# Patent

## Title
Production of renewable bio-distillate

## Abstract

A process and system for separating a light fraction, a bio-distillate fraction, and a heavy fraction from a bio-oil, and for producing a renewable distillate including at least in part the bio-distillate fraction and a stabilizing additive, is provided. In addition, a process and system is provided for upgrading a bio-oil by use of a diluent and/or a recycle stream from the upgrading process to reduce fouling in upgrading equipment, such as a preheater and a hydrodeoxygenation unit.

## Background
CROSS REFERENCE TO RELATED APPLICATIONS/INCORPORATION BY REFERENCE STATEMENT
This application is a Continuation-in-Part of, and claims the benefit of, co-pending U.S. application Ser. No. 13/533,432, filed Jun. 26, 2012, which is hereby incorporated by reference in its entirety herein. Co-pending U.S. application Ser. No. 13/533,432 is a continuation application of U.S. Ser. No. 12/915,872 filed on Oct. 29, 2010, which is also hereby incorporated by reference in its entirety herein. All publications and patents mentioned herein are hereby incorporated by reference in their entirety as if each individual publication or patent was specifically and individually indicated to be incorporated by reference.


BACKGROUND
1. Field of the Invention
The present invention relates generally to processes and systems for separating a bio-distillate fraction from a bio-oil. More specifically, the invention relates to the production of a renewable distillate including at least in part the bio-distillate fraction. An embodiment of the present invention also relates to processes for upgrading a bio-oil by use of a diluent and/or a recycle stream from the upgrading process to reduce fouling in upgrading equipment, such as a hydrodeoxygenation unit.
2. Description of the Related Art
With the rising costs and environmental concerns associated with fossil fuels, renewable energy sources have become increasingly important. The development of renewable fuel sources provides a means for reducing the dependence on fossil fuels. Accordingly, many different areas of renewable fuel research are currently being explored and developed.
With its low cost and wide availability, biomass has increasingly been emphasized as an ideal feedstock in renewable fuel research. Consequently, many different conversion processes have been developed that use biomass as a feedstock to produce useful biofuels and/or specialty chemicals. Existing biomass conversion processes include, for example, combustion, gasification, slow pyrolysis, fast pyrolysis, liquefaction, and enzymatic conversion. One of the useful products that may be derived from the aforementioned biomass conversion processes is a liquid product commonly referred to as “bio-oil.” Bio-oil may be processed into transportation fuels, hydrocarbon chemicals, and/or specialty chemicals.
Despite recent advancements in biomass conversion processes, many of the existing biomass conversion processes produce low-quality bio-oils containing high amounts of oxygen which are difficult, if not impossible, to separate into various fractions. These bio-oils require extensive secondary upgrading in order to be utilized as transportation fuels and/or as fuel additives due to the high amounts of oxygen present in the bio-oil. Furthermore, these transportation fuels and/or fuel additives derived from bio-oil vary in quality depending on the original oxygen content of the bio-oil.
Accordingly, there is a need for an improved process and system for separating bio-oil into various fractions such as bio-distillate, and using such fractions as blend components of renewable fuels.
Further, although bio-oil obtained from biomass catalytic pyrolysis is more stable than thermal pyrolysis oils, it is still generally less stable than petroleum derived hydrocarbons. This instability is associated with bimolecular reactions, such as condensation and/or polymerization reactions, of oxygen-containing compounds. At the typical elevated reactor temperatures of hydrotreating units (such as 300-500° C.), these instability reactions become more pronounced resulting in heavier compounds which create deposits in both the hydrotreating feed pre-heater and in the hydrotreater unit. In order to minimize such fouling in commercial operations, the preheater and hydrotreater temperatures are kept as low as possible while still sufficiently high to provide effective hydrodeoxygenation. However, even with such temperature control there is still significant fouling requiring frequent and costly unit shutdowns for deposit removal, hydrotreating catalyst regeneration, and/or hydrotreating catalyst replacement. Accordingly, there remains a need for an improved process for upgrading bio-oil which reduces fouling of the upgrading equipment.
SUMMARY OF THE INVENTION
In one embodiment, the present invention is directed to a bio-distillate fraction production process comprising (a) converting biomass in a conversion reactor containing a catalyst to thereby produce a conversion reactor effluent comprising vapor conversion products; (b) condensing at least portion of the vapor conversion products to thereby provide a bio-oil having a total oxygen content of less than about 15 weight percent; and (c) separating a bio-distillate fraction from the bio-oil, wherein at least about 75 weight percent of the bio-distillate fraction has a boiling point between about 180° C. and about 380° C., and wherein the bio-distillate fraction comprises at least about 50 or 40 weight percent oxygen-free hydrocarbons.
In another embodiment, the present invention is directed to a renewable distillate production process comprising: (a) separating a bio-oil into at least a bio-distillate fraction, wherein at least about 75 weight percent of the bio-distillate fraction has a boiling point between about 180° C. and about 380° C., wherein the bio-oil has not previously been subjected to an oxygen-removing hydrotreatment step; and (b) combining at least a portion of the bio-distillate fraction with a petroleum-derived-distillate-range stream, and a stabilizing additive having surfactant properties, to thereby produce a renewable distillate having a single clear phase, wherein the renewable distillate comprises the petroleum-derived-distillate-range stream in an amount of between about 5 weight percent and about 99 weight percent, the bio-distillate fraction in an amount of at least about 0.5 weight percent, and the stabilizing additive in an amount between about 0.5 and about 25 weight percent.
In a further embodiment, the present invention is directed to a bio-distillate fraction having a total oxygen content of less than about 15 weight percent, wherein at least about 75 weight percent of the bio-distillate fraction has a boiling point between about 180° C. and about 380° C., and the bio-distillate fraction comprises at least about 50 or 40 weight percent oxygen-free hydrocarbons.
In a further embodiment, the present invention is directed to a renewable distillate composition comprising a petroleum-derived-distillate-range stream in an amount of between about 5 weight percent and about 99 weight percent, a bio-distillate fraction in an amount of at least about 0.5 weight percent, and a stabilizing additive having surfactant properties in an amount between about 0.5 and about 25 weight percent.
In a further embodiment, the present invention is directed to a process for upgrading bio-oil comprising:

