Patent Publication Number: US-2015080622-A1

Title: Methods and systems for supplying hydrogen to a hydrocatalytic reaction

Description:
RELATED APPLICATIONS 
     This application claims the benefit of U.S. Provisional Application No. 61/879,422, filed on Sep. 18, 2013, and U.S. Provisional Application No. 61/919,142, filed on Dec. 20, 2013, the disclosures of which are incorporated herein by reference in their entirety. 
    
    
     TECHNICAL FIELD 
     The present disclosure generally relates to a hydrocatalytic reaction and more specifically, to systems and methods supplying hydrogen to the hydrocatalytic reaction through gasification of a fraction of a product stream of the hydrocatalytic reaction and recovery of one or more organic volatile compounds in the fraction. 
     BACKGROUND 
     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. 
     A number of substances of commercial significance may be produced from natural sources, including biomass. Cellulosic biomass may be particularly suitable in this regard due to the versatility of the abundant carbohydrates found therein in various forms. As used herein, the term “cellulosic biomass” refers to a living or formerly living biological material that contains cellulose. The lignocellulosic material found in the cell walls of plants is one of the world&#39;s largest sources of carbohydrates. Materials commonly produced from cellulosic biomass may include, for example, paper and pulpwood via partial digestion, biofuels, including bioethanol by fermentation. 
     Development of fossil fuel alternatives derived from renewable resources have received recent attention. Cellulosic biomass has garnered particular attention in this regard due to its abundance and the versatility of the various constituents found therein, particularly cellulose and other carbohydrates. Despite promise and intense interest, the development and implementation of bio-based fuel technology has been slow. Existing technologies have heretofore produced fuels having a low energy density (e.g., bioethanol) and/or that are not fully compatible with existing engine designs and transportation infrastructure (e.g., methanol, biodiesel, Fischer-Tropsch diesel, hydrogen, and methane). Moreover, conventional bio-based processes have typically produced intermediates in dilute aqueous solutions (&gt;50% water by weight) that are difficult to further process. Energy- and cost-efficient processes for processing cellulosic biomass into fuel blends having similar compositions to fossil fuels would be highly desirable to address the foregoing issues and others. 
     When converting cellulosic biomass into fuel blends and other materials, cellulose and other complex carbohydrates therein can be extracted and transformed into simpler organic molecules, which can be further processed thereafter. Subsequent transforming reactions include various hydrocatalytic reactions, such as hydrogenation and/or hydrogenolysis reactions, which require hydrogen. While external hydrogen can be provided, such a hydrogen source may not help reduce the carbon footprint of any eventual fuel product, such as when it is based on natural gas reforming. 
     Further, in addition to the desired carbohydrates, other substances may be present within cellulosic biomass that can be especially problematic to deal with in an energy- and cost-efficient manner. For example, during cellulosic biomass processing, the significant quantities of lignin and/or lignin-derived compounds present in cellulosic biomass may lead to fouling of processing equipment, potentially leading to costly system down time. The significant lignin quantities can also lead to realization of a relatively low conversion of the cellulosic biomass into usable substances per unit weight of feedstock. 
     As evidenced by the foregoing, the efficient conversion of cellulosic biomass into fuel blends and other materials is a complex problem that presents immense engineering challenges. The present disclosure addresses these challenges and provides related advantages as well. 
     SUMMARY 
     The present disclosure describes systems and methods supplying hydrogen to a hydrocatalytic biomass conversion reaction through gasification—also known as incomplete combustion—of a fraction of a product stream of the hydrocatalytic reaction. In one embodiment, the present disclosure also provides for recovery of one or more organic compounds from the fraction. In a preferred embodiment, the fraction comprises lignin, lignin-derived compounds, and/or unextracted amounts of cellulose and hemi-cellulose. In another embodiment, the product stream fraction subject to gasification can further comprises a C 14  or greater hydrocarbon, such as an olefin, a paraffin, an aromatic, a cycloalkane, caramels, and/or other oxygenate condensation products. In one embodiment, the one or more organic compounds comprise organic intermediates that are volatile organic compounds, such as oxygenated intermediate, including one or more polyols, alcohols, ketones, mono-oxygenates, diols, and/or any other hydrocarbon having at least one oxygen atom. 
     According to one aspect, the present disclosure provides a method comprising (a) providing a biomass feedstock containing cellulose and water; (b) contacting the biomass feedstock with hydrogen in the presence of a catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture; (c) separating the hydrocatalytically treated mixture into at least a first bottom fraction and a first overhead fraction, wherein the first bottom fraction comprises (i) at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, and (ii) one or more volatile organic compounds; (d) vaporizing at least one volatile organic compound from the first bottom fraction in a first flasher; (e) depositing the at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure on a surface of the first flasher; (f) placing the first flasher in standby mode; (g) vaporizing at least one volatile organic compound from the first bottom fraction in a second flasher; (h) partially oxidizing the deposited at least one compound in the first flasher to generate a gas mixture comprising hydrogen and carbon monoxide; (i) subjecting at least a portion of the gas mixture to a water gas shift reaction to generate hydrogen and carbon dioxide; and (j) providing at least a portion of the hydrogen from step (i) for use in step (b). In one embodiment, the first bottom fraction comprises at least one of lignin, a lignin-derived compound, unextracted cellulose, unextracted hemicellulose, a caramelan, and any combination thereof. 
     In one embodiment, the first bottom fraction comprises at least one compound having a separation point having a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr, such as about 10 Torr. In another embodiment, the first bottom fraction comprises at least one compound having a separation point with a temperature in a range of about 200 to 450 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr, such as about 10 Torr. 
     In one embodiment, the hydrocatalytically treated mixture comprises a plurality of hydrocarbon and oxygenated hydrocarbon molecules, said method further comprising processing at least a portion of the plurality of hydrocarbon and oxygenated hydrocarbon molecules to form a fuel blend comprising a higher hydrocarbon. In another embodiment, at least a portion of the first overhead fraction is subject to a further processing reaction to produce a product stream comprising a higher molecular compound. 
     In one embodiment, the method further comprises separating at least a portion of the product stream comprising a higher molecular compound into a second overhead fraction and a second bottom fraction, wherein the second bottom fraction comprises at least one compound having a separation point having a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 0.10 to 7 bar; partially oxidizing at least a portion of the second bottom fraction to produce a gas mixture comprising carbon monoxide and hydrogen; subjecting at least a portion of the gas mixture generated from partial oxidation of at least a portion of the second bottom fraction to a water gas shift reaction to generate hydrogen and carbon dioxide; and providing at least a portion of the hydrogen from the second bottom fraction to step (b). 
     In one embodiment, the second bottom fraction comprises at least one compound having a separation point having a temperature in a range of about 150 to 400 degrees C. and a pressure in a range of about 0.10 to 7 bar. In another embodiment, the second bottom fraction comprises at least one compound having a separation point having a temperature in a range of about 200 to 400 degrees C. and a pressure in a range of about 0.10 to 7 bar. 
     In one embodiment, the portion of the first bottom fraction subject to partial oxidation has a viscosity of about 1 to 10,000 centipoise (cP) at a temperature of about 75 degrees C. In another embodiment, the portion of the first bottom fraction subject to partial oxidation has a viscosity of about 100 to 5,000 centipoise (cP) at a temperature of about 75 degrees C. In yet another embodiment, the portion of the first bottom fraction subject to partial oxidation has a viscosity of about 500 to 1,000 centipoise (cP) at a temperature of about 75 degrees C. 
     In one embodiment, the hydrocatalytic treatment occurs in liquid phase. In another embodiment, the hydrocatalytic treatment occurs in an aqueous phase solvent. In another embodiment, the hydrocatalytic treatment occurs in an organic phase solvent. In one embodiment, the vaporizing step comprises applying a temperature in a range of 100 to 600 degrees C. and a pressure in a range of 0.01 to 250 psi to the first bottom fraction. 
     According to another aspect, the present disclosure provides a biomass conversion system comprising: a hydrocatalytic treatment system configured to allow contact of a biomass feedstock with hydrogen in the presence of a catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture; a first separation zone coupled to an output of the hydrocatalytic treatment system, said first separation zone configured to separate at least a portion of the hydrocatalytically treated mixture into at least a first bottom fraction and a first overhead fraction, wherein the first bottom fraction comprises (i) at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, wherein the at least one compound is selected from the group consisting of lignin, a lignin-derived compound, unextracted cellulose, unextracted hemicellulose, a caramelan, and any combination thereof, and (ii) one or more volatile organic compounds; a recovery and gasification system coupled to an output of the first separation zone, the recovery and gasification system configured to partially oxidize at least a portion of the first bottom fraction to produce a gas mixture comprising carbon monoxide and hydrogen, wherein the recovery and gasification system comprises: a first flasher coupled to the separation zone to receive at least a portion of the first bottom fraction; a second flasher coupled to the separation zone to receive at least a portion of the first bottom fraction; wherein the recovery and gasification unit is configured to operate one of the first and second flashers to vaporize at least one volatile organic compound in the first bottom fraction while the other flasher is in standby mode; and a water-gas shift reaction zone coupled to an outlet of the recovery and gasification system, the water-gas shift reaction zone is configured to convert at least a portion of the gas mixture into hydrogen and carbon dioxide, wherein an outlet of the water-gas shift reaction zone is coupled to the hydrocatalytic treatment system. 
     Other advantages and features of embodiments of the present invention will become apparent from the following detailed description. It should be understood, however, that the detailed description and the specific examples, while indicating preferred embodiments of the invention, are given by way of illustration only, since various changes and modifications within the spirit and scope of the invention will become apparent to those skilled in the art from this 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       The following figures are included to illustrate certain aspects of the present disclosure, and should not be viewed as exclusive embodiments. The subject matter disclosed is capable of considerable modifications, alterations, combinations, and equivalents in form and function, as will occur to one having ordinary skill in the art and the benefit of this disclosure. 
         FIG. 1  shows an illustrative schematic of one embodiment to supply hydrogen to a hydrocatalytic reaction and recover one or more volatile organic compounds through gasification of a fraction of a product stream of the hydrocatalytic reaction according to aspects of the invention. 
         FIG. 2  shows an illustrative schematic of another embodiment to supply hydrogen to a hydrocatalytic reaction and recover one or more volatile organic compounds through gasification of a fraction of a product stream of the hydrocatalytic reaction according to aspects of the invention. 
         FIGS. 3A and 3B  are schematics a first exemplary embodiment of a recovery and gasification unit according to aspects of the invention. 
         FIGS. 4A and 4B  are schematics a second exemplary embodiment of a recovery and gasification unit according to aspects of the invention. 
         FIGS. 5A and 5B  are schematics a first exemplary embodiment of a recovery and gasification unit according to aspects of the invention. 
     
    
    
