or a tendency to consume relatively large amounts of hydrogen during treatment).
Other undesirable properties include relatively high amounts of undesirable components (for example, residue, organically bound heteroatoms, metal contaminants, metals in metal salts of organic acids, and / or organic oxygen compounds).
Such properties tend to cause problems in conventional transportation and / or treatment facilities, including increased corrosion, decreased catalyst life, process plugging, and / or increased usage of hydrogen during treatment.

Method used

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  • Systems, methods, and catalysts for producing a crude product
  • Systems, methods, and catalysts for producing a crude product
  • Systems, methods, and catalysts for producing a crude product

Examples

Experimental program
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example 1

[0278] Preparation of a Catalyst Support. A support was prepared by mulling 576 grams of alumina (Criterion Catalysts and Technologies LP, Michigan City, Mich., U.S.A.) with 585 grams of water and 8 grams of glacial nitric acid for 35 minutes. The resulting miulied mixture was extruded through a 1.3 Trilobe™ die plate, dried between 90-125° C., and then calcined at 918° C., which resulted in 650 grams of a calcined support with a median pore diameter of 182 Å. The calcined support was placed in a Lindberg furnace. The furnace temperature was raised to about 1000-1100° C. over 1.5 hours, and then held in this range for 2 hours to produce the support. The support included, per gram of support, 0.0003 grams of gamma alumina, 0.0008 grams of alpha alumina, 0.0208 grams of delta alumina, and 0.9781 grams of theta alumina, as determined by x-ray diffraction. The support had a surface area of 110 m2 / g and a total pore volume of 0.821 cm3 / g. The support had a pore size distribution with a m...

example 2

[0280] Preparation of a Vanadium Catalyst Having a Pore Size Distribution With a Median Pore Diameter of At Least 230 Å. The vanadium catalyst was prepared in the following manner. The alumina support, prepared by the method described in Example 1, was impregnated with a vanadium impregnation solution prepared by combining 7.69 grams of VOSO4 with 82 grams of deionized water. A pH of the solution was about 2.27.

[0281] The alumina support (100 g) was impregnated with the vanadium impregnation solution, aged for 2 hours with occasional agitation, dried at 125° C. for several hours, and then calcined at 480° C. for 2 hours. The resulting catalyst contained 0.04 grams of vanadium, per gram of catalyst, with the balance being support. The vanadium catalyst had a pore size distribution with a median pore diameter of 350 Å, a pore volume of 0.69 cm3 / g, and a surface area of 110 m2 / g. Additionally, 66.7% of the total number of pores in the pore size distribution of the vanadium catalyst ha...

example 3

[0283] Preparation of a Molybdenum Catalyst having a Pore Size Distribution With a Median Pore Diameter of At Least 230 Å. The molybdenum catalyst was prepared in the following manner. The alumina support prepared by the method described in Example 1 was impregnated with a molybdenum impregnation solution. The molybdenum impregnation solution was prepared by combining 4.26 grams of (NH4)2Mo2O7, 6.38 grams of MoO3, 1.12 grams of 30% H2O2, 0.27 grams of monoethanolamine (MEA), and 6.51 grams of deionized water to form a slurry. The slurry was heated to 65° C. until dissolution of the solids. The heated solution was cooled to room temperature. The pH of the solution was 5.36. The solution volume was adjusted to 82 mL with deionized water.

[0284] The alumina support (100 grams) was impregnated with the molybdenum impregnation solution, aged for 2 hours with occasional agitation, dried at 125° C. for several hours, and then calcined at 480° C. for 2 hours. The resulting catalyst containe...

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Abstract

Methods and systems for contacting of a crude feed with one or more catalysts produces a total product that includes a crude product are described. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. The produced crude product may include at least one of the catalysts.

Description

PRIORITY CLAIM [0001] This application claims priority to Provisional Patent Application No. 60 / 531,506 entitled “METHODS OF PREPARING IMPROVED CRUDE FEED” filed on Dec. 19, 2003, and to Provisional Patent Application No. 60 / 618,681 entitled “SYSTEMS, METHODS, AND CATALYSTS FOR PRODUCING A CRUDE PRODUCT” filed on Oct. 14, 2004.FIELD OF THE INVENTION [0002] The present invention generally relates to systems, methods, and catalysts for treating crude feed, and to compositions that can be produced using such systems, methods, and catalysts. More particularly, certain embodiments described herein relate to systems, methods, and catalysts for conversion of a crude feed to a total product, wherein the total product includes a crude product that is a liquid mixture at 25° C. and 0.101 MPa and has one or more properties that are changed relative to the respective property of the crude feed. DESCRIPTION OF RELATED ART [0003] Crudes that have one or more unsuitable properties that do not allo...

Claims

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Application Information

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Patent Type & Authority Applications(United States)
IPC IPC(8): C10G11/02C10G11/08C10G29/06C10G45/02C10G45/04C10G45/08C10G47/02C10G47/12
CPCC10G29/06C10G45/02C10G45/04C10G45/08C10G2300/107C10G2300/308C10G2300/202C10G2300/203C10G2300/205C10G2300/301C10G2300/302C10G2300/1074
Inventor BHAN, OPINDER KISHANWELLINGTON, SCOTT LEE
Owner SHELL OIL CO
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