    
    
        a) combining a bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt % with a diluent thereby forming a feed stream;
        b) charging the feed stream to a preheater and heating the feed stream to a temperature in the range of from about 20 to about 450° C. in the preheater thereby forming a heated feed stream;
        c) charging the heated feed stream to a hydrodeoxygenation unit operated at a temperature in the range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil; and
        d) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil.
    
    


In a further embodiment, the present invention is directed to a process for upgrading bio-oil comprising:

    
    
        a) combining a bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt % with a diluent comprising a recycle stream thereby forming a feed stream;
        b) charging the feed stream to a preheater and heating the feed stream to a temperature in the range of from about 20 to about 450° C. in the preheater thereby forming a heated feed stream;
        c) charging the heated feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in the range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
        d) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil, wherein the at least one inter-stage stream and the product stream are each at a higher temperature than the bio-oil; and
        e) utilizing as the recycle stream a portion of at least one of: i) the at least one inter-stage stream, and ii) the product stream.
    
    


In a further embodiment, the present invention is directed to a process for upgrading bio-oil comprising:

    
    
        a) combining a bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt % with a diluent thereby forming a first feed stream;
        b) charging the first feed stream to a preheater and heating the first feed stream to a temperature in the range of from about 20 to about 100° C. in the preheater thereby forming a heated first feed stream;
        c) combining a recycle stream having a temperature of from about 100 to about 460° C. with the heated first feed stream thereby forming a second feed stream having a temperature in the range of from about 20 to about 450° C.;
        d) charging the second feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in the range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
        e) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil, wherein the at least one inter-stage stream and the product stream are each at a higher temperature than the bio-oil; and
        f) utilizing as the recycle stream a portion of at least one of: i) the at least one inter-stage stream, and ii) the product stream.
    