     DETAILED DESCRIPTION 
     Embodiments of the present invention relate to systems and methods supplying hydrogen to the hydrocatalytic reaction through gasification of a fraction of the product stream of the hydrocatalytic reaction, preferably a bottom fraction. Various embodiments of the present invention also allow for recovery of one or more volatile organic compounds in such a fraction. In a preferred embodiment, the bottom fraction comprises at least one of lignin, a lignin-derived compound, unextracted cellulose, unextracted hemicellulose, a caramelan, and any combination thereof. Non-limiting exemplary lignin-derived compounds can include partially depolymerized lignin moieties containing 5-′5, phenylcoumaran, and β-O-4 linkages as characterized by monomeric compounds, phenol, o-cresol, p-cresol, anisole, 4-methylanisole, catechol, guaiacol, 4-methylguaiacol, 1,3-dimethoxybenzene, syringol, and vanillin. Other derived compounds include methanol, methoxyphenol, methyl phenol, dimethyl phenol, ethyl phenol, methyl ethyl phenol, methoxypropylphenol, benzene diol, propyl phenol, and similar compounds. The bottom fraction being gasified can further comprise oligomeric derivatives of carbohydrates, and intermediates, including phenolic intermediates derived from lignin, unreacted or partially hydrolyzed cellulose and hemicellulose, cellulose condensation products, caramelans, and cross polymerization products of sugars and phenolic intermediates. In another embodiment, a second bottom fraction is subject to gasification, where the second bottom fraction comprises a C 14  or greater hydrocarbon, including an olefin, a paraffin, an aromatic, or a cycloalkane. A particular hydrocatalytic reaction comprises contacting a biomass feedstock with hydrogen in the presence of a metal catalyst capable of activating molecular hydrogen to form a hydrocatalytically treated mixture. In certain embodiments, the hydrocatalytically treated mixture comprises a plurality of hydrocarbon, including oxygenated hydrocarbon molecules, which can be suitable for use in transportation fuels and industrial chemicals. As mentioned, in a preferred embodiment, the fraction of the hydrocatalytically treated mixture that is subject to gasification comprises at least one of heavy end components, including caramelans, lignin and lignin-derived compounds, and cross polymerization products of sugars and lignin components. In one embodiment, the bottom fraction of the hydrocatalytically treated mixture has a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure about atmospheric pressure, more preferably a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr; most preferably a temperature in a range of about 200 to 450 degrees C. and a pressure of about 1 to 100 Torr, preferably about 3 to 20 Torr. As used herein, a “separation point” refers to a temperature and pressure at or above which a component does not become a vapor or gas. For example, components in a bottom fraction of the hydrocatalytically treated mixture having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure means those components do not become a vapor or gas, e.g., vaporize, at or above about 100 to 600 degrees C. and a pressure of about atmospheric pressure. In another preferred embodiment, the portion being gasified further comprises a second bottom portion comprising C 14  or greater hydrocarbons having a separation point having a temperature in a range of about 100 to 500 degrees C., more preferably a temperature in a range of about 150 to 400 degrees C., and most preferably a temperature in a range of about 200 to 400 degrees C., and a pressure in a range of about 0.10 to 7 bar. It is understood that components or compounds in a bottom fraction of the hydrocatalytically treated mixture may degrade or convert into different compounds at a separation point. An advantage of embodiments of the invention may include reducing the carbon footprint of the fuels formed from the thermocatalytic reaction because at least a portion of the hydrogen used in the thermocatalytic reaction has low carbon footprint. A fuel with low carbon footprint can qualify for certain governmental status that provides certain benefits. While particular embodiments provide certain advantages or benefits, they are not required as part of the invention. 
     As used herein, the term “hydrocarbons” refers to compounds containing both carbon and hydrogen without reference to other elements that may be present. Thus, heteroatom-substituted compounds are also described herein by the term “hydrocarbons.” The term “hydrocatalytic treatment” refers to a type of thermocatalytic reaction where the reaction is with hydrogen in the presence of a catalyst capable of activating molecular hydrogen, preferably a metal catalyst. 
     Various exemplary embodiments of the invention are further described with reference to the drawings. When like elements are used in one or more figures, identical reference characters will be used in each figure, and a detailed description of the element will be provided only at its first occurrence. Some features of the embodiments may be omitted in certain depicted configurations in the interest of clarity. Moreover, certain features such as, but not limited to, pumps, valves, gas bleeds, gas inlets, fluid inlets, fluid outlets and the like have not necessarily been depicted in the figures, but their presence and function will be understood by one having ordinary skill in the art. 
     Referring to  FIG. 1 , biomass feedstock  11  is provided to hydrocatalytic treatment system  12  where biomass feedstock  11  is reacted with hydrogen in the presence of a metal catalyst capable of activating molecular hydrogen to produce hydrocatalytically treated mixture  13 . Hydrocatalytic treatment system  12  is coupled to separation zone  14  to provide hydrocatalytically treated mixture  13  to separation zone  14 . In a preferred embodiment, hydrocatalytic treatment system  12  is in fluid communication with separation zone  14 . As shown, at least a portion of hydrocatalytically treated mixture  13  is separated or fractionated in separation zone  14  into at least two fractions: overhead fraction  15  and bottom fraction  16 . In a preferred embodiment, overhead fraction  15  comprises compounds having a vaporization point that is lower than that of bottom fraction  16 , and bottom fraction  16  comprises compounds having a separation point having a temperature in a range of about 100 to 600 degrees C. and pressure of about atmospheric pressure, more preferably a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr; most preferably a temperature in a range of about 200 to 450 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr, such as about 10 Torr. That is, overhead fraction  15  comprises compounds that would vaporize at a temperature in a range about 100 to 600 degrees C. and pressure of about atmospheric pressure, more preferably a temperature in a range of about 100 to 500 degrees C. and about 1 to 100 Torr, preferably about 3 to 20 Torr; most preferably a temperature in a range of about 200 to 450 degrees C. and about 1 to 100 Torr, preferably about 3 to 20 Torr. Compounds in overhead fraction  15  can be referred to as light components while compounds in bottom fraction  16  can be referred to as heavy components. 
     Referring to  FIG. 1 , at least a portion of bottom fraction  16  is provided to recovery and gasification system  100  for partial oxidation or incomplete combustion. 
     In one embodiment, oxidant stream  18  provides recovery and gasification system  100  with an oxidant suitable to gasify a carbonaceous material. As used herein, the term “oxidant” includes any oxygen containing compound capable of contributing to the gasification of at least a portion of a carbonaceous material, such as bottom fraction  16 . Illustrative oxidants can include, but are not limited to, air, oxygen, essentially oxygen, oxygen-enriched air, mixtures of oxygen and air, mixtures of air and/or oxygen with steam, mixtures of oxygen and one or more inert gases, for example, nitrogen and/or argon, or any combination thereof. Oxidant stream  18  can contain about 20 vol % oxygen or more, about 30 vol % oxygen or more, about 40 vol % oxygen or more, about 50 vol % oxygen or more, about 60 vol % oxygen or more, about 65 vol % oxygen or more, about 70 vol % oxygen or more, about 75 vol % oxygen or more, about 80 vol % oxygen or more, about 85 vol % oxygen or more, about 90 vol % oxygen or more, about 95 vol % oxygen or more, or about 99 vol % oxygen or more. As used herein, the term “essentially oxygen” refers to an oxygen stream containing more than 50 vol % oxygen. As used herein, the term “oxygen-enriched air” refers to a gas mixture containing oxygen in a range of about 21 to 50 vol % oxygen. In one embodiment, oxygen enriched air or essentially oxygen can be supplied by one or more air separation units (“ASU”) or a pressure swing absorber. The ASU can provide a nitrogen-lean and oxygen-rich stream for oxidant stream  18 , thereby minimizing the nitrogen concentration in the system. The ASU can be a high-pressure, cryogenic type separator that can be supplemented with air. In one embodiment, up to about 50 vol %, or up to about 40 vol %, or up to about 30 vol %, or up to about 20 vol %, or up to about 10 vol % of the total oxidant fed to the gasifier can be supplied by the ASU. In a preferred embodiment, a moderator gas (not shown) can be supplied to recovery and gasification system  100 , separately or with oxidant stream  18 , to control the temperature of recovery and gasification system  100 . Non-limiting examples of suitable moderator gases include steam, carbon dioxide, or a combination thereof. Conditions for applying oxidant stream  18  and the moderator gas, if used, are known to those skilled in the art. 
     In another embodiment, oxidant stream  18  can also include steam and/or natural gas, which can be delivered to recovery and gasification system  100  separately or with the oxidant in stream  18 . The partial oxidation of bottom fraction  16  produces gas mixture  19  comprising hydrogen and carbon monoxide. Recovery and gasification system  100  also generates overhead product  118  that can be further processed in similar manners as overhead fraction  15 . Referring to  FIG. 2 , in one embodiment, overhead product  118  can be fed directly into further processing zone  22  separately and/or combined with overhead fraction  15  for further processing in zone  22 . In one embodiment, overhead product  118  comprises one or more volatile organic compounds in bottom fraction  16  that have been vaporized by recovery and gasification system  100 . In a preferred embodiment, overhead product  118  comprises an organic intermediate, such as an oxygenated intermediate, including one or more polyols, alcohols, ketones, mono-oxygenates, diols, and/or any other hydrocarbon having at least one oxygen atom. In another embodiment, overhead product  118  is produced using at least heat generated by gasification of bottom fraction  16 . 
     Gas mixture  19  can be referred to as synthesis gas or syngas. As shown, recovery and gasification system  100  is coupled to water-gas shift reaction zone, WGS zone  20 , to provide gas mixture  19  to WGS zone  20 . As can be seen, WGS zone  20  is external to hydrocatalytic treatment system  12 . In one embodiment, recovery and gasification system  100  is preferably in fluid communication with WGS zone  20 . At least a portion of gas mixture  19  is subject to a water gas shift reaction in WGS zone  20 , which converts the carbon monoxide from gas mixture  19  to hydrogen rich shifted synthesis gas product comprising hydrogen and carbon dioxide, which is shown as stream  21 . WGS zone  20  is coupled to hydrocatalytic treatment system  12  to provide stream  21  to hydrocatalytic treatment system  12 . In one embodiment, WGS zone  20  is preferably in fluid communication with hydrocatalytic treatment system  12 . As shown, at least a portion of the hydrogen rich synthesis gas product generated in WGS zone  20  is routed to hydrocatalytic treatment system  12  via stream  21  for use in a hydrocatalytic reaction. 
     In a preferred embodiment, the hydrogen contained in stream  21  is provided to hydrocatalytic treatment system  12  at a pressure in a range of about 10-200 bar, more preferably about 20 to 100 bar, most preferably 30 to 80 bar, and a temperature in a range of 35-450 degrees C., more preferably about 50 to 250 degrees C., and most preferably about 100 to 200 degrees C. In some embodiments, steam generated in gasification and recovery system  100  can be routed to other processes for use in any suitable manner known to those skilled in the art, such as a heating medium. In another embodiment, recovery and gasification system  100  is coupled to hydrocatalytic treatment system  12  to provide hydrocatalytic treatment system  12  with steam generated in recovery and gasification system  100  via stream  27 . In a preferred embodiment, the steam contained in stream  27  is provided to hydrocatalytic treatment system  12  at a pressure in a range of about 20-120 bar, more preferably about 40 to 100 bar, most preferably 40 to 90 bar. The steam can be saturated or with superheat. In one embodiment, steam from another source can be provided to hydrocatalytic treatment system  12 . In such an embodiment, stream  27  can be combined with steam from the boiler and the mixture of both can be provided as one stream or steam from the boiler and steam from recovery and gasification system  100  can be provided separately. In addition or alternatively, steam from recovery and gasification system  100  can be routed to WGS zone  20  via stream  27  as shown in  FIGS. 1 and 2  to facilitate additional hydrogen generation. 
       FIG. 2  comprises similar processes and systems and  FIG. 1 , and further includes separation zone  14  coupled to processing zone  22  to provide processing zone  22  with overhead fraction  15 . In one embodiment, separation zone  14  is preferably in fluid communication with processing zone  22 . In another embodiment, at least a portion of overhead fraction  15  is subject to one or more reactions in processing zone  22  to produce product stream  23  comprising higher molecular weight compounds. Processing zone  22  is coupled to separation zone  24 . In one embodiment, processing zone  22  is preferably in fluid communication with separation zone  24 . In another embodiment, product stream  23  is further separated or fractionated into at least two fractions in separation zone  24 : overhead fraction  25  and bottom fraction  26 . In a preferred embodiment, a first fraction exiting separation zone  24  is overhead fraction  25  comprising compounds having a vaporization point that is below the vaporization point of bottom fraction  26 . A second fraction exiting separation zone  24  is preferably bottom fraction  26  comprising compounds having a separation point having a temperature in a range of about 100 to 500 degrees C., more preferably a temperature in a range of about 150 to 400 degrees C., and most preferably a temperature in a range of about 200 to 400 degrees C., and a pressure in a range of about 0.10 to 7 bar. That is, overhead fraction  25  comprises compounds that would vaporize at a temperature in a range about 100 to 500 degrees C., more preferably a temperature in a range of about 150 to 400 degrees C., and most preferably a temperature in a range of about 200 to 400 degrees C., and a pressure in a range of about 0.10 to 7 bar. In one embodiment, bottom fraction  26  comprises a C 14  or greater hydrocarbon, such as an olefin, a paraffin, an aromatic, a cycloalkane, caramels, and/or other oxygenate condensation products. Separation zone  24  is coupled to recovery and gasification system  100 . In one embodiment, separation zone  24  is preferably in fluid communication with recovery and gasification system  100 . In addition to or alternatively to bottom fraction  16 , in one embodiment, at least a fraction of bottom fraction  26  is provided to recovery and gasification system  100  also for partial oxidation, generating syngas in gas mixture  19  that can be converted to hydrogen in WGS zone  20  for further use in a hydrocatalytic reaction in hydrocatalytic treatment system  12 . As shown, overhead product  118  generated by recovery and gasification system  100  can be combined with overhead fraction  15  for processing in further processing zone  22 . In addition to or alternatively, overhead product  118  can be routed directly to further processing zone  22  without being combined with overhead fraction  15 . 
     Referring to  FIGS. 1-2 , in practice of one embodiment, biomass feedstock  11  is introduced to hydrocatalytic treatment system  12  along with a predetermined amount of hydrogen or hydrogen containing gas, preferably from stream  21 . Additional hydrogen from an external source can also be provided to hydrocatalytic treatment system  12  as needed, for example, during start up when recovery and gasification system  100  may not yet generate a sufficient amount of hydrogen. In such circumstance, in one embodiment, natural gas can also be provided to recovery and gasification system  100 . Biomass feedstock  11  reacts with hydrogen in the presence of a metal catalyst capable of activating molecular hydrogen to form hydrocatalytically treated mixture  13 , at least a portion of which is discharged and passed to separation zone  14  where mixture  13  is separated into overhead fraction  15  and bottom fraction  16  comprising lignin and lignin-derived compounds. Bottom fraction  16  is discharged and provided to recovery and gasification system  100  where it is partially oxidized with oxidant provided by stream  18  to generate gas mixture  19  comprising hydrogen and carbon monoxide, or synthesis gas. Gas mixture  19  is discharged and introduced to WGS zone  20  to generate stream  21  comprising a hydrogen rich shifted synthesis gas product. Stream  21  is discharged and routed to hydrocatalytic treatment system  12  for use in a hydrocatalytic reaction. In an alternative embodiment (not shown), a portion of overhead fraction  15  can also be routed to recovery and gasification system  100 . Recovery and gasification system  100  also generates overhead product  118 . In one embodiment, overhead product  118  comprises organic intermediates, such as oxygenated intermediate, including one or more polyols, alcohols, ketones, mono-oxygenates, diols, and/or any other hydrocarbon having at least one oxygen atom. Overhead product  118  can be combined with overhead fraction  15  for further processing as described herein. 
     Referring to  FIG. 2 , in another embodiment, at least a portion of overhead fraction  15  is discharged and passed to processing zone  22  to produce product stream  23  comprising higher molecular weight compounds. Product stream  23  is discharged and passed to separation zone  24  to separate product stream  23  into overhead fraction  25  and bottom fraction  26 , which can be discharged and routed to recovery and gasification system  100  for partial oxidation to additionally generate gas mixture  19 . 
     Any suitable type of biomass can be used as biomass feedstock  11 . Suitable cellulosic biomass sources may include, for example, forestry residues, agricultural residues, herbaceous material, municipal solid wastes, waste and recycled paper, pulp and paper mill residues, and any combination thereof. Thus, in some embodiments, a suitable cellulosic biomass may include, for example, corn stover, straw, bagasse, miscanthus,  sorghum  residue, switch grass, bamboo, water hyacinth, hardwood, hardwood chips, hardwood pulp, softwood, softwood chips, softwood pulp, duckweed, and any combination thereof. Leaves, roots, seeds, stalks, husks, and the like may be used as a source of the cellulosic biomass. Common sources of cellulosic biomass may include, for example, agricultural wastes (e.g., corn stalks, straw, seed hulls, sugarcane leavings, nut shells, and the like), wood materials (e.g., wood or bark, sawdust, timber slash, mill scrap, and the like), municipal waste (e.g., waste paper, yard clippings or debris, and the like), and energy crops (e.g., poplars, willows, switch grass, alfalfa, prairie bluestream, corn, soybeans, and the like). The cellulosic biomass may be chosen based upon considerations such as, for example, cellulose and/or hemicellulose content, lignin content, growing time/season, growing location/transportation cost, growing costs, harvesting costs, and the like. 
     Biomass feedstock  11  may be natively present in any sizes, shapes, or forms, or it may be further processed prior to entering hydrocatalytic treatment in system  12 . Examples of further processing include washing (such as, with water, an acid, a base, combinations thereof, and the like), torrefaction, liquefaction, such as pyrolysis, or reduction in size. In some embodiments, the reduction in size may include chipping, chopping, grounding, shredding, pulverizing, and the like to produce a desired size. Thus, in some embodiments, providing a biomass material can comprise harvesting a lignocelluloses-containing plant such as, for example, a hardwood or softwood tree. The tree can be subjected to debarking, chipping to wood chips of desirable thickness, and washing to remove any residual soil, dirt and the like. 
     Biomass feedstock  11  is preferably treated to convert the cellulose and other complex carbohydrates into a more usable form, which can be further transformed into compounds with one or more alcohol functional groups through downstream reactions. While suitable for further transformation, soluble carbohydrates can be very reactive and can rapidly degrade to produce caramelans and other degradation products, especially under higher temperature conditions, such as above about 150° C. One way to protect soluble carbohydrates from thermal degradation is to subject them to one or more catalytic reduction reactions, which may include hydrogenation and/or hydrogenolysis reactions. Depending on the reaction conditions and catalyst used, reaction products formed as a result of conducting one or more catalytic reduction reactions on soluble carbohydrates may comprise, as mentioned, one or more alcohol functional groups, particularly including triols, diols, monohydric alcohols, and any combination thereof, some of which may also include a residual carbonyl functionality (e.g., an aldehyde or a ketone). Such reaction products are typically more thermally stable than soluble carbohydrates and may be readily transformable into fuel blends and other materials through conducting one or more downstream further processing reactions. That is, soluble carbohydrates formed during hydrothermal digestion may be intercepted and converted into more stable compounds before they have an opportunity to significantly degrade, even under thermal conditions that otherwise promote their degradation. 
     In a preferred embodiment, a hydrocatalytic reaction that takes place in system  12  of  FIGS. 1 and 2  is conducted in the presence of hydrogen, specifically molecular hydrogen, with a catalyst that is capable of activating molecular hydrogen to participate in various reactions such as hydrothermal digestion; catalytic reduction reactions, including hydrogenation, hydrogenolysis, and/or hydrodeoxygenation; and optionally hydrodesulfurization and hydrodenitrification. Any suitable hydrocatalytic reaction can take place in system  12 . Exemplary hydrocatalytic reactions, including hydrogenation and hydrogenolysis, are described in U.S. Publication Application No. US2011/0154721, the disclosure of which is incorporated herein by reference in its entirety. 
