Process for conversion of a cellulosic material

a cellulosic material and cellulosic technology, applied in the field of cellulosic material conversion, can solve the problems of improper handling of solid biomass feedstock, inability to convert non-edible cellulosic materials into biofuels, and inability to meet the requirements of biofuels,

Inactive Publication Date: 2013-05-16
SHELL OIL CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

[0022]Certain embodiments of the process according to the invention therefore provide a less critical process for conversion of a cellulosic material.

Problems solved by technology

Most of these non-edible cellulosic materials, however, are solid materials that are cumbersome to convert into biofuels.
A disadvantage of the process as described in WO2010 / 135734, however, is that proper handling of the biomass feedstock comprising the solid biomass particles is critical to avoid instability of the feedstock, clogging of feed lines to a fluidized catalytic cracking unit and / or coking in a fluidized catalytic cracking unit.
As explained in the article, fast polymerization reactions may cause plugging of a reactor.

Method used

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Examples

Experimental program
Comparison scheme
Effect test

example 1

[0145]About 30 grams of birch wood and 1.70 grams of palladium acetate (Pd(OAc)2) were loaded into a Premex Batch autoclave of 300 ml equipped with electrical heating, stirrer, injection system, manometer and temperature recording.

[0146]Stirring was started (300 rpm) and the autoclave was closed. Stirring speed was increased to 750 rpm and a solution of water (84 g), acetic acid (36 g) and sulphuric acid (0.86 g) was injected. The autoclave was pressurised with hydrogen (H2) to 4 MegaPascal (40 bar) and subsequently heated in 70 min to 200° C. Reactor pressure was subsequently increased to 8 MegaPascal (80 bar) by adding H2. The reaction was continued for 60 min, occasionally H2 was added to maintain the pressure at 8 MegaPascal. The reaction was stopped by rapid cooling to room temperature (20° C.), subsequently H2 was vented and 143.2 g of a first total product (including liquid, tar, insoluble humins and catalyst) was collected. In a duplo experiment applying identical conditions...

example 2

[0155]Furfural respectively furfuryl alcohol was used as an artificial representative of a final liquefied product. In addition a heavy feed mixture having a composition as illustrated in tables 2a and 2b was used as a fluid hydrocarbon co-feed.

TABLE 2aBoiling range distribution of the fluid hydrocarbon feed as determined bygas chromatography according to ASTM D2887-06a.wt %° C.wt %° C.wt %° C.IBP240344106847622813641470481430638417724866321404217449283334242576498103424442878504123514643280511143584843582519163655043884527183715244286548203775444588563223825644990585243875845392n.d.263926045894n.d.283976246296n.d.304016446798n.d.3240566471FBPn.d.n.d: not determined

TABLE 2bElement analyses of fluid hydrocarbon co-feed[C][H][O][S][N]Feed description.[wt %][wt %][wt %][ppm][ppm]fluid hydrocarbon co-feed86.65%12.65%0.00%33602220

[0156]The furfural respectively furfuryl alcohol was blended with the fluid hydrocarbon co-feed to prepare a feed mixture containing a weight percentage of 20 w...

example 3

[0163]Respectively tetrahydrofuran (THF), butanone and 2-butanol were used as an artificial representative of a final liquefied product. In addition a vacuum gas oil (VGO) was used as a fluid hydrocarbon co-feed.

[0164]The tetrahydrofuran (THF), butanone or 2-butanol respectively was blended with the fluid hydrocarbon co-feed to prepare a feed mixture containing a weight percentage of 20 wt % of tetrahydrofuran (THF), butanone or 2-butanol respectively, based on the total weight of the feed mixture. The feed mixture was injected into the fluidized catalyst bed of a MAT-5000 fluidized catalytic cracking unit. The fluidized catalyst bed contained 10 grams of FCC equilibrium catalyst containing ultra stable zeolite Y. The fluidized catalyst bed was kept at 550° C. and about 1 bar absolute (about 0.1 MegaPascal). The catalyst / feed weight ratio was 3.

[0165]The effective molar ratios of hydrogen to carbon (H / Ceff) of tetrahydrofuran (THF), butanone and 2-butanol respectively are 1.5, 1.5 a...

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Abstract

A process for conversion of a cellulosic material comprising
  • a) a liquefaction step, comprising
    • contacting a cellulosic material with a liquid solvent at a temperature of equal to or more than 200° C.; or
    • contacting a cellulosic material with a liquid solvent at a temperature of equal to or more than 100° C. in the presence of a catalyst,
  • to produce a final liquefied product;
  • b) a catalytic cracking step, comprising contacting at least part of the final liquefied product with a fluidized catalytic cracking catalyst at a temperature of equal to or more than 400° C., to produce one or more cracked products.

Description

[0001]This application claims the benefit of priority of European Patent Application No. 11189049.7, filed on Nov. 14, 2011, and of European Patent Application No. 12190054.2, filed on Oct. 25, 2012, the disclosures of which are incorporated by reference herein in their entirety.FIELD OF THE INVENTION[0002]Embodiments of the invention relate to a process for conversion of a cellulosic material and use of the products produced in such a process.BACKGROUND OF THE INVENTION[0003]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.[0004]With the diminishing supply of crude mineral oil, use of renewable energy sources i...

Claims

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Application Information

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Patent Type & Authority Applications(United States)
IPC IPC(8): C10G1/00C10L1/02
CPCC10G1/006C10L1/02C10G3/50C10G1/042C10G11/18C10G1/002Y02P30/20
Inventor LANGE, JEAN PAULSCHAVERIEN, COLIN JOHNWAY, NICOLAAS WILHELMUS JOSEPHGOSSELINK, JOHAN WILLEMHARRIS, JOHN WILLIAMBOON, ANDRIES QUIRIN MARIAJANSSEN, ANDRIES HENDRIKESPINOSA ALONSO, LETICIA
Owner SHELL OIL CO
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