    


In a further embodiment, the present invention is directed to a process for upgrading bio-oil comprising:

    
    
        a) combining a bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt % with a diluent thereby forming a feed stream;
        b) charging a portion of the feed stream as a preheater feed stream to a preheater and heating the preheater feed stream to a temperature in the range of from about 20 to about 450° C. in the preheater thereby forming a heated feed stream;
        c) charging the heated feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in the range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
        d) charging a portion of the feed stream as a quench to at least one of the inter-stage streams to thereby form a quenched inter-stage stream and control the temperature of the downstream stages; and
        e) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil.
    
    





BRIEF DESCRIPTION OF THE FIGURES
FIG. 1 is a schematic diagram of a biomass conversion system according to one embodiment of the present invention.
FIG. 2 is a schematic diagram of a bio-oil upgrading system according to one embodiment of the present invention.
FIG. 3 is a schematic diagram of a bio-oil upgrading system according to one embodiment of the present invention.
FIG. 4 is a schematic diagram of a bio-oil upgrading system according to one embodiment of the present invention.
FIG. 5 is a schematic diagram of a bio-oil upgrading system according to one embodiment of the present invention.



DETAILED DESCRIPTION
FIG. 1 depicts a biomass conversion system 10 that includes a means for separating bio-oil into various fractions or fuel additives and blending the bio-distillate fraction with a petroleum-derived-distillate-range stream, as a blend stock or fuel additive, to form renewable distillate.
It should be understood that the biomass conversion system shown in FIG. 1 is just one example of a system within which the present invention can be embodied. The present invention may find application in a wide variety of other systems where it is desirable to efficiently and effectively separate bio-oil into renewable fuels and/or fuel additives. The exemplary biomass conversion system illustrated in FIG. 1 will now be described in detail.
The biomass conversion system 10 of FIG. 1 includes a biomass source 12 for supplying a biomass feedstock to be converted to bio-oil. The biomass source 12 can be, for example, a hopper, storage bin, railcar, over-the-road trailer, or any other device that may hold or store biomass. The biomass supplied by the biomass source 12 can be in the form of solid particles. The biomass particles can be fibrous biomass materials comprising cellulose. Examples of suitable cellulose-containing materials include algae, paper waste, and/or cotton linters. In one embodiment, the biomass particles can comprise a lignocellulosic material. Examples of suitable lignocellulosic materials include forestry waste such as wood chips, saw dust, pulping waste, and tree branches; agricultural waste such as corn stover, wheat straw, and bagasse; and/or energy crops such as eucalyptus, switch grass, and coppice.
As depicted in FIG. 1, the solid biomass particles from the biomass source 12 can be supplied to a biomass feed system 14. The biomass feed system 14 can be any system capable of feeding solid particulate biomass to a biomass conversion reactor 16. While in the biomass feed system 14, the biomass material may undergo a number of pretreatments to facilitate the subsequent conversion reactions. Such pretreatments may include drying, roasting, torrefaction, demineralization, steam explosion, mechanical agitation, and/or any combination thereof.
In one embodiment, it may be desirable to combine the biomass with a catalyst in the biomass feed system 14 prior to introducing the biomass into the biomass conversion reactor 16. Alternatively, the catalyst may be introduced directly into the biomass conversion reactor 16. The catalyst may be fresh and/or regenerated catalyst. The catalyst can, for example, comprise a solid acid, such as a zeolite. Examples of suitable zeolites include ZSM-5, mordenite, beta, ferrierite, and zeolite-Y. Additionally, the catalyst may comprise a super acid. Examples of suitable super acids include sulfonated, phosphated, or fluorinated forms of zirconia, titania, alumina, silica-alumina, and/or clays. In another embodiment, the catalyst may comprise a solid base. Examples of suitable solid bases include metal oxides, metal hydroxides, and/or metal carbonates. In particular, the oxides, hydroxides, and carbonates of alkali metals, alkaline earth metals, transition metals, and/or rare earth metals are suitable. Other suitable solid bases are layered double hydroxides, mixed metal oxides, hydrotalcite, clays, and/or combinations thereof. In yet another embodiment, the catalyst can also comprise an alumina, such as alpha-alumina.