     For example, in one embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in US2011/0154721, such as a hydrogenolysis reaction and/or a hydrogenation reaction, where soluble carbohydrate is catalytically reacted with hydrogen to produce desired reaction products. Examples of desired or suitable reactions products may include, but are not limited to, alcohols, polyols, aldehydes, ketones, other oxygenated intermediates, and any combination thereof. For instance, hydrocatalytic treatment system  12  can comprise hydrogenation reaction 104 and/or hydrogenolysis reaction 106 of FIGS. 1-3 of US2011/0154721. The descriptions corresponding to hydrogenation reaction 104 and hydrogenolysis reaction 106 are provided by US2011/0154721, which is incorporated by reference in its entirety, and thus need not be repeated. 
     In such an embodiment, at least a portion of the products exiting hydrogenation reaction 104 and/or hydrogenolysis reaction 106 FIGS. 1-3 of US2011/0154721 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated from the products stream as described herein. For instance, in one embodiment, separation zone  14  can comprise separation unit 108 in FIG. 3 of US2011/0154721, which can provide a fraction having separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, more preferably a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr; most preferably a temperature in a range of about 200 to 450 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr. The fraction can be routed to recovery and gasification system  100  of  FIGS. 1-2  for partial oxidation to generate gas mixture  19 . Additional details of separation zone  14  and recovery and gasification system  100  are provided below. 
     In another embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure further comprises a digestion process to convert cellulose and other complex carbohydrates contained in biomass feedstock  11  into a soluble carbohydrate. As used herein, the term “soluble carbohydrates” refers to monosaccharides or polysaccharides that become solubilized in a digestion process. Any suitable digestion process that forms a pretreated biomass containing soluble carbohydrates can be used. Examples of suitable digestion processes can be found in U.S. Application Publication Nos. US2012/0152836, and US2012/0156743, the disclosure of each is incorporated herein by reference in its entirety. 
     In one embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in US2012/0152836. For instance, hydrocatalytic treatment system  12  can comprise any combination of hydrogenolysis systems 126, 126A, 126B, and 126C shown in FIGS. 1-5 of US2012/0152836. In another embodiment, hydrocatalytic treatment system  12  can further comprise digestion system 106 shown in FIGS. 1-5 of US2012/0152836. The descriptions corresponding to digestion system 106 and hydrogenolysis systems 126, 126A, 126B, and 126C are provided by US2012/0152836, which is incorporated by reference in its entirety, and thus need not be repeated. In such embodiments, at least a portion of any product stream exiting a hydrogenolysis system, such as stream 122, stream 123, or stream 130, of FIGS. 1-5 of US2012/0152836 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated from the products stream and gasified as described herein. 
     In another embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in US2012/0156743. For instance, hydrocatalytic treatment system  12  can comprise hydrogenolysis system 120 shown in FIGS. 1-2 of US2012/0156743. In another embodiment, hydrocatalytic treatment system  12  can further comprise pretreat system 104, optionally along with digestive system 190, and/or treatment system 110 of FIGS. 1-2 of US2012/0156743. In such embodiments, at least a portion of oxygenated intermediate stream 122 of FIGS. 1-2 of US2012/0156743 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated from the products stream and gasified as described herein. 
     It is understood that the hydrocatalytic treatment that takes place in hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can employ aqueous phase and/or organic phase solvents. For example, US2011/0154721, US2012/0152836, and US2012/0156743 provide examples of hydrocatalytic treatment that occurs in aqueous phase. Exemplary descriptions of a hydrocatalytic treatment that takes place in an organic phase can be found in U.S. Application Publication No. US2013/0109896, the disclosure of which is hereby incorporated by reference in its entirety. 
     In one embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in US2013/0109896. For example, hydrocatalytic treatment system  12  can comprise organic phase hydrocatalytic treatment system 20 shown in FIG. 1 of US2013/0109896. In another embodiment, hydrocatalytic treatment system  12  can further comprise digestive system 10 shown in FIG. 1 of US2013/0109896. The descriptions corresponding to digestive system 10 and organic phase hydrocatalytic treatment system 20 are provided by US2013/0109896, which is incorporated by reference in its entirety, and thus need not be repeated. In such embodiments, at least a portion of organic hydrocarbon-rich phase stream 32 shown in FIG. 1 of US2013/0109896 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated from the organic hydrocarbon-rich phase stream  32  and gasified as described. In one embodiment, the liquid-liquid separation 30 in FIG. 1 of US2013/0109896 can be part of separation zone  14 . That is, separation zone  14  can comprise the liquid-liquid separation 30 in FIG. 1 of US2013/0109896. For example, in one embodiment, separation zone  14  comprises a liquid-liquid separation step, such as that described in US2013/0109896, which provides bottom fraction  16  that can be routed to recovery and gasification system  100 . In addition to or as an alternative, in one embodiment, the liquid-liquid separation step provides an organic hydrocarbon-rich phase that is further separated in separation zone  14  to provide bottom fraction  16 . 
     In yet another embodiment, if a digestion process is employed, the digestion process preferably comprises hydrothermal digestion, particularly as described in U.S. Application Publication Nos. 61/665,641, filed on Jun. 28, 2012, 61/720,757, filed on Oct. 31, 2012, and 61/817,996, filed on May 1, 2013, the disclosures of which are hereby incorporated by reference in their entirety. Hydrothermal digestion of biomass feedstock  11  is preferably conducted in the presence of molecular hydrogen and a slurry catalyst capable of activating the molecular hydrogen. In such particular embodiments, the hydrothermal digestion of cellulosic biomass and the catalytic reduction of soluble carbohydrates produced therefrom preferably take place in the same vessel, which can be referred to as “in situ catalytic reduction reaction processes.” As used herein, the term “slurry catalyst” will refer to a catalyst comprising fluidly mobile catalyst particles that can be at least partially suspended in a fluid phase via gas flow, liquid flow, mechanical agitation, or any combination thereof. 
     In one embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in U.S. Application No. 61/665,641. For example, hydrocatalytic treatment system  12  can comprise at least one of hydrothermal digestion unit 2 and catalytic reduction reactor unit 4 shown in FIG. 1 of U.S. Application No. 61/665,641. In another embodiment, hydrocatalytic treatment system  12  can further comprise solids separation mechanism 24 also shown in FIG. 1 of U.S. Application No. 61/665,641. Solids separation mechanism 24 can comprise any suitable mechanism that can remove at least a solid contained in a product stream exiting catalytic reduction reactor unit 4, such as reaction product takeoff line 18 shown in FIG. 1 of U.S. Application No. 61/665,641. Non-limiting examples of suitable solids separation mechanisms may include, for example, any number and combination of filters, hydroclones, centrifuges, membranes, and settling tanks. The descriptions corresponding to hydrothermal digestion unit 2, catalytic reduction reactor unit 4, and solids separation mechanism 24 are provided by U.S. Application No. 61/665,641, which is incorporated by reference in its entirety, and thus need not be repeated. In such embodiments, at least a portion of reaction product takeoff line 18 shown in FIG. 1 of U.S. Application No. 61/665,641, whether having passed through solids separation mechanism 24, can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated and gasified as described. In one embodiment, phase separation mechanism 26 in FIG. 1 of U.S. Application No. 61/665,641 can be part of separation zone  14 . That is, separation zone  14  can comprise phase separation mechanism 26 in FIG. 1 of U.S. Application No. 61/665,641 that provides bottom fraction  16  which can be routed to recovery and gasification system  100 . In addition to or alternatively, in one embodiment, phase separation mechanism 26 in FIG. 1 of U.S. Application No. 61/665,641 provides an organic phase that is further separated in separation zone  14  to provide bottom fraction  16 . 
     In another embodiment, hydrocatalytic treatment system  12  can comprise a reaction as described in U.S. Application No. 61/720,757. For example, hydrocatalytic treatment system  12  can comprise at least one of hydrothermal digestion unit 2 and polishing reactor 16 shown in FIG. 1 of U.S. Application No. 61/720,757. If employed, polishing reactor 16 shown in FIG. 1 of U.S. Application No. 61/720,757 is where one or more catalytic reduction reactions can further take place to protect soluble carbohydrates from thermal degradation as described. The descriptions corresponding to hydrothermal digestion unit 2 and polishing reactor 16 are provided by U.S. Application No. 61/720,757, which is incorporated by reference in its entirety, and thus need not be repeated. In such embodiments, at least a portion of lignin removal line 18 shown in FIG. 1 of U.S. Application No. 61/720,757 can be routed to separation zone  14  shown in  FIGS. 1-2 , so a bottom fraction  16  can be separated and gasified as described. In addition to or alternatively, in embodiments comprising polishing reactor 16 shown in FIG. 1 of U.S. Application No. 61/720,757, at least a portion of the product stream exiting polishing reactor 16 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated and gasified as described. That is, the input to separation zone  14  can include a product from hydrothermal digestion unit 2 and/or polishing reactor 16 of U.S. Application No. 61/720,757. 
     In yet another embodiment, hydrocatalytic treatment system  12  shown in  FIGS. 1 and 2  of the present disclosure can comprise a reaction as described in U.S. Application No. 61/817,996. For example, hydrocatalytic treatment system  12  can comprise at least one of hydrothermal digestion unit 2 and polishing reactor 16 shown in FIGS. 1-12 of U.S. Application No. 61/817,996. If employed, polishing reactor 16 shown in FIGS. 1-12 of U.S. Application No. 61/817,996 is where one or more catalytic reduction reactions can further take place to protect soluble carbohydrates from thermal degradation as described. The descriptions corresponding to hydrothermal digestion unit 2 and polishing reactor 16 are provided by U.S. Application No. 61/817,996, which is incorporated by reference in its entirety, and thus need not be repeated. In such embodiments, at least a portion of lignin removal line 18 shown in FIGS. 1-12 of U.S. Application No. 61/817,996 can be routed to separation zone  14  shown in  FIGS. 1-2 , so a bottom fraction  16  can be separated and gasified as described. In addition to or alternatively, in embodiments comprising polishing reactor 16 shown in FIGS. 1-12 of U.S. Application No. 61/817,996, at least a portion of the product stream exiting polishing reactor 16 can be routed to separation zone  14  shown in  FIGS. 1-2  of the present disclosure, so a bottom fraction  16  can be separated and gasified as described. That is, the input to separation zone  14  can include a product from hydrothermal digestion unit 2 and polishing reactor 16 of U.S. Application No. 61/817,996. In one embodiment, separations unit 32 in FIGS. 1-12 of U.S. Application No. 61/817,996 can be part of separation zone  14 . That is, separation zone  14  can comprise separations unit 32 in FIGS. 1-12 of U.S. Application No. 61/817,996 that provides bottom fraction  16  which can be routed to recovery and gasification system  100 . 
     Referring to  FIGS. 1-2  of the present disclosure, at least a portion of hydrocatalytically treated mixture  13  formed in hydrocatalytic treatment system  12  is routed to separation zone  14  where mixture  13  can be separated into different components that can be further processed accordingly. In a preferred embodiment, at least a portion of hydrocatalytically treated mixture  13  is separated in separation zone  14  into at least two fractions: overhead fraction  15  and bottom fraction  16 . In one embodiment, separation zone  14  can comprise a phase separator, a stripping column, an extractor, a filter, a distillation column, a flasher, or any combination thereof. 
     In a preferred embodiment, separation zone  14  separates hydrocatalytically treated mixture  13  into various components based on the volatility property (separation point) of the compounds in mixture  13  under various temperature and pressure conditions. For example, a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure, more preferably a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr, such as about 10 Torr; most preferably a temperature in a range of about 200 to 450 degrees C. and a pressure in a range of about 1 to 100 Torr, preferably about 3 to 20 Torr, such as about 10 Torr, can be applied to at least a portion of hydrocatalytically treated mixture  13 . Referring to  FIGS. 1-2 , in one embodiment, compounds that vaporize under these conditions become overhead fraction  15 , which can be collected for further processing, and compounds that do not vaporize remain to form bottom fraction  16 . The temperature and pressure can be applied gradually in a continuous or step-wise manner or rapidly as desired or according to operating conditions using suitable techniques known to those skilled in the art, such as those employed in distillation columns. The temperature and pressure can be applied for any suitable duration. Such manners of applying temperature and pressure to separate components based on vaporization properties are known to those skilled in the art. Examples of a suitable time period include about 1-60 minutes. In a preferred embodiment, the components that remain after the separation temperature and pressure have been applied constitute bottom fraction  16  shown in  FIGS. 1-2 . Bottom fraction  16  preferably comprises lignin and/or lignin-derived compounds, such as partially depolymerized lignin moieties containing 5-′5, phenylcoumaran, and β-O-4 linkages as characterized by monomeric compounds phenol, o-cresol, p-cresol, anisole, 4-methylanisole, catechol, guaiacol, 4-methylguaiacol, 1,3-dimethoxybenzene, syringol, and vanillin. Other derived compounds include methanol, methoxyphenol, methyl phenol, dimethyl phenol, ethyl phenol, methyl ethyl phenol, methoxypropylphenol, benzene diol, propyl phenol, and similar compounds. In a preferred embodiment, bottom fraction  16  is a solid at ambient temperature and can flow at higher temperatures, such as greater than 100 degrees C. The viscosity of bottom fraction  16  preferably decreases with increasing temperature. In one embodiment, the viscosity of bottom fraction  16  at a temperature of about 75 degrees C. is preferably about 1 to 10,000 centipoise (cP), more preferably about 100 to 5,000 cP, most preferably about 500 to 1000 cP. As will be understood by those of ordinary skill in the art, the viscosity and therefore the pumpability of bottom fraction  16  from separation zone  14  and/or bottom fraction  26  from separation zone  24  can be affected by various factors, including temperature, pressure, concentration of various compounds in the particular bottom fraction, composition, diluents, if any are used, impurity levels, storage time. If the physical state of bottom fraction  16  and/or bottom fraction  26  is solid to viscous, or a semi-solid liquid, it can be heated to a temperature and/or the pressure suitable to render it sufficiently fluid to be pumped, as desired. 
     Overhead fraction  15  is preferably subject to further processing to produce a higher molecular weight compound. In one embodiment, the further processing takes place in processing zone  22  shown in  FIG. 2 . Non-limiting exemplary further processing methods include (i) reforming reactor 38 shown in FIGS. 1-12 of U.S. Application No. 61/817,996, (ii) reforming reactor 28 shown in FIG. 1 of U.S. Application No. 61/720,757, (iii) processing system 130 shown in FIGS. 1-2 of US2012/0156743, (iv) processing step 136 shown in FIGS. 1-5 of US2012/0152836; and processing reaction 110 shown in FIGS. 1-3 of US2011/0154721. In general, suitable further processing reactions include, but are not limited to, hydrogenolysis reactions, hydrogenation reactions, condensation reactions, isomerization reactions, oligomerization reactions, hydrotreating reactions, alkylation reactions, and any combination thereof. For example, referring to  FIG. 2 , overhead fraction  15  is subject to a condensation reaction in processing zone  22  to produce product stream  23 , which is routed to separation zone  24  where product stream  23  can be fractionated into desired components. 
     The further processing can comprise one or more reactions that may be catalytic or non-catalytic. It is to be understood that any number of reactors may be employed to carry out the further processing, such as that in processing zone  22 . In some embodiments, a first further processing reaction may comprise a condensation reaction. Additional further processing reactions may comprise any combination of further catalytic reduction reactions (e.g., hydrogenation reactions, hydrogenolysis reactions, hydrotreating reactions, and the like), further condensation reactions, isomerization reactions, desulfurization reactions, dehydration reactions, oligomerization reactions, alkylation reactions, and the like. Such reactions may be used to convert the initially produced soluble carbohydrates into a biofuel, including, for example, gasoline hydrocarbons, diesel fuels, jet fuels, and the like. As used herein, the term “gasoline hydrocarbons” refers to substances comprising predominantly C 5 -C 9  hydrocarbons and having a boiling point of about 32 to 204 degrees C. More generally, any fuel blend meeting the requirements of ASTM D2887 may be classified as a gasoline hydrocarbon. Suitable gasoline hydrocarbons may include, for example, straight run gasoline, naphtha, fluidized or thermally catalytically cracked gasoline, VB gasoline, and coker gasoline. As used herein, the term “diesel fuel” refers to substances comprising paraffinic hydrocarbons and having a boiling point in a range of about 187 to 417 degrees C., which is suitable for use in a compression ignition engine. More generally, any fuel blend meeting the requirements of ASTM D975 may also be defined as a diesel fuel. As used herein, the term “jet fuel” refers to substances meeting the requirements of ASTM D1655. In some embodiments, jet fuels may comprise a kerosene-type fuel having substantially C 8 -C 16  hydrocarbons (Jet A and Jet A-1 fuels). In other embodiments, jet fuels may comprise a wide-cut or naphtha-type fuel having substantially C 5 -C 15  hydrocarbons present therein (Jet B fuels). 
     In another embodiment, the products of a further processing reaction can be separated further to produce a second overhead fraction and a second bottom fraction which can be gasified in recovery and gasification system  100 . As shown in  FIG. 2 , at least a portion of overhead fraction  15  is routed to processing zone  22  to form higher molecular weight compounds, which exit processing zone  22  as product stream  23 . In one embodiment, at least a portion of product stream  23  is routed to separation zone  24  for further separation, preferably into at least two fractions: overhead fraction  25  and bottom fraction  26 . In a preferred embodiment, a first fraction exiting separation zone  24  is overhead fraction  25  comprising compounds that vaporize at a separation point of bottom fraction  26 . A second fraction exiting separation zone  24  is preferably bottom fraction  26  comprising compounds having a separation point having a temperature in a range of about 100 to 500 degrees C., more preferably a temperature in a range of about 150 to 400 degrees C., and most preferably a temperature in a range of about 200 to 400 degrees C., and a pressure in a range of about 0.10 to 7 bar. In addition to or alternatively to bottom fraction  16 , in one embodiment, at least a fraction of bottom fraction  26  enters recovery and gasification system  100  to be partially oxidized and routed to hydrocatalytic treatment system  12  as described in this disclosure. Separation zone  24  preferably functions similar to separation  14  where components can be separated based on their vaporization properties. For instance, overhead fraction  25  and bottom fraction  26  can be generated from application of a temperature in a range of about 100 to 500 degrees C. and a pressure in a range of about 0.10 to 7 bar. Compounds that would vaporize at the applied temperature and pressure can form overhead fraction  25 , which can be collected for further processing or other use. Compounds that would not vaporize at the applied temperature and pressure remain to form bottom fraction  26 . Bottom fraction  26  preferably comprises C 14  or greater hydrocarbons, including an olefin, a paraffin, an aromatic, or a cycloalkane. 
     Referring to  FIGS. 1-2 , at least one of a portion of bottom fraction  16  and/or a portion of bottom fraction  26  is routed to recovery and gasification system  100  where it serves as a carbonaceous feed. In recovery and gasification system  100 , bottom fraction  16  is partially oxidized to produce gas mixture  19  which comprises primarily of hydrogen (H 2 ) and carbon monoxide (CO). Bottom fraction  16  can enter recovery and gasification system  100  in any form, such as a dry feed or a wet feed, including a solid, a liquid, or a solid coated with a liquid. The term “liquid” used in context of bottom fraction  16  and/or bottom fraction  26  refers to a carbonaceous feed that is a liquid, an emulsion, or a pumpable slurry at the feed pressure and temperature into recovery and gasification system  100 . 
     Operation of recovery and gasification system  100  also generates overhead product  118  an organic intermediate, such as an oxygenated intermediate, including one or more polyols, alcohols, ketones, mono-oxygenates, diols, and/or any other hydrocarbon having at least one oxygen atom, which can be routed directly to further processing zone  22  separately and/or combined with overhead fraction  15 . In one embodiment, overhead product  118  comprises one or more volatile organic compounds in bottom fraction  16  that have been vaporized by recovery and gasification system  100 . In another embodiment, overhead product  118  is produced using at least heat generated by gasification of bottom fraction  16 . 
     The gasification process is well known in the art and can be employed using solid and liquid carbonaceous sources. The gasification process uses partial oxidation or incomplete combustion to convert carbonaceous materials at high temperature into synthesis gas (“syngas”), which comprises carbon monoxide and hydrogen. This is in contrast to a full combustion or complete oxidation reaction where primarily steam and carbon dioxide are produced by the reaction of a fuel, such as a carbonaceous material, and an oxidant, such as oxygen. A complete oxidation typically take place under conditions that have excess oxygen according to the following equation: 
       C n H m +(n+¼ m)O 2 →½ mH 2 O+nCO 2    Equation (1)
 
