Methods and systems for processing cellulosic biomass

A biomass and logistics technology, applied in the use of microorganism/enzyme cellulose treatment, pulping of cellulose raw materials, biological raw materials, etc., can solve the problems of high cost, system downtime, low conversion rate, etc.

Inactive Publication Date: 2017-08-29
SHELL INT RES MAATSCHAPPIJ BV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] Furthermore, in addition to the desired carbohydrates, other substances may also be present within the cellulosic biomass, which may be particularly difficult to process in an energy- and cost-effective manner
For example, during cellulosic biomass processing, the high amounts of lignin present in cellulosic biomass can cause fouling of processing equipment, which can lead to costly system downtime
Lignin also results in a relatively low conversion rate of cellulosic biomass to usable matter per unit weight of feedstock
[0008] As demonstrated above, efficient conversion of cellulosic biomass into fuel blends and other materials is a complex problem that presents great engineering challenges

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

[0182] Example 1: Distillation of the total reactor contents

[0183] A 450ml Parr reactor is 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% by weight), and less than 2% nickel) supported on alumina, the catalyst is obtained from Criterion Catalyst&Technologies LP and Vulcanization was carried out by the method described in Example 5 of US2010 / 0236988.

[0184] Then, 14.02 grams of small pieces of southern pine (10% moisture) with a nominal size of 3×5×5mm were loaded into the reactor, and then pressurized with 52 bar of hydrogen, and heated to 190°C for 1 Hours, then slowly increase the temperature to 245°C and keep it for 2.5 hours.

[0185] After the reaction, the reactor was cooled and depressurized. A nominal 14 grams of wood chips were added, then...

example 2

[0195] Example 2: Separation by extraction followed by distillation of the phases

[0196] Using 5.035 grams of RaneyTM cobalt catalyst (WR Grace 2724), and a solvent containing 21.1 grams of 2,6-xylenol as the phenolic solvent, Example 1 was repeated. The 2,6-xylenol was first dissolved to 7.00 grams of methyl isopropyl alcohol. In butyl methanol, and 182.01 grams of deionized water was added to the 450ml reactor. The reaction cycle was carried out at 160°C for 1 hour, then at 190°C for 1 hour, and then at 240°C for 3 hours. Six cycles of wood addition were performed, followed by heating overnight at 270°C under 52 bar H2 to complete the conversion of the intermediate.

[0197] At the end of the reaction procedure, 87.03 grams of toluene (a simulated aromatic gasoline product) was added to the reactor, and the reactor was stirred at 150°C for 2 hours to achieve extraction. Then the stirring was stopped and the reactor was allowed to cool. 127.39 g of the upper toluene-rich phas...

example 3

[0210] Example 3: Adding miscible solvents

[0211] A 75 ml Parr 5000 reactor was charged with 3.01 g of xylenol (2,6-dimethylphenol), 21.07 g of deionized water, 0.107 g of potassium carbonate buffer, and 0.301 g of Raney cobalt 2724 catalyst (WR Grace ). Load 2.0 grams of ground American longleaf pine (nominal 10% moisture). The reactor was pressurized to 52 bar with hydrogen and heated to 190°C for 1 hour, then to 240°C for 4 hours.

[0212] Three more cycles of nominal 2.0 grams of wood addition are completed, and then the last cycle needs to be pressurized with hydrogen to 35 bar and heated to 270°C for 15 hours to expand the degree of conversion of the hydrodeoxygenation reaction.

[0213] At the end of the conversion cycle, the reactor is cooled and depressurized. 44.3 grams of acetone was added to dissolve all reactor contents. As confirmed by magnetic attraction, 0.3 g of recovered catalyst was obtained by filtration, in which there were no visible organic solids and no ...

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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

[0001] Cross references to related applications [0002] This application claims the benefits of U.S. Provisional Application No. 62 / 097756, which was filed on December 30, 2014. Background technique [0003] This section is intended to introduce various aspects in the art that may be related to exemplary embodiments of the invention. It is believed that this discussion helps to provide a framework to facilitate a better understanding of certain aspects of the invention. Therefore, it should be understood that this section should be read from this perspective and not necessarily as an endorsement of any prior art. [0004] The present disclosure generally relates to the processing of cellulosic biomass solids, and more specifically, to methods and systems for processing lignin-containing reaction products that can be obtained by the hydrothermal reaction of cellulosic biomass. [0005] A variety of commercially important substances can be manufactured from natural sources including b...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G3/00C10G7/00C10G1/00C10G1/06C10G1/08C10G21/00D21C3/20D21C3/22D21C5/00D21C11/00
CPCC10G1/002C10G1/065C10G1/083C10G3/50C10G7/00C10G21/00C10G2300/1014D21C3/20D21C3/222D21C5/005D21C11/0007D21C11/0042Y02P30/20
Inventor J·B·鲍威尔G·C·康姆普林J·N·驰赫达
Owner SHELL INT RES MAATSCHAPPIJ BV
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