It should be noted that solid biomass materials generally contain minerals. It is recognized that some of these minerals, such as potassium carbonate, can have catalytic activity in the conversion of the biomass material.
The biomass feed system 14 introduces the biomass feedstock into a biomass conversion reactor 16. In the biomass conversion reactor 16, biomass is subjected to a conversion reaction that produces bio-oil. The biomass conversion reactor 16 can facilitate different chemical conversion reactions such as fast pyrolysis, slow pyrolysis, liquefaction, gasification, or enzymatic conversion. The biomass conversion reactor 16 can be, for example, a fluidized bed reactor, a cyclone reactor, an ablative reactor, or a riser reactor.
In one embodiment, the biomass conversion reactor 16 can be a riser reactor and the conversion reaction can be fast pyrolysis. More specifically, fast pyrolysis may include catalytic cracking. As used herein, “pyrolysis” refers to the thermochemical conversion of biomass caused by heating the feedstock in an atmosphere that is substantially free of oxygen. In one embodiment, pyrolysis is carried out in the presence of an inert gas, such as nitrogen, carbon dioxide, and/or steam. Alternatively, pyrolysis can be carried out in the presence of a reducing gas, such as hydrogen, carbon monoxide, non-condensable gases recycled from the biomass conversion process, and/or any combination thereof.
Fast pyrolysis is characterized by short residence times and rapid heating of the biomass feedstock. The residence times of the fast pyrolysis reaction can be, for example, less than 10 seconds, less than 5 seconds, or less than 2 seconds. Fast pyrolysis may occur at temperatures between 200 and 1,000° C., between 250 and 800° C., or between 300 and 600° C.
Referring again to FIG. 1, the conversion effluent 18 exiting the biomass conversion reactor 16 generally comprises gas, vapors, and solids. As used herein, the vapors produced during the conversion reaction may interchangeably be referred to as “bio-oil,” which is the common name for the vapors when condensed into their liquid state. In one embodiment of the present invention, the conversion reaction carried out in the biomass conversion reactor 16 produces a bio-oil. Such bio-oil can have an oxygen content that is less than 15, 12, 10, or 8 percent by weight of the bio-oil. The oxygen content can also be greater than about 0.5, 1, 3, or 5 percent by weight of the bio-oil.
When fast pyrolysis is carried out in the biomass conversion reactor 16, the conversion effluent 18 generally comprises solid particles of char, ash, and/or spent catalyst. The conversion effluent 18 can be introduced into a solids separator 20. The solids separator 20 can be any conventional device capable of separating solids from gas and vapors such as, for example, a cyclone separator or a gas filter. The solids separator 20 removes a substantial portion of the solids (e.g., spent catalysts, char, and/or heat carrier solids) from the conversion effluent 18. The solid particles 22 recovered in the solids separator 20 can be introduced into a regenerator 24 for regeneration, typically by combustion. After regeneration, at least a portion of the hot regenerated solids can be introduced directly into the biomass conversion reactor 16 via line 26. Alternatively or additionally, the hot regenerated solids can be directed via line 28 to the biomass feed system 14 for combination with the biomass feedstock prior to introduction into the biomass conversion reactor 16.
The substantially solids-free fluid stream 30, also referred to as bio-oil, exiting the solids separator 20 can then be introduced into a fluids separator 32. In one embodiment, it is preferred that the bio-oil 30 entering the fluids separator 32 has not previously been subjected to a deoxygenation process such as, for example, hydrotreating. The fluids separator 32 can be any system capable of separating the bio-oil 30 into at least a light fraction 34, a bio-distillate fraction 36, and a heavy fraction 38. Suitable systems to be used as the fluids separator 32 include, for example, systems for affecting separation by fractional distillation, heated distillation, extraction, membrane separation, partial condensation, and/or non-heated distillation. In some cases, it may be preferred to employ heated distillation to affect separation, where such heated distillation raises the temperature of the bio-oil 30 above 100° C. As shown in FIG. 1, non-condensable gases 40 may be removed from the fluids separator 32 and, optionally, recycled via line 42 to the biomass conversion reactor 16 for use as a lift gas.