     For gasification processes, oxygen is restricted to less than a stoichiometric concentration of oxygen relative to fuel where process generates primarily hydrogen and carbon monoxide through incomplete combustion or partial oxidation of the fuel, as represented by the equation below: 
       C n H m +½ nO 2 →½ mH 2 +nCO   Equation (2)
 
     One or more oxidants and one or more feed, e.g., bottom fraction  16  and/or bottom fraction  26 , can be directed, fed, or otherwise introduced to recovery and gasification system  100 . The one or more oxidants and one or more feed can be introduced to recovery and gasification system  100  continuously, intermittently, interspersingly, simultaneously, separately, sequentially, or a combination thereof. Any number of oxidants can be directed, fed, or otherwise introduced to recovery and gasification system  100 . For example, the number of oxidants introduced to recovery and gasification system  100  can be 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more. It is understood that conditions for partial oxidation or incomplete combustions may be provided at least by limiting the amount of oxygen available in recovery and gasification system  100  to less than what is required for full oxidation or combustion. For example, this can be done by controlling the amount of oxidant stream  18  entering recovery and gasification system  100  and/or by the amount of oxygen in oxidant stream  18  itself. 
     In one embodiment, recovery and gasification system  100  comprises at least two flashers, at least one flasher is in operation mode while at least another flasher is in stand-by mode. The flasher in operation can be used to vaporize volatile organic compounds in the reaction product mixture that can be collected for further processing. During operation, lignin, lignin-derived compounds, and/or and other high molecular weight carbonaceous compounds derived from adverse reactions of carbohydrates, sugars, and lignin-derived species are deposited inside the flasher. As the deposited material accumulates the flasher&#39;s ability to flash volatile organic compounds from the reaction product mixture decreases. When the flasher&#39;s capability falls below a certain level of performance, the less efficient flasher loaded with deposited material can be replaced with the flasher on stand-by so flashing operations can continue. The deposited material can be removed from the flasher by adding a fluid containing oxygen to partially oxidize the deposited material in-situ while generating syngas. This allows for continued flashing of the reaction product mixture without significant delay waiting for removal of the deposited material, which can include lignin and/or lignin-derived compounds. In another embodiment, one or more flashers can further comprise one or more conduits configured to circulate a heat exchange medium to allow for further control of the flashing process where the reaction product can be additionally heated or cooled in the flasher during operation to achieve vaporization of desired volatile organic compounds. 
     In yet another embodiment, the system comprises a flasher coupled to at least two reboilers, at least one in operation and at least one other on stand-by. The heat to operate the flasher is provided by the at least one reboiler in operation or on-line. During operation, lignin and/or lignin-derived compounds are deposited inside the reboiler. As the lignin and/or lignin-derived compounds accumulate, the reboiler&#39;s heat transfer capability decreases. When the reboiler&#39;s capability falls below a certain level of performance, the less efficient reboiler containing buildup of the deposited material can be replaced with the reboiler on stand-by or off-line so flashing operations can continue. The deposited material can be removed from the reboiler through gasification. 
     In one embodiment, at least one flasher can further include one or more packer elements preferably comprising a heat resistant material, such as ceramic, metal, or inorganic oxide material, to increase the surface area onto which lignin, lignin-derived compounds, and/or other high molecular weight carbonaceous compounds can be deposited during the flashing operation. A heat resistant material is preferred to withstand gasification conditions in such embodiments. The one or more packer elements may comprise any suitable material known to those skilled in the art. 
       FIGS. 3A and 3B  illustrate an exemplary embodiment of recovery and gasification system  100 . As shown, recovery and gasification system  100  comprises flasher  102 , flasher  104 , valve  106 , valve  108 , heating component  110 , and steam generating superheater  112 . Flasher  102  and flasher  104  are adapted to receive the flow of bottom fraction  16  therethrough. While only two flashers are shown in  FIGS. 3A and 3B , it is understood that system  100  can comprise more than two flashers. Valve  106  controls flow of bottom fraction  16  into flasher  102  and flasher  104 . Valve  108  controls flow of overhead product  118  out of flasher  102  and flasher  104 . In operation, if flasher  102  is on-line or in use and flasher  104  is off-line or on standby, valve  106  is set to allow bottom fraction  16  to flow into flasher  102  and not flasher  104  and valve  108  is set to allow overhead product  118  to exit flasher  102 . If flasher  104  is on-line and flasher  102  is off-line, valve  106  is set to allow bottom fraction  16  to flow into flasher  104  and not flasher  102  and valve  108  is set to allow overhead product  118  to exit flasher  104 . It is understood that suitable means other than valves known to those skilled in the art can be used to allow flasher  102  and  104  to switch between on-line and off-line modes. Referring to  FIGS. 3A and 3B , prior to entering the respective flasher in operation, bottom fraction  16  is heated by heating component  110 . Heating component  110  can comprise any suitable heating device, such as a furnace or heat exchanger. 
     Referring to  FIG. 3A , flasher  102  is on-line, where valve  106  and valve  108  are set to allow fluid communication between flasher  102  and separation zone  14  and further processing zone  22  so flasher  102  can receive bottom fraction  16  from separation zone  14  and forward overhead product  118  to the next process, such as further processing zone  22 , while flasher  104  is off-line or in standby mode. In standby mode, flasher  104  does not receive bottom fraction  16 . Referring to  FIG. 3B , flasher  104  is on-line where valve  106  and valve  108  are set to allow fluid communication between flasher  104  and separation zone  14  and further processing zone  22  so flasher  104  can receive bottom fraction  16  from separation zone  14  and forward overhead product  118  to further processing zone  22  while flasher  102  is off-line or in standby mode. Referring to  FIGS. 3A and 3B , the flow of bottom fraction  16  into and of overhead product  118  out of the on-line flasher is designated by solid lines while similar lines are dashed for the flasher that is in standby mode. 
     As shown in  FIGS. 3A and 3B , after bottom fraction  16  is heated by heating component  110 , it preferably enters recovery and gasification unit  100  as a fluid, e.g., having fluid-like properties. In one embodiment, bottom fraction  16  comprises (i) at least one compound having a separation point having a temperature in a range of about 100 to 600 degrees C. and a pressure of about atmospheric pressure and (ii) one or more volatile organic compounds. As bottom fraction  16  flows through flasher  102  or  104 , one or more volatile organic compounds are flashed or vaporized while lignin and/or other components not vaporized during operation are deposited on a surface of flasher  102  or  104 . In one embodiment, a surface of flasher  102  or  104  onto which material is deposited can comprise a surface of a packer disposed in the respective flasher. The vaporized organic compounds, represented as overhead product  118 , exit flasher  102  or  104  where it can be collected for further processing, such as that of further processing zone  22 , as desired. In a particular embodiment, overhead product  118  comprises one or more organic intermediates, such as an oxygenated intermediate, including one or more polyols, alcohols, ketones, mono-oxygenates, diols, and/or any other hydrocarbon having at least one oxygen atom. In certain embodiments where bottom fraction  16  comes from digestion of cellulosic material, particularly coming from a digester operating at higher temperatures, bottom fraction  16  also includes caramel, or caramelan, formed from heating sugars in the cellulosic biomass material, which are not vaporized and are deposited on a surface of flasher  102  or  104 . 
     Referring to  FIG. 3A , in operation, at least a portion of bottom fraction  16  exits separation zone  14  and enters flasher  102  of recovery and gasification system  100 . In a preferred embodiment, bottom fraction  16  is heated by heating component  110  prior to entering flasher  102 . One or more volatile organic compounds are flashed into overhead product  118  in flasher  102  and the remaining compounds are deposited on a surface of flasher  102 . At least a portion of overhead product  118  exits flasher  102  and enters further processing zone  22 . Operation of recovery and gasification system  100  continues until the flashing capability of flasher  102  diminishes beyond a certain level, which can be established as desired and/or dictated by operating conditions. Referring to  FIG. 3B , flasher  102  can be taken off-line and flasher  104  can be put on-line where valve  106  and valve  108  are set to allow bottom fraction  16  to enter flasher  104  to produce overhead product  118  so operation of recovery and gasification system  100  may continue with minimal interruptions. The operation of recovery and gasification system  100  can continue with the switching back and forth between flasher  102  and flasher  104 , or any additional flashers as described. 
     Referring to  FIGS. 3A and 3B , the material deposited in the flasher that is in standby mode, e.g., flasher  104  in  FIG. 3A  and flasher  102  in  FIG. 3B , is removed through gasification. As shown, oxidant  18  is supplied to flasher  102  or  104  to support gasification of the deposited material and removes it from the flasher in standby mode. Slag  130  generated during gasification can be discharged from flasher  102  or  104 . In one embodiment, at least some lignin in bottom fraction  16  deposited on a surface of flasher  102  or  104  is gasified. The gasification process generates gas mixture  19  comprising hydrogen and carbon monoxide at high temperature. 
     As shown, at least a portion of gas mixture  19  generated from the gasification of deposited material in flasher  102  or  104  enter WSG zone  20  for further hydrogen generation as described herein. In addition to or alternatively, the thermal energy in gas mixture  19  can be harnessed instead of and/or before entering WSG zone  20 . One exemplary manner of harnessing the thermal energy in gas mixture  19  is to generate steam with the thermal energy using means known to those skilled in the art. For example, as shown, steam can be generated by applying the thermal energy in gas mixture  19  to steam generating superheater  112 , which can comprise one or more conduits (not shown), such as tubes, containing water. When enough heat is transferred to the conduits, the water evaporates and becomes steam, which can be routed to other processes for use in any suitable manner known to those skilled in the art, such as a heating medium. For example, in one embodiment, recovery and gasification unit  100  is coupled to hydrocatalytic treatment system  12  to provide hydrocatalytic treatment system  12  with steam generated in recovery and gasification unit  100  via stream  27  as shown in  FIGS. 1 and 2 . In addition or alternatively, steam from recovery and gasification unit  100  can be routed to WGS zone  20  via stream  27  as shown in  FIGS. 1 and 2  to facilitate additional hydrogen generation. In yet another embodiment (not shown), at least two flashers (e.g.,  102  and  104 ) are heat integrated in operation so that the thermal energy generated from gasification in the off-line flasher can be used in the flashing operation of the on-line flasher. Additional heat from another source may also be provided to the on-line flasher as desired. 
     Referring to  FIGS. 3A and 3B , another way of harnessing the thermal energy in gas mixture  19  is to route it to heating component  110  for use to heat up bottom fraction  16  prior to entering the flasher in operation. Yet another way of harnessing the thermal energy in gas mixture  19  is to generate electricity using the steam generated to turn a turbine (not shown) as known to those skilled in the art. Because a product of gasification in the flasher in standby mode is steam, this steam can be harnessed directly in similar manners described above with respect to steam in stream  27  or in other suitable manners known to those skilled in the art. In one embodiment, after thermal energy in gas mixture  19  has been harnessed by steam generating superheater  112 , gas mixture  19  may also exit steam generating superheater  112  and enter WGS zone  20  for additional hydrogen generation as described herein for processing of gas mixture  19  to generate additional hydrogen. 
       FIGS. 4A and 4B  illustrate another exemplary embodiment of recovery and gasification system  100  where flasher  102  and flasher  104  further comprise conduit  132  configured to circulate a heat exchange medium to further heat or cool bottom fraction  16  to achieve vaporization of desired volatile organic compounds. Conduit  132  can have any suitable configuration known to those skilled in the art.  FIGS. 4A and 4B  illustrate two exemplary embodiments of such configurations. In  FIG. 4A , conduit  132  comprises one or more folds or undulations while in  FIG. 4B , at least a portion of conduit  132  has a spiral shape. The number, size, spacing, and other properties of such shapes can be of any suitable manner and can be adjusted as desired or as needed by operating conditions as known by one of ordinary skill The heat exchange medium can be of any suitable type and in any suitable phase including liquid or gas. The temperature and type preferably depends at least on whether it is desired to heat or cool bottom fraction  16  in the respective flasher. 
     Referring to  FIGS. 4A and 4B , during operation, if it is desired to further heat up bottom fraction  16  in flasher  102  or  104 , a heat exchange medium with temperature higher than the temperature of bottom fraction  16  can be circulated through conduit  132 . When bottom fraction  16  comes in contact with conduit  132 , it is heated up further. If it is desired to cool bottom fraction  16  in flasher  102  or  104 , a heat exchange medium with temperature lower than the temperature of bottom fraction  16  can be circulated through conduit  132 . When bottom fraction  16  comes in contact with conduit  132 , it is cooled down. As such, conduit  132  can be used to further regulate or control the temperature of bottom fraction  16  in flasher  102  or  104  to achieve the desired vaporization conditions. 
       FIGS. 5A and 5B  illustrate yet another embodiment of recovery and gasification system  100 . Referring to  FIGS. 5A and 5B , recovery and gasification system  100  comprises flasher  102  and reboiler  532  and reboiler  534 , valve  536 , and steam generating superheater  112 . While only two reboilers are shown in  FIGS. 4A and 4B , it is understood that system  100  can comprise more than two reboilers. Flasher  102  is coupled to reboiler  532  and reboiler  534  to receive thermal energy  538  generated by the respective reboiler. Valve  536  controls flow of thermal energy  538  generated by reboiler  532  or  534  into flasher  102 . In operation, if reboiler  532  is on-line or in use and reboiler  534  is off-line or on standby, valve  536  is set to allow thermal energy  538  to flow into flasher  102 . If reboiler  534  is on-line and reboiler  532  is off-line, valve  536  is set to allow thermal energy  538  to flow into flasher  102 . It is understood that suitable means other than valves known to those skilled in the art can be used to allow reboiler  532  and  534  to switch between on-line and off-line modes. Referring to  FIGS. 5A and 5B , the flow of thermal energy  538  into the on-line reboiler is designated by solid lines while similar lines are dashed for the flasher that is in standby mode. 
     Referring to  FIG. 5A , during operation where reboiler  532  is on-line, bottom fraction  16  is fed to flasher  102  from separation zone  14 . One or more volatile organic compounds in bottom fraction  16  is flashed into overhead product  118  in flasher by thermal energy  538  generated by reboiler  532 . At least a portion of overhead product  118  exits flasher  102  for further processing as described herein. Residue  540  of remaining components that are not vaporized returns to reboiler  532 . As operation continues, the remaining components are deposited on a surface of reboiler  532 . Operation of recovery and gasification system  100  continues until the heat transfer capability of reboiler  532  diminishes beyond a certain level, which can be established as desired and/or dictated by operating conditions. Referring to  FIG. 5B , reboiler  532  can be taken off-line and flasher  534  can be put on-line where valve  536  is set to allow thermal energy  538  to enter reboiler  534  to produce overhead product  118  so operation of recovery and gasification system  100  may continue with minimal interruptions when a reboiler&#39;s heat transfer capability falls below a certain level. The operation of recovery and gasification system  100  can continue with the switching back and forth between reboiler  532  and reboiler  534 , or any additional reboilers as described. In one embodiment, flasher  102  can further comprise conduit  132  illustrated and described with respect to  FIGS. 4A and 4B . 
     The material deposited in the reboiler in standby mode, e.g., reboiler  534  in  FIG. 5A  and reboiler  532  in  FIG. 5B , is removed through gasification. As shown, oxidant  18  is supplied to reboiler  532  or  534  to support gasification of the deposited material and removes it from the reboiler in standby mode. In one embodiment, at least some lignin in bottom fraction  16  deposited on a surface of reboiler  532  or  534  is gasified. The gasification process generates gas mixture  19  comprising hydrogen and carbon monoxide at high temperature. 
     As shown, at least a portion of gas mixture  19  generated from the gasification of deposited material in reboiler  532  or  534  enter WSG zone  20  for further hydrogen generation as described with respect to  FIGS. 1 and 2 . In addition to or alternatively, the thermal energy in gas mixture  19  can be harnessed instead of and/or before entering WSG zone  20 . Thermal energy  116  generated by the gasification can be harnessed in several ways. One exemplary manner of harnessing thermal energy  116  is to generate steam where thermal energy  116  can be used to generate steam using means known to those skilled in the art. For example, as shown, steam in stream  27  can be generated by applying thermal energy  116  to steam generating superheater  112 , which can comprise one or more conduits (not shown), such as tubes, containing water. When enough heat is transferred to the conduits, the water evaporates and becomes steam designated by numeral  27 , which can be used as a heating medium for other parts of the process, including hydrocatalytic treatment system  12  as shown in  FIGS. 1 and 2 . Another way of harnessing thermal energy  116  is to generate electricity using the generated steam to turn a turbine (not shown) as known to those skilled in the art. Because a product of gasification in the reboiler in standby mode is steam, this steam can be harnessed directly in similar manners described above with respect to steam in stream  27  or in other suitable manners known to those skilled in the art. In one embodiment, after thermal energy in gas mixture  19  has been harnessed by steam generating superheater  112 , gas mixture  19  may also exit steam generating superheater  112  and enter WGS zone  20  for additional hydrogen generation as described herein for processing of gas mixture  19  to generate additional hydrogen. 
     Any suitable flashing techniques known to one of ordinary skill in the art can be used to vaporize organic compounds in bottom fraction  16 . For example, one or more temperatures between about 100 to 600 degrees C. at a pressure of about 0.01 to 250 psi can be applied to bottom fraction  16  in a flasher in operation, such as flasher  102  or  104 , in one or multiple stages. Preferably, one or more temperatures in a range of about 100 to 600 degrees C. at a pressure of about 0.05 to 150 psi can be applied to bottom fraction  16  in one or multiple stages. More preferably, one or more temperatures in a range of about 200 to 450 degrees C. at a pressure of about 0.01 to 250 psi or about 0.05 to 150 psi can be applied to bottom fraction  16  in one or multiple stages. Most preferably, a temperature of at least 300 degrees C. at a pressure of about 0.01 to 250 psi or about 0.05 to 150 psi can be applied to bottom fraction  16  in one or multiple stages. In a preferred embodiment, if a multistage distillation technique is used, the initial stage starts with low temperature and subsequent stages have increasingly higher temperatures until the final or bottoms stage has the highest temperature. 
