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Methods and systems for processing cellulosic biomass

Inactive Publication Date: 2016-06-30
SHELL OIL CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

This patent describes a process for separating compounds from a reaction product. The process involves extracting a liquid phase containing compounds from a larger liquid phase containing non-water miscible compounds. The separated liquid phase is then treated to recover light compounds. The non-aqueous phase can also be treated to reduce its viscosity and improve product separation. The non-aqueous phase can then be distilled to separate the compounds. The process can allow for more efficient separation of compounds at lower temperatures and can recover more light compounds.

Problems solved by technology

Recovery of various compounds from a product of reactions involving cellulosic biomass may be challenging due to the various components contained therein, including lignin.
While feasible, distillation of a reaction product with multiple liquid phases that contains water into various product fractions can result in poor product separation and steam stripping, where water vapors carry heavier compounds, like phenols, into the overhead fraction.
Although this may be addressed by conducting the distillation at higher pressure and temperature where multiple phases can be reduced or minimized, the higher pressure and temperature presents additional expenses including equipment costs, as well as risks to product from onset of undesired degradation reactions at higher temperatures.
While the water in the reaction product can be removed through flashing prior to full distillation into product fractions, doing so can also result in steam stripping, thereby resulting in less efficient product separation in a subsequent distillation process.
The complex mixture of constituents that is co-present with the cellulose can make its processing difficult, as discussed hereinafter.
Lignin, in particular, may be an especially difficult constituent to deal with.

Method used

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  • Methods and systems for processing cellulosic biomass
  • Methods and systems for processing cellulosic biomass
  • Methods and systems for processing cellulosic biomass

Examples

Experimental program
Comparison scheme
Effect test

example 1

Distillation of Total Reactor Contents

[0157]A 450-ml Parr reactor was charged with 20.02 grams of 2-methoxy-4-propylphenol (MPP), 190.01 grams of deionized water, 0.4192 grams of potassium hydroxide buffer, and 7.2522 grams of nickel-oxide promoted cobalt molybdate catalyst (DC-2534, containing 1-10% cobalt oxide and molybdenum trioxide (up to 30 wt %) on alumina, and less than 2% nickel), obtained from Criterion Catalyst & Technologies L.P., and sulfided by the method described in US2010 / 0236988 Example 5.

[0158]The reactor was then charged with 14.02 grams of southern pine mini-chips (10% moisture), of nominal size 3×5×5 mm in dimension, before pressuring with 52 bar of hydrogen, and heating to 190° C. for 1 hours, then ramping to 245° C. for 2.5 hours.

[0159]After reaction, the reactor was cooled and depressured. A nominal 14 grams of wood chips were added, followed by repressuring with 52 bar H2, and conducting a second reaction cycle using the same heating profile. The sequence w...

example 2

Separation by Extraction Followed by Distillation of Separate Phases

[0169]Example 1 was repeated using 5.0035 grams of Raney™ cobalt catalyst (WR Grace 2724), and a solvent comprising of 21.1 grams of 2,6-xylenol as the phenolic solvent, solubilized first into 7.00 grams of methylisobutylcarbinol, and added together with 182.01 grams of deionized water to the 450-ml reactor. Reaction cycles entailed 1 hour at 160° C., followed by 1 hour at 190° C., followed by 3 hours at 240° C. Six cycles of wood addition were effected, followed by heating overnight at 270° C. under 52 bar of H2 to complete the conversion of intermediates.

[0170]At the end of the reaction sequence, 87.03 grams of toluene (simulated aromatics gasoline product) were added to the reactor, and the reactor was stirred at 150° C. for 2 hours to effect extraction. Stirring was then stopped, and the reactor was allowed to cool. An upper toluene-rich phase of 127.39 grams was decanted, followed by 220.65 grams of a lower aqu...

example 3

Miscibilizing Solvent Addition

[0181]A 75-ml Parr5000 reactor was charged with 3.01 grams of xylenol (2,6-dimethylphenol) and 21.07 grams of deionize water, 0.107 grams of potassium carbonate buffer, and 0.301 grams of Raney Cobalt 2724 catalyst (WR Grace). 2.0 grams of ground Southern pine wood (nominal 10% moisture) were charged. The reactor was pressured to 52 bar with hydrogen, and heated to 190° C. for 1 hour, followed by heating to 240° C. for 4 hours.

[0182]Three more cycles of nominal 2.0 grams of wood addition were completed, before a final cycle entailing pressuring to 35 bar with hydrogen, and heating to 270° C. for 15 hours to extend the extent pf conversion of hydrodeoxygenation reactions.

[0183]At the end of the conversion cycle, the reactor was cooled and depressured. 44.3 grams of acetone were added to dissolve all reactor contents. Filtration yielded 0.3 grams of recovered catalyst, as evidenced by magnetic attraction, with no visible organic solids present, and no dep...

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Abstract

Separation of a product of digestion of cellulosic biomass solids may be challenging due to the various components contained therein. Methods and systems for processing cellulosic biomass, particularly a reaction product of a hydrothermal reaction containing lignin-derived products, such as phenolics, comprise providing the reaction product of a further processing (such as condensation reaction) to a non-aqueous stream to at least part precipitate the lignin and removing the precipitated lignin.

Description

CROSS-REFERENCE TO RELATED APPLICATION[0001]The present application claims the benefit of pending U.S. Provisional Application Ser. No. 62 / 097,756, filed 30 Dec. 2014, the entire disclosure of which is hereby incorporated by reference.BACKGROUND OF THE INVENTION[0002]This section is intended to introduce various aspects of the art, which may be associated with exemplary embodiments of the present invention. This discussion is believed to assist in providing a framework to facilitate a better understanding of particular aspects of the present invention. Accordingly, it should be understood that this section should be read in this light, and not necessarily as admissions of any prior art.[0003]The present disclosure generally relates to processing of cellulosic biomass solids, and, more specifically, to methods and systems for processing a reaction product comprising lignin that may be obtained by a hydrothermal reaction of cellulosic biomass.[0004]A number of substances of commercial...

Claims

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Application Information

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IPC IPC(8): C10G1/06C10G21/00C10G7/00C10G1/00
CPCC10G1/065C10G7/00C10G21/00C10G1/002C10G1/083C10G3/50C10G2300/1014D21C3/20D21C3/222D21C5/005D21C11/0007D21C11/0042Y02P30/20
Inventor POWELL, JOSPEH BROUNKOMPLIN, GLENN CHARLESCHHEDA, JUBEN NEMCHAND
Owner SHELL OIL CO
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