The light fraction 34 exiting fluids separator 32 can have a boiling range comparable to petroleum-derived gasoline. The bio-distillate fraction 36 exiting fluids separator 32 can have a boiling range comparable to petroleum-derived distillates.
The boiling range of the bio-distillate fraction 36 can be such that at least 75, 85, 95, or 100 weight percent of the bio-distillate fraction 36 boils at a temperature between about 180° C. and about 380° C., between about 190° C. and about 370° C., or between about 205° C. and about 355° C. The boiling range of the heavy fraction 38 can be such that at least 75, 85, 95, or 100 weight percent of the heavy fraction 38 boils at a temperature greater than 380° C., 370° C., or 355° C. The boiling range of the light fraction 34 can be such that at least 75, 85, 95, or 100 weight percent of the light fraction 34 boils at a temperature less than about 205° C., 190° C., or 180° C.
In one embodiment, at least 5, 15, 25, or 35 weight percent of the bio-oil 30 entering the fluids separator 32 is separated into the bio-distillate fraction 36. In another embodiment at least 10, 20, or 30 weight percent of the bio-oil 30 entering the fluids separator 32 is separated into the light fraction 34, and less than 60 weight percent of the bio-oil 30 subjected to separation is separated into the heavy fraction 38.
Bio-Distillate Fraction/Composition
The bio-distillate fraction 36 can have an oxygen content that is less than 15, 12, 10, 8 and/or greater than about 0.5, 1, or 4 weight percent. The bio-distillate fraction, which can also be referred to as a bio-distillate composition, can comprise at least about 40 or 50 weight percent oxygen-free hydrocarbons, and can have less than about 1 or 0.5 weight percent carbonyls, and can have less than about 0.5 or 0.2 weight percent carboxylic acid.
The bio-distillate fraction can have less than about 0.5 or less than about 0.2 weight percent aldehydes, and can further comprise between about 10 and about 40, or between about 20 and about 40 weight percent oxygen-and-carbon-containing compounds. The oxygen-and-carbon-containing compounds can be selected from the group consisting of phenolics, furans, ketones, aldehydes, and mixtures thereof.
The bio-distillate fraction/composition preferably has a copper corrosion test value of less than No. 3.
Renewable Distillate
As illustrated in FIG. 1, biomass production system 10 can be located near or connected by a transportation system with a petroleum-derived distillate source 44. Petroleum-derived distillate source 44 can be, for example, a petroleum refinery, a petroleum fuel storage facility, and/or a petroleum fuel transportation system.
A distillate blending system 46 can be used to combine a petroleum-derived distillate-range stream 48, which can have between 12 and 25 carbon atoms per molecule, from petroleum-derived distillate source 44 with at least a portion of the bio-distillate fraction 36 and a stabilizing additive 50 to thereby produce a renewable distillate composition 52 having a single clear phase.
The renewable distillate composition can comprise the petroleum-derived-distillate-range stream 48 in an amount of at least 5, 15, or 25 weight percent and/or at most 99, 98, or 96 weight percent; the bio-distillate fraction 36 in an amount of at least 0.5, 2, 5, 25, or 60 weight percent, and the stabilizing additive having surfactant properties in an amount between about 0.5 and about 25 weight percent.
The stabilizing additive can comprise a material selected from the group consisting of: 1) a non-ionic block-copolymer having a Hydrophile-Lipophile Balance (HLB) of at most eight, seven, or six and/or at least two or three; 2) a non-ionic homopolymer having an HLB of at most eight, seven, or six and/or at least two or three, 3) a mixture of a non-ionic block-copolymer and a non-ionic homopolymer having an average HLB of at most eight, seven, or six and/or at least two or three; 4) a non-ionic surfactant having an HLB of at most eight, seven, or six and/or at least two or three, 5) a Fatty Acid Methyl Ester (FAME), or 6) a combination thereof. Examples of stabilizing additives include, but are not limited to, Hypermer series polymers, Brij series surfactants, Propylene Glycol Isostereate, Span series surfactants, Glycol Stearate, Sorbitan Sesquioleate, Glyceryl Stearate, Lecithin series surfactants, Sorbitan Oleate, Sorbitan Monostearate NF, Sorbitan Stearate, Sorbitan Iso stearate, Steareth-2, 0leth-2, Glyceryl Laurate, Ceteth-2, PEG series polymer surfactants, Dipolyhydroxystearate, Glyceryl Stearate SE, Methyl Glucose Sesquistearate, Atsurf series surfactants, and mixtures thereof.