     In one embodiment, flasher  102  or  104  in standby mode furnace component  104  has gasification conditions sufficient to gasify least a portion of the deposited material, preferably at a temperature and pressure sufficient to gasify at least some lignin in the deposited material. In a particular embodiment, the gasification temperature of flasher  102  or  104  is in a range of 800 to 1700 degrees C., such as about 1000 degrees C. In another embodiment, the gasification temperature is up to about 1700 degrees C. In a preferred embodiment, the gasification temperature of flasher  102  or  104  is in the range of about 1000 to 1700 degrees C. in another embodiment, the gasification temperature of flasher  102  or  104  is in a range of about 1250 to 1600 degrees C. In yet another embodiment, the temperature is in a range of about 750 to 1050. In one embodiment, the gasification pressure of flasher  102  or  104  is in the range of about 15 to 80 bar, preferably 20 to 70 bar, and more preferably 25 to 45 bar. 
     In embodiments where the flashing of organic compounds in bottom fraction  16  is carried out at higher than atmospheric pressure (about 1 atm or about 14.696 psi), the higher pressure can facilitate transport of overhead product  118  to the next processing step, such as the further processing described herein. In a preferred embodiment, if higher than atmospheric pressure is used, the pressure applied is about the same pressure or slightly higher than the pressure of the next reaction stage. For example, in one embodiment, the pressure for overhead product  118  can be the same or slightly higher than the operating pressure of further processing zone  22 . For such embodiments employing distillation at higher than atmospheric pressure, the process can be more energy efficient since the need to condense the VOCs and subsequent vaporization in preparation for the next stage is eliminated or substantially minimized. In one embodiment, a stripping agent such as steam can optionally be used to facilitate flow of overhead product  118  to the next reaction zone. In another embodiment, a pressure of about 15 to 30 psi is used if it is desired to prevent air from entering the heat exchange process. In yet another embodiment, the heat exchange can take place under vacuum, which can prevent formation of heavy ends. 
     Heating component  110  can comprise any system suitable to transfer heat to bottom fraction  16 . Non-limiting examples include suitable heat exchangers such as shell and tube heat exchangers, pipe-in-pipe, exchangers, spiral or coiled tube, plate-type, tube-fin or plate-fin, and compact heat exchangers. Other exemplary suitable heat transfer systems include furnaces with integral heat exchange or an indirect heating fluid such as steam or hot oil. In embodiments employing reboilers, such as reboilers  532  and  534  in  FIGS. 5A-5B , exemplary types of reboilers that can be employed include kettle-type, fired, thermosiphon, forced recirculation, and/or electrically heated reboilers. The reboilers can be operated under any suitable condition known to one of ordinary skill in the art. 
     In one embodiment, one or more sorbents can also be introduced to recovery and gasification system  100 . The sorbents can capture one or more contaminants from the syngas, such as sodium vapor in the gas phase within a gasifier. 
     In one embodiment, gas mixture  19  discharged from recovery and gasification system  100  can be routed to WGS zone  20 . In one embodiment, at least a portion of gas mixture  19  can be further processed before it is introduced to WGS zone  20 . Further processing can be part of recovery and gasification system  100 . For example, in certain embodiments, recovery and gasification system  100  can further comprise one or more particulate removal systems (not shown) and/or one or more cooling zones (not shown). In other embodiments, recovery and gasification system  100  can also include one or more hydrogen separators (not shown). 
     One or more particulate removal systems can be used to partially or completely remove any particulates from the syngas to provide the particulates or particulate-containing fluid and a separated syngas. The particulate removal system can include a separation device for example conventional disengagers and/or cyclones. Particulate control devices (“PCD”) capable of providing an outlet particulate concentration below the detectable limit of about 0.1 parts per million by weight (ppmw) can also be used. Examples of suitable PCDs can include, but are not limited to, sintered metal filters, metal filter candles, and ceramic filter candles (for example, iron alum inide filter material). The particulates, for example, fine ash, coarse ash, and combinations thereof, can be recycled to the gasifier, purged from the system, utilized as the particulates, or any combination thereof. 
     If desired or necessary, the separated syngas can be cooled in one or more syngas coolers in one or more cooling zones. For example, the syngas can be cooled to about 540 degrees C. or less, such as about 300 degrees C., using a suitable heat exchange system known to those skilled in the art. In another embodiment, such cooling may not be needed as gas mixture  19  is cooled by passing through the heat exchange component of recovery and gasification system  100 . 
     In certain embodiments, the separated and/or cooled syngas can be treated within a gas purification system to remove contaminants. The gas purification system can include a system, a process, or a device to remove sulfur and/or sulfur-containing compounds from the syngas. Examples of a suitable catalytic gas purification system include, but are not limited to, systems using zinc titanate, zinc ferrite, tin oxide, zinc oxide, iron oxide, copper oxide, cerium oxide, or mixtures thereof. Examples of a suitable process-based gas purification system include, but are not limited to, the SELEXOL® process, the RECTISOL® process, the CRYSTASULF® process, and the Sulfinol gas treatment process. 
     In one embodiment, one or more amine solvents such as methyl-diethanolamine (MDEA) can be used to remove acid gas from the syngas. Physical solvents, for example SELEXOL® (dimethyl ethers of polyethylene glycol) or RECTISOL® (cold methanol), can also be used. If the syngas contains carbonyl sulfide (COS), the carbonyl sulfide can be converted by hydrolysis to hydrogen sulfide by reaction with water over a catalyst and then absorbed using the methods described above. If the syngas contains mercury, the mercury can be removed using a bed of sulfur-impregnated activated carbon. 
     One or more catalysts, such as a cobalt-molybdenum (“Co—Mo”) catalyst can be incorporated into the gas purification system to perform a sour shift conversion of the syngas. The Co—Mo catalyst can operate at a temperature of about 288° C. in the presence of H 2 S, for example, about 100 parts per million by weight (ppmw) H 2 S. If a Co—Mo catalyst is used to perform a sour shift, subsequent downstream removal of sulfur can be accomplished using any of the above described sulfur removal methods and/or techniques. 
     Recovery and gasification system  100  can also discharge ash or slag material (not shown), such as that described above. The slag material is optionally recycled back to recovery and gasification system  100  to increase the content of solid ash-forming materials. 
     In WGS zone  20 , carbon monoxide is converted to hydrogen in the presence of steam through the water-gas shift reaction represented by CO+H 2 O→CO 2 +H 2 . In one embodiment, steam generated by recovery and gasification system  100  and/or a heat exchanger, if used, can provide at least a portion of the steam for the water-gas shift reaction. The water-gas shift process is well established as a means to increase the hydrogen content and/or reduce the carbon monoxide content of synthesis gases produced by gasification of carbonaceous material. In WGS zone  20 , carbon monoxide reacts with steam at high temperature, and optionally in the presence of one or more catalysts, to yield carbon dioxide and hydrogen. A mixture of hydrogen, carbon dioxide, unreacted carbon monoxide and other impurities is discharged from WGS zone  20  as shifted synthesis gas. At least a portion of the hydrogen generated in WGS zone  20  is provided to hydrocatalytic treatment system  12  via hydrogen stream  21  for use in hydrocatalytic reactions. 
     In a preferred embodiment, WGS zone  20  can comprise one or more shift reactors to adjust the hydrogen to carbon monoxide ratio (H 2 :CO) of the syngas by converting CO to CO 2 . Within a shift reactor, a water-gas shift reaction reacts at least a portion of the carbon monoxide in the syngas with water in the presence of a catalyst and a high temperature to produce hydrogen and carbon dioxide. Examples of a suitable shift reactor can include, but are not limited to, single stage adiabatic fixed bed reactors, multiple-stage adiabatic fixed bed reactors with interstage cooling, steam generation or cold quench reactors, tubular fixed bed reactors with steam generation or cooling, fluidized bed reactors, or any combination thereof. A sorption enhanced water-gas shift (SEWGS) process, utilizing a pressure swing adsorption unit having multiple fixed bed reactors packed with shift catalyst and at high temperature, e.g. a carbon dioxide adsorbent at about 480° C., can be used. Various shift catalysts can be employed. 
     In one embodiment, the shift reactor can include two reactors arranged in series. A first reactor can be operated at high temperature (about 340° C. to about 400° C.) to convert a majority of the CO present in the syngas to CO, at a relatively high reaction rate using an iron-chrome catalyst. A second reactor can be operated at a relatively low temperature (about 145° C. to about 205° C.) to complete the conversion of CO to CO 2 using a mixture of copper oxide and zinc oxide. 
     In one embodiment, at least a portion of gas mixture  19  can be directed to a hydrogen separator (not shown) before it is routed to WGS zone  20 . In another embodiment, which is not shown, at least a portion of gas mixture  19  can bypass WGS zone  20  and can be fed directly to the hydrogen separator. At least a portion of the hydrogen separated by the hydrogen separator can be fed to hydrocatalytic treatment system  12 . 
     The hydrogen separator can include any system or device to selectively separate hydrogen from syngas to provide a purified hydrogen stream and a waste gas stream. The hydrogen separator can provide a carbon dioxide rich fluid and a hydrogen rich fluid. The hydrogen separator can utilize pressure swing absorption, cryogenic distillation, and/or semi-permeable membranes. Examples of suitable absorbents include, but are not limited to, caustic soda, potassium carbonate or other inorganic bases, and/or alanolamines. 
     In one embodiment, the hydrogen generated in WGS zone  20  and/or separately by a hydrogen separator can be routed to processing zone  22  for use in hydrocatalytic reactions including further catalytic reduction reactions (e.g., hydrogenation reactions, hydrogenolysis reactions, hydrotreating reactions, and the like), further condensation reactions, isomerization reactions, oligomerization reactions, and any combination thereof. 
     Accordingly, the hydrogen used in a hydrocatalytic reaction of system  12  can include external hydrogen, recycled hydrogen, in situ generated hydrogen, and any combination thereof. The term “in situ generated hydrogen” as used herein refers to hydrogen that is produced within the overall process; it is not limited to a particular reactor for production or use and is therefore synonymous with an in process generated hydrogen. As explained, at least one source of the hydrogen used in hydrocatalytic treatment system  12  comes from gasification of bottom fraction  16  and/or bottom fraction  26 , which is a product of hydrocatalytic treatment system  12 . 
     Descriptions of exemplary suitable hydrocatalytic reactions that can take place in hydrocatalytic treatment system  12  are known to those skilled in the art and/or provided by U.S. Application Publication Nos. US2011/0154721, US2012/0152836, US2012/0156743, and US2013/0109896, and U.S. Application Nos. 61/665,641, filed on Jun. 28, 2012, and 61/720,757, filed on Oct. 31, 2012, and 61/817,996, where each disclosure is incorporated herein by reference. Likewise, descriptions of exemplary suitable further processing reactions that can take place in processing zone  22  are known to those skilled in the art and/or provided by the materials that have been incorporated by reference in their entirety. Accordingly, the details of hydrocatalytic reactions and further processing reactions need not be repeated. 
     Nevertheless, the descriptions below highlight some aspects of certain hydrocatalytic reactions, such as hydrothermal digestion and catalytic reduction reactions, and further processing reactions. It is understood that hydrocatalytic treatment system  12  can comprise any number, combination, and type of reactors to perform one or more hydrocatalytic reactions. 
     In certain embodiments where hydrocatalytic treatment system  12  comprises hydrothermal digestion and one or more catalytic reduction reactions, the hydrothermal digestion and one or more catalytic reduction reactions take place in the same vessel, which can provide an effective stabilization of soluble carbohydrates. The foregoing may be accomplished by including a slurry catalyst capable of activating molecular hydrogen within a hydrothermal digestion unit containing cellulosic biomass solids. That is, the catalyst that is capable of activating molecular hydrogen may comprise a slurry catalyst. As used herein, the term “slurry catalyst” refers to a catalyst comprising fluidly mobile catalyst particles that can be at least partially suspended in a fluid phase via gas flow, liquid flow, mechanical agitation, or any combination thereof. Formation of the reaction product may reduce the amount of thermal decomposition that occurs during hydrothermal digestion, thereby enabling high yield conversion of cellulosic biomass solids into a desired reaction product to take place in a timely manner. 
     Once the soluble carbohydrates have been at least partially transformed into a more stable reaction product during hydrothermal digestion, completion of the conversion of the soluble carbohydrates into the reaction product may take place in a separate catalytic reduction reactor unit that also employs the slurry catalyst or a different catalyst that is capable of activating molecular hydrogen. The transformation that takes place in the catalytic reduction reactor unit may comprise a further reduction in the degree of oxidation of the initial reaction product, an increased conversion of soluble carbohydrates into oxygenated intermediates, or both. As used herein, the term “oxygenated intermediates” refers to alcohols, polyols, ketones, aldehydes, and mixtures thereof that are produced from a catalytic reduction reaction of soluble carbohydrates. 
     Continuous, high temperature hydrothermal digestion may be accomplished by configuring the biomass conversion systems such that fresh biomass may be continuously or semi-continuously supplied to the hydrothermal digestion unit, while it operates in a pressurized state. As used herein, the term “continuous addition” and grammatical equivalents thereof will refer to a process in which cellulosic biomass is added to a hydrothermal digestion unit in an uninterrupted manner without fully depressurizing the hydrothermal digestion unit. As used herein, the term “semi-continuous addition” and grammatical equivalents thereof will refer to a discontinuous, but as-needed, addition of biomass to a hydrothermal digestion unit without fully depressurizing the hydrothermal digestion unit. 
     In some embodiments described herein, a slurry catalyst may be used both in the hydrothermal digestion unit and in the catalytic reduction reactor unit to mediate the catalytic reduction reaction of soluble carbohydrates into a reaction product. Retention of the slurry catalyst in the hydrothermal digestion unit may also be aided by the low recycle ratios that may be used in the biomass conversion systems described herein. In any event, circulation of the slurry catalyst through the cellulosic biomass charge within the hydrothermal digestion unit can provide good catalyst distribution within the biomass, thereby allowing soluble carbohydrates to be effectively stabilized via a catalytic reduction reaction as soon as possible following their formation. 
     Since a slurry catalyst can be fluidly mobile, hydrogen sparge, solvent recycle, or any combination thereof may be used to distribute the slurry catalyst throughout the cellulosic biomass charge in the hydrothermal digestion unit. Good catalyst distribution in the cellulosic biomass may improve yields by intercepting soluble carbohydrates before they have an opportunity to degrade. Furthermore, use of a slurry catalyst may allow a fixed bed digestion unit to be more successfully used, since mechanical stirring or like mechanical agitation is not needed to affect catalyst distribution. This can allow higher biomass to solvent ratios to be utilized per unit volume of the digestion unit than would be possible in stirred tank or like digestion unit configurations. Furthermore, since stirring is not necessary, there is no express need to alter the size of the biomass solids prior to digestion taking place. 
     In one embodiment, poison-tolerant slurry catalyst is used. Use of a poison-tolerant catalyst may be particularly desirable, since catalyst poisons are not removed from the cellulosic biomass solids before hydrothermal digestion and integrated catalytic reduction take place. As used herein, a “poison-tolerant catalyst” is defined as a catalyst that is capable of activating molecular hydrogen without needing to be regenerated or replaced due to low catalytic activity for at least about 12 hours of continuous operation. 
     In some embodiments, suitable poison-tolerant catalysts may include, for example, sulfided catalysts. In some or other embodiments, nitrided catalysts may be used as poison-tolerant catalysts. Sulfided catalysts suitable for activating molecular hydrogen are described in commonly owned U.S. application Ser. No. 13/495,785, filed on Jun. 13, 2012, and 61/553,591, filed on Oct. 31, 2011, each of which is incorporated herein by reference in its entirety. Sulfiding may take place by treating the catalyst with hydrogen sulfide or an alternative sulfiding agent, optionally while the catalyst is disposed on a solid support. In more particular embodiments, the poison-tolerant catalyst may comprise a sulfided cobalt-molybdate catalyst, such as a catalyst comprising about 1-10 wt. % cobalt oxide and up to about 30 wt. % molybdenum trioxide prior to sulfidation. In other embodiments, catalysts containing Pt or Pd may also be effective poison-tolerant catalysts for use in the techniques described herein. When mediating in situ catalytic reduction reaction processes, sulfided catalysts may be particularly well suited to form reaction products comprising a substantial fraction of glycols (e.g., C 2 -C 6  glycols) without producing excessive amounts of the corresponding monohydric alcohols. Although poison-tolerant catalysts, particularly sulfided catalysts, may be well suited for forming glycols from soluble carbohydrates, it is to be recognized that other types of catalysts, which may not necessarily be poison-tolerant, may also be used to achieve a like result in alternative embodiments. As will be recognized by one having ordinary skill in the art, various reaction parameters (e.g., temperature, pressure, catalyst composition, introduction of other components, and the like) may be modified to favor the formation of a desired reaction product. Given the benefit of the present disclosure, one having ordinary skill in the art will be able to alter various reaction parameters to change the product distribution obtained from a particular catalyst and set of reactants. 
     Catalysts that are not particularly poison-tolerant may also be used in conjunction with the techniques described herein. Such catalysts may include, for example, Ru, Pt, Pd, or compounds thereof disposed on a solid support such as, for example, Ru on titanium dioxide or Ru on carbon. Although such catalysts may not have particular poison tolerance, they may be regenerable, such as through exposure of the catalyst to water at elevated temperatures, which may be in either a subcritical state or a supercritical state. 
     In some embodiments, slurry catalysts suitable for use in the methods described herein may be sulfided by dispersing a slurry catalyst in a fluid phase and adding a sulfiding agent thereto. Suitable sulfiding agents may include, for example, organic sulfoxides (e.g., dimethyl sulfoxide), hydrogen sulfide, salts of hydrogen sulfide (e.g., NaSH), and the like. In some embodiments, the slurry catalyst may be concentrated in the fluid phase after sulfiding and then added to the hydrothermal digestion unit. 
