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Methods for producing a crude product from selected feed

a technology of crude products and feed, applied in the field of systems and methods for treating feed, can solve the problems of difficult and expensive transportation and/or processing of crude using conventional facilities, difficult water removal of less viscous crude and/or crude mixtures using conventional means, and disadvantaged crudes often contain relatively high residue levels

Inactive Publication Date: 2007-12-27
SHELL OIL CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

The patent describes systems and methods for producing a total product by contacting a feed with a supported inorganic salt catalyst in the presence of a hydrogen source and steam. The system can separate inorganic salts from the combustion gas produced during the process. The invention also provides methods for controlling the contacting conditions to optimize the conversion of the feed to hydrocarbon gas and liquid. The technical effects of the invention include improved efficiency in the production of crude products and the ability to produce non-condensable gas.

Problems solved by technology

Disadvantaged crudes often contain relatively high levels of residue.
Such crudes tend to be difficult and expensive to transport and / or process using conventional facilities.
During processing, water removal from the less viscous crudes and / or crude mixtures may be difficult using conventional means.
When processing hydrogen deficient hydrocarbons, consistent quantities of hydrogen generally need to be added, particularly if unsaturated fragments resulting from cracking processes are produced.
Processes such as reforming that are used to produce hydrogen are generally endothermic and, typically, require additional heat.
Hydrogen and / or heat is costly to produce and / or costly to transport to treatment facilities.
It may be costly to regenerate the catalytic activity of a catalyst contaminated by coke.
High temperatures used during regeneration may also diminish the activity of the catalyst and / or cause the catalyst to deteriorate.
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.
Such deposits may cause a decline in the activity of the catalyst.
Organically bound heteroatoms may, in some situations, have an adverse effect on catalysts.
These processes tend to result in poor desulfurization efficiency, production of oil insoluble sludge, poor demetallization efficiency, formation of substantially inseparable salt-oil mixtures, utilization of large quantities of hydrogen gas, and / or relatively high hydrogen pressures.
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 process, 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 residue, a tendency to corrode equipment, 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, relatively high TAN, organically bound heteroatoms, and / or metal contaminants).
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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  • Methods for producing a crude product from selected feed
  • Methods for producing a crude product from selected feed
  • Methods for producing a crude product from selected feed

Examples

Experimental program
Comparison scheme
Effect test

example 1

[0253] TAP Testing of a K2CO3 / Rb2CO3 / Cs2CO3 Catalyst and the Individual Inorganic Salts. In all TAP testing, a 300 mg sample was heated in a reactor of a TAP system from room temperature (about 27° C.) to 500° C. at a rate of about 50° C. per minute. Emitted water vapor and carbon dioxide gas were monitored using a mass spectrometer of the TAP system.

[0254] The K2CO3 / Rb2CO3 / Cs2CO3 catalyst supported on alumina showed a current inflection of greater than 0.2 volts for emitted carbon dioxide and a current inflection of 0.01 volts for emitted water from the inorganic salt catalyst at about 360° C. The minimum TAP temperature was about 360° C., as determined by plotting the log 10 of the ion current versus temperature. FIG. 10 is a graphical representation of log 10 plots of ion current of emitted gases from the K2CO3 / Rb2CO3 / Cs2CO3 catalyst (“log(I)”) versus temperature (“T”). Curves 232 and 234 are log 10 values for the ion currents for emitted water and CO2 from the inorganic salt ca...

example 2

[0257] DSC Testing of an Inorganic Salt Catalyst and Individual Inorganic Salts. In all DSC testing, a 10 mg sample was heated to 520° C. at a rate of 10° C. per min, cooled from 520° C. to 0.0° C. at rate of 10° C. per minute, and then heated from 0° C. to 600° C. at a rate of 10.0° C. per min using a differential scanning calorimeter (DSC) Model DSC-7, manufactured by Perkin-Elmer (Norwalk, Conn., U.S.A.).

[0258] DSC analysis of a K2CO3 / Rb2CO3 / Cs2CO3 catalyst during second heating of the sample shows that the salt mixture exhibited a broad heat transition between 219° C. and 260° C. The midpoint of the temperature range was about 250° C. The area under heat transition curve was calculated to be 1.75 Joules per gram. The beginning of crystal disorder was determined to start at the minimum DSC temperature of 219° C.

[0259] In contrast to these results, no definite heat transitions were observed for cesium carbonate.

[0260] DSC analysis of a mixture of Li2CO3, Na2CO3, and K2CO3 durin...

example 3

[0261] Ionic Conductivity Testing of an Inorganic Salt Catalysts or an Individual Inorganic Salt Relative to K2CO3. All testing was conducted by placing 3.81 cm (1.5 inches) of the inorganic salt catalysts or the individual inorganic salts in a quartz vessel with platinum or copper wires separated from each other, but immersed in the sample in a muffle furnace. The wires were connected to a 9.55 volt dry cell and a 220,000 ohm current limiting resistor. The muffle furnace was heated to 600° C. and the current was measured using a microammeter.

[0262]FIG. 11 is a graphical representation of log plots of the sample resistance relative to potassium carbonate resistance (“log(rK2CO3)”) versus temperature (“T”). Curves 240, 242, 244, 246, and 248 are log plots of K2CO3 resistance, CaO resistance, K2CO3 / Rb2CO3 / Cs2CO3 catalyst resistance, Li2CO3 / K2CO3 / Rb2CO3 / Cs2CO3 catalyst resistance, and Na2CO3 / K2CO3 / Rb2CO3 / Cs2CO3 catalyst resistance, respectively.

[0263] CaO (curve 242) exhibits relativ...

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Abstract

Methods of producing a crude product are described. A method includes providing a feed and a supported inorganic salt catalyst to a contacting zone. The feed has at total content, per gram of feed, of at least 0.9 grams of hydrocarbons having a boiling range distribution between 343° C. and 538° C. Contact of the supported inorganic salt catalyst with the feed in the presence of a hydrogen source and steam is performed such that the supported inorganic salt catalyst becomes fluidized, and a total product that includes a crude product is produced. The crude product has a total content of at least 0.2 grams per gram of crude product of hydrocarbon have a boiling range distribution between 204° C. and 343° C.

Description

CROSS REFERENCE TO RELATED APPLICATION [0001] This application claims the benefit of U.S. Provisional Application 60 / 805,570 filed Jun. 22, 2006, the entire disclosure of which is hereby incorporated by reference.FIELD OF THE INVENTION [0002] The present invention generally relates to systems and methods for treating feed, and to compositions that are produced, for example, using such systems and methods. DESCRIPTION OF RELATED ART [0003] Crudes that have one or more unsuitable properties that do not allow the crudes to be economically transported, or processed using conventional facilities, are commonly referred to as “disadvantaged crudes”. [0004] Disadvantaged crudes often contain relatively high levels of residue. Such crudes tend to be difficult and expensive to transport and / or process using conventional facilities. High residue crudes may be treated at high temperatures to convert the crude to coke. Alternatively, high residue crudes are typically treated with water at high t...

Claims

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Application Information

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Patent Type & Authority Applications(United States)
IPC IPC(8): C10G25/00
CPCC10G47/30
Inventor BROWNSCOMBE, THOMAS FAIRCHILDGILLESPIE, WILLIAM DOUGLASMO, WEIJIANPARUCHURI, ESWARACHANDRA KUMARPFREHM, SUSAN SECORRAMACHANDRAN, CHEN ELIZABETHWALLACE, DAVID WILLIAMWELLINGTON, SCOTT LEE
Owner SHELL OIL CO
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