     In some embodiments, the slurry catalyst may be operable to generate molecular hydrogen. For example, in some embodiments, catalysts suitable for aqueous phase reforming (i.e., APR catalysts) may be used. Suitable APR catalysts may include, for example, catalysts comprising platinum, palladium, ruthenium, nickel, cobalt, or other Group VIII metals alloyed or modified with rhenium, molybdenum, tin, or other metals, or sulfided. However, in other embodiments, an external hydrogen feed may be used, optionally in combination with internally generated hydrogen. 
     In various embodiments, slurry catalysts used in embodiments described herein may have a particulate size of about 250 microns or less. In some embodiments, the slurry catalyst may have a particulate size of about 100 microns or less, or about 10 microns or less. In some embodiments, the minimum particulate size of the slurry catalyst may be about 1 micron. 
     In general, digestion in the hydrothermal digestion unit may be conducted in a liquor phase. In some embodiments, the liquor phase may comprise a digestion solvent that comprises water. In some embodiments, the liquor phase may further comprise an organic solvent. Although any organic solvent that is at least partially miscible with water may be used as a digestion solvent, particularly suitable organic solvents are those that can be directly converted into fuel blends and other materials without being separated from hydrocatalytically treated mixture  13 . That is, particularly suitable organic solvents are those that may be co-processed along with hydrocatalytically treated mixture  13  into fuel blends and other materials during further processing reactions. Suitable organic solvents in this regard may include, for example, ethanol, ethylene glycol, propylene glycol, glycerol, and any combination thereof. In some embodiments, the organic solvent may comprise oxygenated intermediates produced from a catalytic reduction reaction of soluble carbohydrates. For example, in some embodiments, a digestion solvent may comprise oxygenated intermediates produced by a hydrogenolysis reaction or other catalytic reduction reaction of soluble carbohydrates. In some embodiments, the oxygenated intermediates may include those produced from an in situ catalytic reduction reaction and/or from the catalytic reduction reactor unit. 
     In some embodiments employing hydrothermal digestion, the digestion solvent may further comprise a small amount of a monohydric alcohol. The presence of at least some monohydric alcohols in the fluid phase digestion medium may desirably enhance the hydrothermal digestion and/or the catalytic reduction reactions being conducted therein. For example, inclusion of about 1% to about 5% by weight monohydric alcohols in the fluid phase digestion medium may desirably maintain catalyst activity due to a surface cleaning effect. Monohydric alcohols present in the digestion solvent may arise from any source. In some embodiments, the monohydric alcohols may be formed via the in situ catalytic reduction reaction process being conducted therein. In some or other embodiments, the monohydric alcohols may be formed during further chemical transformations of the initially formed hydrocatalytically treated mixture  13 . In still other embodiments, the monohydric alcohols may be sourced from an external feed that is in flow communication with the cellulosic biomass solids. 
     In some embodiments, the digestion solvent may comprise between about 1% water and about 99% water. Although higher percentages of water may be more favorable from an environmental standpoint, higher quantities of organic solvent may more effectively promote hydrothermal digestion due to the organic solvent&#39;s greater propensity to solubilize carbohydrates and promote catalytic reduction of the soluble carbohydrates. In some embodiments, the digestion solvent may comprise about 90% or less water by weight. In other embodiments, the digestion solvent may comprise about 80% or less water by weight, or about 70% or less water by weight, or about 60% or less water by weight, or about 50% or less water by weight, or about 40% or less water by weight, or about 30% or less water by weight, or about 20% or less water by weight, or about 10% or less water by weight, or about 5% or less water by weight. 
     In some embodiments, the digestion solvent may comprise an organic solvent comprising oxygenated intermediates resulting from a catalytic reduction reaction of soluble carbohydrates. The catalytic reduction reaction may take place in the hydrothermal digestion unit and/or in the catalytic reduction reactor unit. In some embodiments, the organic solvent may comprise at least one alcohol, ketone, or polyol. In alternative embodiments, the digestion solvent may be at least partially supplied from an external source. For example, in some embodiments, bio-ethanol may be used to supplement the organic solvent. Other water-miscible organic solvents may be used as well. In some embodiments, the digestion solvent may be separated, stored, or selectively injected into the hydrothermal digestion unit so as to maintain a desired concentration of soluble carbohydrates or to provide temperature regulation in the hydrothermal digestion unit. 
     In various embodiments, digestion may take place over a period of time at elevated temperatures and pressures. In some embodiments, digestion may take place at a temperature ranging between about 100 to about 240 degrees C. for a period of time. In some embodiments, the period of time may range of about 0.25 to 24 hours. In some embodiments, the digestion to produce soluble carbohydrates may occur at a pressure ranging between about 1 bar (absolute) and about 100 bar. In general, the higher the temperature, the shorter the amount of time needed for hydrothermal digestion steps to take place. As an example, hydrothermal digestion may take place for about 1 hour to about 10 hours at a temperature of about 180 to about 270 degrees C., most typically from about 190 to 250 degrees C. 
     In various embodiments, suitable biomass digestion techniques may include, for example, acid digestion, alkaline digestion, enzymatic digestion, and digestion using hot-compressed water. In some embodiments, the methods may further comprise withdrawing at least a portion of the reaction product from the biomass conversion system (e.g., from the outlet of the catalytic reduction reactor unit or from the fluid circulation loop). In some embodiments, the methods may further comprise converting the reaction product into a biofuel, as described in further detail hereinafter. In some embodiments, the methods may further comprise separating solids (e.g., slurry catalyst, biomass fines, and the like) from the reaction product after its withdrawal from the biomass conversion system, as described above. 
     In some embodiments, the methods may further comprise recirculating at least a portion of the liquor phase from the catalytic reduction reactor unit to the hydrothermal digestion unit. As set forth above, the biomass conversion systems described herein are particularly suitable in being capable of rapidly at least partially transforming soluble carbohydrates into a reaction product comprising oxygenated intermediates by performing an in situ catalytic reduction reaction in the hydrothermal digestion unit. As also noted above, the liquor phase containing the reaction product may be recirculated from the catalytic reduction reactor unit to the hydrothermal digestion unit, where the liquor phase may, for example, help regulate temperature therein, serve as a digestion solvent, and the like. Recirculation from the catalytic reduction reactor unit to the hydrothermal digestion unit may take place at various recycle ratios. As used herein, the term “recycle ratio” refers to the amount of liquor phase that is recirculated to the hydrothermal digestion unit (e.g., within the fluid circulation loop) relative to the amount of liquor phase that is withdrawn from the biomass conversion system (e.g., by a reaction product takeoff line). 
     In some embodiments, the catalytic reduction reactions carried out in the hydrothermal digestion unit and the catalytic reduction reactor unit may be hydrogenolysis reactions. In some embodiments, the catalytic reduction reaction used to produce an alcoholic component in hydrocatalytically treated mixture  13  may take place at a temperature ranging between about 110° C. and about 300° C., or between about 170° C. and about 300° C., or between about 180° C. and about 290° C., or between about 150° C. and about 250° C. In some embodiments, the catalytic reduction reaction may take place at a pH ranging between about 7 and about 13, or between about 10 and about 12. In other embodiments, the catalytic reduction reaction may take place under acidic conditions, such as at a pH of about 5 to about 7. Acids, bases, and buffers may be introduced as necessary to achieve a desired pH level. In some embodiments, the catalytic reduction reaction may be conducted under a hydrogen partial pressure ranging between about 1 bar (absolute) and about 150 bar, or between about 15 bar and about 140 bar, or between about 30 bar and about 130 bar, or between about 50 bar and about 110 bar. 
     In some embodiments, catalysts capable of activating molecular hydrogen and conducting a catalytic reduction reaction may comprise a metal such as, for example, Cr, Mo, W, Re, Mn, Cu, Cd, Fe, Co, Ni, Pt, Pd, Rh, Ru, Ir, Os, and alloys or any combination thereof, either alone or with promoters such as Au, Ag, Cr, Zn, Mn, Sn, Bi, B, O, and alloys or any combination thereof. In some embodiments, the catalysts and promoters may allow for hydrogenation and hydrogenolysis reactions to occur at the same time or in succession of one another. In some embodiments, such catalysts may also comprise a carbonaceous pyropolymer catalyst containing transition metals (e.g., Cr, Mo, W, Re, Mn, Cu, and Cd) or Group VIII metals (e.g., Fe, Co, Ni, Pt, Pd, Rh, Ru, Ir, and Os). In some embodiments, the foregoing catalysts may be combined with an alkaline earth metal oxide or adhered to a catalytically active support. In some or other embodiments, the catalyst capable of activating molecular hydrogen may be deposited on a catalyst support that is not itself catalytically active. 
     In some embodiments, slurry catalysts suitable for use in the methods described herein may be sulfided by dispersing a slurry catalyst in a fluid phase and adding a sulfiding agent thereto. Suitable sulfiding agents may include, for example, organic sulfoxides (e.g., dimethyl sulfoxide), hydrogen sulfide, salts of hydrogen sulfide (e.g., NaSH), amino acids derived from proteins present in biomass feedstock  11  and the like. In some embodiments, the slurry catalyst may be concentrated in the fluid phase after sulfiding, and the concentrated slurry may then be distributed in the cellulosic biomass solids using fluid flow. Illustrative techniques for catalyst sulfiding that may be used in conjunction with the methods described herein are described in U.S. application Ser. No. 12/407,479 (U.S. Application Publication No. 20100236988), filed on Mar. 19, 2009 and incorporated herein by reference in its entirety. 
     In some embodiments, as mentioned above, hydrocatalytically treated mixture  13 , preferably overhead fraction  15 , may be further processed into a biofuel. Further processing of hydrocatalytically treated mixture  13  into a biofuel or other material may comprise any combination and sequence of further hydrogenolysis reactions and/or hydrogenation reactions, condensation reactions, isomerization reactions, oligomerization reactions, hydrotreating reactions, alkylation reactions, dehydration reactions, desulfurization reactions, and the like. The subsequent further processing reactions may be catalytic or non-catalytic. In some embodiments, an initial operation of downstream further processing may comprise a condensation reaction, often conducted in the presence of a condensation catalyst, in which hydrocatalytically treated mixture  13  or a product derived therefrom is condensed with another molecule to form a higher molecular weight compound. As used herein, the term “condensation reaction” will refer to a chemical transformation in which two or more molecules are coupled with one another to form a carbon-carbon bond in a higher molecular weight compound, usually accompanied by the loss of a small molecule such as water or an alcohol. An illustrative condensation reaction is the Aldol condensation reaction, which will be familiar to one having ordinary skill in the art. Additional disclosure regarding condensation reactions and catalysts suitable for promoting condensation reactions is provided hereinbelow. 
     In some embodiments, methods described herein may further comprise performing a condensation reaction on hydrocatalytically treated mixture  13  or a product derived therefrom. In various embodiments, the condensation reaction may take place at a temperature ranging between about 5° C. and about 500° C. The condensation reaction may take place in a condensed phase (e.g., a liquor phase) or in a vapor phase. For condensation reactions taking place in a vapor phase, the temperature may range between about 75° C. and about 500° C., or between about 125° C. and about 450° C. For condensation reactions taking place in a condensed phase, the temperature may range between about 5° C. and about 475° C., or between about 15° C. and about 300° C., or between about 20° C. and about 250° C. 
     In various embodiments, the higher molecular weight compound produced by the condensation reaction may comprise ≧C 4  hydrocarbons. In some or other embodiments, the higher molecular weight compound produced by the condensation reaction may comprise ≧C 6  hydrocarbons. In some embodiments, the higher molecular weight compound produced by the condensation reaction may comprise C 4 -C 30  hydrocarbons. In some embodiments, the higher molecular weight compound produced by the condensation reaction may comprise C 6 -C 30  hydrocarbons. In still other embodiments, the higher molecular weight compound produced by the condensation reaction may comprise C 4 -C 24  hydrocarbons, or C 6 -C 24  hydrocarbons, or C 4 -C 18  hydrocarbons, or C 6 -C 18  hydrocarbons, or C 4 -C 12  hydrocarbons, or C 6 -C 12  hydrocarbons. As used herein, the term “hydrocarbons” refers to compounds containing both carbon and hydrogen without reference to other elements that may be present. Thus, heteroatom-substituted compounds are also described herein by the term “hydrocarbons.” 
     The particular composition of the higher molecular weight compound produced by the condensation reaction may vary depending on the catalyst(s) and temperatures used for both the catalytic reduction reaction and the condensation reaction, as well as other parameters such as pressure. For example, in some embodiments, the product of the condensation reaction may comprise ≧C 4  alcohols and/or ketones that are produced concurrently with or in lieu of ≧C 4  hydrocarbons. In some embodiments, the ≧C 4  hydrocarbons produced by the condensation reaction may contain various olefins in addition to alkanes of various sizes, typically branched alkanes. In still other embodiments, the ≧C 4  hydrocarbons produced by the condensation reaction may also comprise cyclic hydrocarbons and/or aromatic compounds. In some embodiments, the higher molecular weight compound produced by the condensation reaction may be further subjected to a catalytic reduction reaction to transform a carbonyl functionality therein to an alcohol and/or a hydrocarbon and to convert olefins into alkanes. 
     Exemplary compounds that may be produced by a condensation reaction include, for example, ≧C 4  alkanes, ≧C 4  alkenes, ≧C 5  cycloalkanes, ≧C 5  cycloalkenes, aryls, fused aryls, ≧C 4  alcohols, ≧C 4  ketones, and mixtures thereof. The ≧C 4  alkanes and ≧C 4  alkenes may range from 4 to about 30 carbon atoms (i.e. C 4 -C 30  alkanes and C 4 -C 30  alkenes) and may be branched or straight chain alkanes or alkenes. The ≧C 4  alkanes and ≧C 4  alkenes may also include fractions of C 7 -C 14 , C 12 -C 24  alkanes and alkenes, respectively, with the C 7 -C 14  fraction directed to jet fuel blends, and the C 12 -C 24  fraction directed to diesel fuel blends and other industrial applications. Examples of various ≧C 4  alkanes and ≧C 4  alkenes that may be produced by the condensation reaction include, without limitation, butane, butene, pentane, pentene, 2-methylbutane, hexane, hexene, 2-methylpentane, 3-methylpentane, 2,2-dimethylbutane, 2,3-dimethylbutane, heptane, heptene, octane, octene, 2,2,4,-trimethylpentane, 2,3-dimethylhexane, 2,3,4-trimethylpentane, 2,3-dimethylpentane, nonane, nonene, decane, decene, undecane, undecene, dodecane, dodecene, tridecane, tridecene, tetradecane, tetradecene, pentadecane, pentadecene, hexadecane, hexadecene, heptyldecane, heptyldecene, octyldecane, octyldecene, nonyldecane, nonyldecene, eicosane, eicosene, uneicosane, uneicosene, doeicosane, doeicosene, trieicosane, trieicosene, tetraeicosane, tetraeicosene, and isomers thereof. 
     The ≧C 5  cycloalkanes and ≧C 5  cycloalkenes may have from 5 to about 30 carbon atoms and may be unsubstituted, mono-substituted or multi-substituted. In the case of mono-substituted and multi-substituted compounds, the substituted group may include a branched ≧C 3  alkyl, a straight chain ≧C 1  alkyl, a branched ≧C 3  alkylene, a straight chain ≧C 1  alkylene, a straight chain ≧C 2  alkylene, an aryl group, or a combination thereof. In some embodiments, at least one of the substituted groups may include a branched C 3 -C 12  alkyl, a straight chain C 1 -C 12  alkyl, a branched C 3 -C 12  alkylene, a straight chain C 1 -C 12  alkylene, a straight chain C 2 -C 12  alkylene, an aryl group, or a combination thereof. In yet other embodiments, at least one of the substituted groups may include a branched C 3 -C 4  alkyl, a straight chain C 1 -C 4  alkyl, a branched C 3 -C 4  alkylene, a straight chain C 1 -C 4  alkylene, a straight chain C 2 -C 4  alkylene, an aryl group, or any combination thereof. Examples of ≧C 5  cycloalkanes and ≧C 5  cycloalkenes that may be produced by the condensation reaction include, without limitation, cyclopentane, cyclopentene, cyclohexane, cyclohexene, methylcyclopentane, methylcyclopentene, ethylcyclopentane, ethylcyclopentene, ethylcyclohexane, ethylcyclohexene, and isomers thereof. 
     The moderate fractions of the condensation reaction, such as C 7 -C 14 , may be separated for jet fuel, while heavier fractions, such as C 12 -C 24 , may be separated for diesel use. The heaviest fractions may be used as lubricants or cracked to produce additional gasoline and/or diesel fractions. The ≧C 4  compounds may also find use as industrial chemicals, whether as an intermediate or an end product. For example, the aryl compounds toluene, xylene, ethylbenzene, para-xylene, meta-xylene, and ortho-xylene may find use as chemical intermediates for the production of plastics and other products. Meanwhile, C 9  aromatic compounds and fused aryl compounds, such as naphthalene, anthracene, tetrahydronaphthalene, and decahydronaphthalene, may find use as solvents or additives in industrial processes. 
     In some embodiments, a single catalyst may mediate the transformation of hydrocatalytically treated mixture  13  into a form suitable for undergoing a condensation reaction as well as mediating the condensation reaction itself. In other embodiments, a first catalyst may be used to mediate the transformation of hydrocatalytically treated mixture  13  into a form suitable for undergoing a condensation reaction, and a second catalyst may be used to mediate the condensation reaction. Unless otherwise specified, it is to be understood that reference herein to a condensation reaction and condensation catalyst refers to either type of condensation process. Further disclosure of suitable condensation catalysts now follows. 
     In some embodiments, a single catalyst may be used to form a higher molecular weight compound via a condensation reaction. Without being bound by any theory or mechanism, it is believed that such catalysts may mediate an initial dehydrogenation of hydrocatalytically treated mixture  13 , followed by a condensation reaction of the dehydrogenated alcoholic component. Zeolite catalysts are one type of catalyst suitable for directly converting alcohols to condensation products in such a manner. A particularly suitable zeolite catalyst in this regard may be ZSM-5, although other zeolite catalysts may also be suitable. 
     In some embodiments, two catalysts may be used to form a higher molecular weight compound via a condensation reaction. Without being bound by any theory or mechanism, it is believed that the first catalyst may mediate an initial dehydrogenation of hydrocatalytically treated mixture  13 , and the second catalyst may mediate a condensation reaction of the dehydrogenated hydrocatalytically treated mixture  13 . Like the single-catalyst embodiments discussed previously above, in some embodiments, zeolite catalysts may be used as either the first catalyst or the second catalyst. Again, a particularly suitable zeolite catalyst in this regard may be ZSM-5, although other zeolite catalysts may also be suitable. 
     Various catalytic processes may be used to form higher molecular weight compounds by a condensation reaction. In some embodiments, the catalyst used for mediating a condensation reaction may comprise a basic site, or both an acidic site and a basic site. Catalysts comprising both an acidic site and a basic site will be referred to herein as multi-functional catalysts. In some or other embodiments, a catalyst used for mediating a condensation reaction may comprise one or more metal atoms. Any of the condensation catalysts may also optionally be disposed on a solid support, if desired. 
     In some embodiments, the condensation catalyst may comprise a basic catalyst comprising Li, Na, K, Cs, B, Rb, Mg, Ca, Sr, Si, Ba, Al, Zn, Ce, La, Y, Sc, Y, Zr, Ti, hydrotalcite, zinc-aluminate, phosphate, base-treated aluminosilicate zeolite, a basic resin, basic nitride, alloys or any combination thereof. In some embodiments, the basic catalyst may also comprise an oxide of Ti, Zr, V, Nb, Ta, Mo, Cr, W, Mn, Re, Al, Ga, In, Co, Ni, Si, Cu, Zn, Sn, Cd, Mg, P, Fe, or any combination thereof. In some embodiments, the basic catalyst may comprise a mixed-oxide basic catalyst. Suitable mixed-oxide basic catalysts may comprise, for example, Si—Mg—O, Mg—Ti—O, Y—Mg—O, Y—Zr—O, Ti—Zr—O, Ce—Zr—O, Ce—Mg—O, Ca—Zr—O, La—Zr—O, B—Zr—O, La—Ti—O, B—Ti—O, and any combination thereof. In some embodiments, the condensation catalyst may further include a metal or alloys comprising metals such as, for example, Cu, Ag, Au, Pt, Ni, Fe, Co, Ru, Zn, Cd, Ga, In, Rh, Pd, Ir, Re, Mn, Cr, Mo, W, Sn, Bi, Pb, Os, alloys and combinations thereof. Use of metals in the condensation catalyst may be desirable when a dehydrogenation reaction is to be carried out in concert with the condensation reaction. Basic resins may include resins that exhibit basic functionality. The basic catalyst may be self-supporting or adhered to a support containing a material such as, for example, carbon, silica, alumina, zirconia, titania, vanadia, ceria, nitride, boron nitride, a heteropolyacid, alloys and mixtures thereof. 
     In some embodiments, the condensation catalyst may comprise a hydrotalcite material derived from a combination of MgO and Al 2 O 3 . In some embodiments, the condensation catalyst may comprise a zinc aluminate spinel formed from a combination of ZnO and Al 2 O 3 . In still other embodiments, the condensation catalyst may comprise a combination of ZnO, Al 2 O 3 , and CuO. Each of these materials may also contain an additional metal or alloy, including those more generally referenced above for basic condensation catalysts. In more particular embodiments, the additional metal or alloy may comprise a Group 10 metal such Pd, Pt, or any combination thereof. 
     In some embodiments, the condensation catalyst may comprise a basic catalyst comprising a metal oxide containing, for example, Cu, Ni, Zn, V, Zr, or any mixture thereof. In some or other embodiments, the condensation catalyst may comprise a zinc aluminate containing, for example, Pt, Pd, Cu, Ni, or any mixture thereof. 
     In some embodiments, the condensation catalyst may comprise a multi-functional catalyst having both an acidic functionality and a basic functionality. Such condensation catalysts may comprise a hydrotalcite, a zinc-aluminate, a phosphate, Li, Na, K, Cs, B, Rb, Mg, Si, Ca, Sr, Ba, Al, Ce, La, Sc, Y, Zr, Ti, Zn, Cr, or any combination thereof. In further embodiments, the multi-functional catalyst may also include one or more oxides from the group of Ti, Zr, V, Nb, Ta, Mo, Cr, W, Mn, Re, Al, Ga, In, Fe, Co, Ir, Ni, Si, Cu, Zn, Sn, Cd, P, and any combination thereof. In some embodiments, the multi-functional catalyst may include a metal such as, for example, Cu, Ag, Au, Pt, Ni, Fe, Co, Ru, Zn, Cd, Ga, In, Rh, Pd, Ir, Re, Mn, Cr, Mo, W, Sn, Os, alloys or combinations thereof. The basic catalyst may be self-supporting or adhered to a support containing a material such as, for example, carbon, silica, alumina, zirconia, titania, vanadia, ceria, nitride, boron nitride, a heteropolyacid, alloys and mixtures thereof. 
     In some embodiments, the condensation catalyst may comprise a metal oxide containing Pd, Pt, Cu or Ni. In still other embodiments, the condensation catalyst may comprise an aluminate or a zirconium metal oxide containing Mg and Cu, Pt, Pd or Ni. In still other embodiments, a multi-functional catalyst may comprise a hydroxyapatite (HAP) combined with one or more of the above metals. 
     In some embodiments, the condensation catalyst may also include a zeolite and other microporous supports that contain Group IA compounds, such as Li, Na, K, Cs and Rb. Preferably, the Group IA material may be present in an amount less than that required to neutralize the acidic nature of the support. A metal function may also be provided by the addition of group VIIIB metals, or Cu, Ga, In, Zn or Sn. In some embodiments, the condensation catalyst may be derived from the combination of MgO and Al 2 O 3  to form a hydrotalcite material. Another condensation catalyst may comprise a combination of MgO and ZrO 2 , or a combination of ZnO and Al 2 O 3 . Each of these materials may also contain an additional metal function provided by copper or a Group VIIIB metal, such as Ni, Pd, Pt, or combinations of the foregoing. 
     The condensation reaction mediated by the condensation catalyst may be carried out in any reactor of suitable design, including continuous-flow, batch, semi-batch or multi-system reactors, without limitation as to design, size, geometry, flow rates, and the like. The reactor system may also use a fluidized catalytic bed system, a swing bed system, fixed bed system, a moving bed system, or a combination of the above. In some embodiments, bi-phasic (e.g., liquid-liquid) and tri-phasic (e.g., liquid-liquid-solid) reactors may be used to carry out the condensation reaction. 
     In some embodiments, an acid catalyst may be used to optionally dehydrate at least a portion of the reaction product. Suitable acid catalysts for use in the dehydration reaction may include, but are not limited to, mineral acids (e.g., HCl, H 2 SO 4 ), solid acids (e.g., zeolites, ion-exchange resins) and acid salts (e.g., LaCl 3 ). Additional acid catalysts may include, without limitation, zeolites, carbides, nitrides, zirconia, alumina, silica, aluminosilicates, phosphates, titanium oxides, zinc oxides, vanadium oxides, lanthanum oxides, yttrium oxides, scandium oxides, magnesium oxides, cerium oxides, barium oxides, calcium oxides, hydroxides, heteropolyacids, inorganic acids, acid modified resins, base modified resins, and any combination thereof. In some embodiments, the dehydration catalyst may also include a modifier. Suitable modifiers may include, for example, La, Y, Sc, P, B, Bi, Li, Na, K, Rb, Cs, Mg, Ca, Sr, Ba, and any combination thereof. The modifiers may be useful, inter alia, to carry out a concerted hydrogenation/dehydrogenation reaction with the dehydration reaction. In some embodiments, the dehydration catalyst may also include a metal. Suitable metals may include, for example, Cu, Ag, Au, Pt, Ni, Fe, Co, Ru, Zn, Cd, Ga, In, Rh, Pd, Ir, Re, Mn, Cr, Mo, W, Sn, Os, alloys, and any combination thereof. The dehydration catalyst may be self supporting, supported on an inert support or resin, or it may be dissolved in a fluid. 
     Various operations may optionally be performed on hydrocatalytically treated mixture  13  prior to conducting a condensation reaction. In addition, various operations may optionally be performed on a fluid phase containing hydrocatalytically treated mixture  13 , thereby further transforming hydrocatalytically treated mixture  13  or placing it in a form more suitable for taking part in a condensation reaction. These optional operations are now described in more detail below. 
     As described above, one or more liquid phases may be present when digesting cellulosic biomass solids. Particularly when cellulosic biomass solids are fed continuously or semi-continuously to the hydrothermal digestion unit, digestion of the cellulosic biomass solids may produce multiple liquid phases in the hydrothermal digestion unit. The liquid phases may be immiscible with one another, or they may be at least partially miscible with one another. In some embodiments, the one or more liquid phases contained in hydrocatalytically treated mixture  13  may comprise a phenolics liquid phase comprising lignin or a product formed therefrom, an aqueous phase comprising an alcoholic component, a light organics phase, or any combination thereof. 
     In some embodiments, heating of biomass feedstock  11  and the fluid phase digestion medium to form soluble carbohydrates and a phenolics liquid phase may take place while biomass feedstock  11  is in a pressurized state. As used herein, the term “pressurized state” refers to a pressure that is greater than atmospheric pressure (1 bar). Heating a fluid phase digestion medium in a pressurized state may allow the normal boiling point of the digestion solvent to be exceeded, thereby allowing the rate of hydrothermal digestion to be increased relative to lower temperature digestion processes. In some embodiments, heating biomass feedstock  11  and the fluid phase digestion medium may take place at a pressure of at least about 30 bar. In some embodiments, heating biomass feedstock  11  and the fluid phase digestion medium may take place at a pressure of at least about 60 bar, or at a pressure of at least about 90 bar. In some embodiments, heating biomass feedstock  11  and the fluid phase digestion medium may take place at a pressure ranging between about 30 bar and about 430 bar. In some embodiments, heating biomass feedstock  11  and the fluid phase digestion medium may take place at a pressure ranging between about 50 bar and about 330 bar, or at a pressure ranging between about 70 bar and about 130 bar, or at a pressure ranging between about 30 bar and about 130 bar. 
     To facilitate a better understanding of the present invention, the following examples of preferred embodiments are given. In no way should the following examples be read to limit, or to define, the scope of the invention. 
     EXAMPLES 
     To facilitate a better understanding of the present invention, the following examples of preferred embodiments are given. In no way should the following examples be read to limit, or to define, the scope of the invention. 
     Example 1  
     A 100-ml Parr reactor was charged with 60.18 grams of deionized water solvent, and 0.754 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 &amp; Technologies L.P. The catalyst was sulfided by the method described in Example 5 of U.S. Application Publication No. 2010/0236988. The reactor was charged with about 5.05 grams of southern pine mini-chips (39% moisture, having a nominal size of about 3 mm×5 mm×5 mm in dimension), and about 0.195 grams of potassium carbonate buffer, before pressuring with 54 bar of hydrogen under magnetic stirring. The stirred reactor was heated to 190° C. for 1 hour. Subsequently, the reactor was heated to 250° C. for 5 hours, which was the end of a cycle. A sample of about 1-2 grams of mixed product was removed via a 0.5 micron sintered metal dip tube at the end of the cycle, while the reactor was still at reaction temperature and stirred. At the end of a cycle, the reactor was cooled, depressurized, and opened for additional wood to be added. Wood addition for cycles 2 through 5 entailed addition of 4.91, 5.09, 5.84, and 5.59 grams of wood. For cycle 6, 2.5 grams of glycerol were added to assess kinetics. For cycle 7, 5.9 grams of nominal 39% moisture ground pine chips were added. For cycle 8, 6.5 grams of pine chips were added. Following the addition of material (wood or glycerol) at the beginning of each cycle, the reactor was repressurized with hydrogen, and again reheated to initiate another cycle. After eight cycles of adding wood or glycerol, the 0.5 micron sintered metal dip tube plugged, and it was not possible to sample the mixed reaction phases. The mixture from the reactant was cooled down and a bottom fraction was separated by liquid-liquid separation. The bottom fraction exhibited a viscosity of greater than about 10,000 cP, measured via timing and flow on an inclined plane while reheating to about 110 degrees C. 
     The bottom fraction was analyzed by gas chromatography (“DB5-ox method”) via dissolving the sample in excess acetone solvent using a 60-m×0.32 mm ID DB-5 column of 1 μm thickness, with 50:1 split ratio, 2 ml/min helium flow, and column oven at 40° C. for 8 minutes, followed by ramp to 285° C. at 10° C./min, and a hold time of 53.5 minutes. The injector temperature was set at 250° C., and the detector temperature was set at 300° C. Analysis revealed the presence of components with a boiling point greater than that of n-butanol, and the bottom fraction included methoxypropyl phenol and tetrahydrofurfural alcohol. The total weight percent of species detected in the bottom fraction was less than 100%, indicating the presence of higher molecular weight oligomers which could not elute from the heated GC injector. 
     Example 1 shows separation of a bottom fraction containing a lignin-derived phase from a top fraction liquid phase, where the bottom fraction contains phenolics and other heavy oligomers. This bottom fraction can be gasified to form hydrogen according to embodiments of the invention. 
     Example 2  
     Example 1 was repeated with 60.06 grams of 25% ethanol in water as solvent, and 0.749 grams of sulfided cobalt molybdate catalyst. The reactor was pressurized to 52 bar with hydrogen, and heated to 190° C. for 1 hour, then to 250° C. for 3 hours, and subsequently to 270° C. for 2 hours. After 8 cycles of adding 6 grams of wood for each cycle as described above in Example 1, formation of a viscous phase on reactor internals was observed. The viscous phase exhibited a viscosity greater than 1000 cP at room temperature. This phase was separated using liquid-liquid separation to generate a bottom fraction. Analysis of this heavy bottoms fraction again revealed the presence of compounds with a boiling point that is higher than that of n-butanol, including tetrahydrofurfural alcohol and methoxypropyl phenol and propyl phenol. The total weight percent of species detected in the bottom fraction was less than 100%, indicating the presence of higher molecular weight oligomers which could not elute from the heated GC injector. Example 2 also shows the formation of a heavy phase which can be separated from a main reaction mixture by gravity settling, and which can be gasified to form hydrogen according to embodiments of the invention. 
     Example 3  
     Example 1 was repeated with 50% ethanol in water as solvent. A heavy viscous phase coating internals and the bottom of the reactor was observed after 10 cycles of adding wood chips as described above in Example 1, with viscosity greater than 10,000 cP. Wood additions comprised 6.05, 6.06, 6.06, 6.06, 6.01, 6.00, 6.01, 6.02, 6.06, and 6.06 for completion of ten cycles. After the 10 cycles, the reactor was subjected to 5 hours of treatment under 52 bar of H 2  at 290° C., upon which the viscosity of the lower layer was reduced to less than about 500 cP. The high temperature hydrogen treatment led to increased formation of methoxy and alkyl phenols, such that the observed weight percent of compounds in the GC was more than 3-fold higher than for the similar phase formed in Example 2. The treated phase can be distilled to remove the components of lower volatility that can elute from a GC injector. The remaining bottom fraction containing heavy components, which comprise the unseen weight percent in the GC analysis, can be gasified to form hydrogen according to embodiments of the invention. 
     Example 4  
     A 100-ml Parr reactor was charged with a solvent mixture comprising 29.3 grams of 1,2-propylene glycol, 3.3 grams of ethylene glycol, and 32.5 grams of deionized water. 0.75 grams of nickel-oxide promoted cobalt molybdate catalyst were added (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 &amp; Technologies L.P., and sulfided by the method described in US2010/0236988 Example 5. 
     The reactor was charged with 6.1 grams of southern pine mini-chips (39% moisture), of nominal size 3×5×5 mm in dimension, before pressuring with 53 bar of hydrogen. The stirred reactor was heated to 190° C. for 1 hour, and subsequently heated to 250 ° C. for 5 hours to complete a cycle as described above in Example 1. 
     At the end of each cycle, 5.4 grams of product were withdrawn via a pipette. 6.0 grams of wood were charged to initiate a second reaction cycle using the protocol described in Example 1, along with 0.05 to 0.15 grams of buffer as needed to maintain pH between 5 and 6. Reactor product after each cycle was analyzed by gas chromatography using a 60-m×0.32 mm ID DB-5 column of 1 μm thickness, with 50:1 split ratio, 2 ml/min helium flow, and column oven at 40° C. for 8 minutes, followed by ramp to 285° C. at 10° C./min, and a hold time of 53.5 minutes. The injector temperature was set at 250° C., and the detector temperature was set at 300° C. The reaction sequence was continued through 45 cycles. At the end of cycle 45, 19.1262 grams of aqueous phase were decanted from the viscous heavy components phase. The remaining viscous heavy components phase can be gasified to form hydrogen according to embodiments of the invention. 
     A distillation of the aqueous layer was conducted at ambient pressure under N2 blanket, using a 50-ml micro flask with short-path distillation head. The distillation was continued until 58% of the initial still contents were collected as overhead distillate. A first distillation cut was taken as bottoms temperature increased from 120 to 168 degrees C. A second distillation cut was taken at bottoms temperatures between 169 and 186 degrees C. The atmospheric distillation was terminated at 196.9 degrees C. bottoms temperature, and gave a fraction comprising diols and acids. 
     The distillation of this fraction was resumed under vacuum at a nominal pressure of 10 Torr. A maximum temperature of 279 degrees C. was obtained, and 32% of the heavy ends from vacuum distillation were recovered as overhead distillate. The resulting bottom fraction from vacuum distillation was dissolved in dichloromethane and analyzed by GC MS. Many components were too heavy to analyze. Overall structures resembled asphaltenes, with some phenolic groups present. 
     The distillation bottoms flask was unwrapped and tipped sideways to demonstrate flow of heavy residue at a bottoms temperature of about 268 degrees C., at an estimated viscosity in excess of 1000 cP. About 82% of the final residue could be poured out of the hot flask. Upon cooling, the residue would not flow and required removal by spatula for sampling. 
     This example shows thermal distillation of intermediate production from digestion-reaction of wood biomass using a catalyst capable of activating molecular hydrogen, under a hydrogen atmosphere. Mono- and di-oxygenates which can be coupled via condensation-oligomeration reactions could be separated by distillation at atmospheric pressure and under vacuum, leaving a heavy tar-like residue. The heavy residue could be kept molten to flow out of distillation kettle when heated above 250 degrees C. This bottom fraction from vacuum distillation containing heavy residues can be gasified to form hydrogen according to embodiments of the present invention. Alternatively, the temperature of the atmospheric distillation can be increased to produce a bottom fraction that can be gasified to form hydrogen according to embodiments of the invention. 
     Example 5  
     Example 4 was repeated using 4-methyl-2-pentanol (methyl isobutyl carbinol or “MIBC”) as the digestion medium, and with use of larger scale batches were run conducted in a 450 mL Parr reactor. The reactor was initially charged with 220.06 g of MIBC, 25.08 g deionized water, 0.855 g of potassium carbonate buffer, and 8.1065 g of sulfided cobalt-molybdate catalyst as described in Example 1. For each reaction cycle, 27 g of softwood pine mini-chips were added, and an equivalent amount of liquid sample was removed at the end of each cycle. For liquid sample removal after each cycle, a portion of the lower aqueous layer was removed from as liquid above the settled catalyst layer, if present, followed by removal of a sufficient amount of the upper layer if required to maintain the liquid inventory in the reactor at a 60% level. After 17 cycles, a sample of the upper layer was distilled at atmospheric pressure under nitrogen, followed by vacuum distillation at 10 Torr. Distillate cut number 2 was collected under nitrogen at atmospheric pressure with a kettle bottoms temperature of about 110 to 140 degrees C. and an overheads temperature of about 90 degrees C. Cut number 2 contains a mixture of oxygenated and alkane intermediates. With a kettle temperature of about 258 to 302 degrees C., a vacuum distillation cut containing an estimated 30% of the reactor product was obtained as distillate cut number 6. In addition to alcohols (including glycols and other diols), significant quantities of phenolic compounds were obtained in cut number 6. For example, methoxy propyl phenol was found to be present in quantities greater than 4%. Tetrahydrofurfural alcohol was also found as a significant reaction product. No observable viscous layer or tar was formed under the experimental conditions of Example 5. A final vacuum distillation cut representing the end point of distillation (final 1% of feed) is produced and reported in Table 1 below. 
     
       
         
           
               
             
               
                 TABLE 1 
               
             
            
               
                   
               
               
                 Final vacuum distillation cut at  
               
               
                 348 degrees C. bottom temperature 
               
            
           
           
               
               
               
            
               
                   
                 Name 
                 area % 
               
               
                   
                   
               
               
                   
                 acetone (diluent) 
                 N/A 
               
               
                   
                 1-butanol (internal 
                 N/A 
               
               
                   
                 standard) 
                   
               
               
                   
                 4-methyl-2-Pentanol 
                 N/A 
               
               
                   
                 tetrahydro 
                 3.27% 
               
               
                   
                 Furanmethanol 
                   
               
               
                   
                 phenol 
                 6.93% 
               
               
                   
                 methoxy phenol 
                 8.61% 
               
               
                   
                 methyl phenol 
                 12.39%  
               
               
                   
                 unknown 
                 3.89% 
               
               
                   
                 dimethy phenol 
                 7.37% 
               
               
                   
                 methyl methoxy phenol 
                 6.27% 
               
               
                   
                 ethyl phenol 
                 6.15% 
               
               
                   
                 methyl ethyl phenol 
                 5.51% 
               
               
                   
                 unknown 
                 2.58% 
               
               
                   
                 ethyl methoxy phenol 
                 5.24% 
               
               
                   
                 unknown 
                 3.76% 
               
               
                   
                 propyl phenol 
                 6.09% 
               
               
                   
                 unknown 
                 0.91% 
               
               
                   
                 benzene diol 
                 5.24% 
               
               
                   
                 propyl methoxy phenol 
                 6.30% 
               
               
                   
                 unknown 
                 1.15% 
               
               
                   
                 unknown 
                 2.50% 
               
               
                   
                 unknown 
                 5.84% 
               
               
                   
                   
               
            
           
         
       
     
     The distillation flask bottoms after distillation with a final temperature of about 345 degrees C. continued to boil and bubble, but formed a solid char with resemblance to coal, upon cooling to room temperature. This example shows digestion and reaction intermediates. Distillation allows removal of monooxygenates and diols, with some phenols. Some heavy tar components with separation points in excess of 350 degrees C. remain in the bottoms, and for a char phase upon cooling. At least one of distillation cut number 6, the final vacuum distillation cut, and the heavy tar components remaining in the bottoms can be gasified to form hydrogen according to embodiments of the invention. 
     Example 6  
     Example 5 was repeated with 34 cycles of wood addition. Distillation was conducted at atmospheric pressure under N 2  to remove 85% of the reactor contents as overhead product, analyzed as a mixture of monooxygenates and some diols. The remaining 15% kettle bottoms formed a non-flowable viscous tar at room temperature, for which dissolution in acetone solvent required reheating. The remaining 15% kettle bottoms can be gasified to form hydrogen according to embodiments of the invention. 
     Further modifications and alternative embodiments of various aspects of the invention will be apparent to those skilled in the art in view of this description. Accordingly, this description is to be construed as illustrative only and is for the purpose of teaching those skilled in the art the general manner of carrying out the invention. It is to be understood that the forms of the invention shown and described herein are to be taken as the presently preferred embodiments. Elements and materials may be substituted for those illustrated and described herein, parts and processes may be reversed, and certain features of the invention may be utilized independently, all as would be apparent to one skilled in the art after having the benefit of this description of the invention. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the following claims.