Among other choices, the petroleum-derived-distillate-range stream can be selected from the group consisting of a regular distillate, low sulfur distillate, hydroprocessed light cycle oil, hydrotreated straight run gas oil, ultra low sulfur distillate, refinery processed middle distillate, or mixtures thereof.
In cases wherein the stabilizing additive which is used comprises non-ionic surfactant, non-ionic block-copolymer, or non-ionic homopolymer, or a mixture of non-ionic block-copolymer and the non-ionic homopolymer; for ease of processing it is preferred to either simultaneously or sequentially add the stabilizing additive and the bio-distillate fraction to the petroleum-derived-distillate-range stream, thereby forming the renewable distillate.
In cases wherein the stabilizing additive comprises a FAME; it has been discovered that a significant operational advantage is achieved by combining the bio-distillate fraction with the stabilizing additive prior to combination of the two components with the petroleum-derived-distillate-range stream, thereby forming the renewable distillate.
Bio-Oil Upgrading
FIGS. 2-5 depict bio-oil upgrading systems that each include a preheater, a hydrodeoxygenation unit and a product separator.
It should be understood that the bio-oil upgrading systems shown in FIGS. 2-5 are just examples and embodiments of systems within which the present invention can be embodied. The present invention may find application in a wide variety of other systems where it is desirable to efficiently and effectively upgrade bio-oil.
The bio-oil useful in the following embodiments can comprise oxygenated hydrocarbons and can have a total oxygen content greater than about 5, or greater than about 8, or greater than about 10 wt %.
The hydrodeoxygenation unit useful in the following embodiments can be operated at a temperature in the range of from about 300 to about 500° C., or from about 320 to about 450° C., or from about 350 to about 420° C.
In accordance with the bio-oil upgrading system 20 of FIG. 2, the bio-oil is combined with a diluent via lines 202 and 204 thereby forming a feed stream. The feed stream is charged to a preheater 206 via line 202 wherein the feed stream is heated to a temperature in the range of from about 20 to about 450° C., or from about 80 to about 430° C., or from about 100 to about 400° C.; thereby forming a heated feed stream.
The heated feed stream is charged to a hydrodeoxygenation unit 208 via line 210 wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil. The effluent stream is charged to a separator 212 via line 214 wherein at least a portion of the at least partially upgraded bio-oil is separated from the effluent stream thereby forming a product stream 216 comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil. The at least partially upgraded bio-oil can have a total oxygen content less than about 15, or less than about 10, or less than about 8, or less than about 6, or less than about 4 wt %. The product stream can further comprise at least a portion of the diluent. A water-containing stream is also formed and removed from separator 212 via line 218.
A portion of the oxygenated hydrocarbons in the feed stream 202 react with each other in the preheater 206 or the hydrodeoxygenation unit 208 or both the preheater 206 and the hydrodeoxygenation unit 208 forming heavier compounds which are deposited in the preheater 206 or the hydrodeoxygenation unit 208 or both the preheater 206 and the hydrodeoxygenation unit 208. Further, the total amount of heavier compounds deposited in the preheater 206 and in the hydrodeoxygenation unit 208 is less than the total amount of heavier compounds deposited in the preheater 206 and the hydrodeoxygenation unit 208 when the feed stream 202 does not contain the diluent. In addition, the diluent provides dilution of the bio-oil in the preheater 206 and the hydrodeoxygenation unit 208 which slows the reaction of the oxygenated hydrocarbons in the feed stream 202 with each other, minimizing or preventing buildup of carbonaceous deposits in the preheater 206 or in the hydrodeoxygenation unit 208 or both the preheater 206 and the hydrodeoxygenation unit 208.
The diluent can be present in the feed stream 202 in an amount of about 0.5 to about 50, or from about 2 to about 45, or from about 5 to about 40 wt %. The diluent can be any material capable of serving as a diluent for a bio-oil feed. More particularly, the diluent can be a renewable diluent selected from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, a recycled portion of the at least partially upgraded bio-oil described above, and combinations thereof.
The temperature of the upgraded bio-oil is generally higher than the temperature of the bio-oil. When the diluent comprises a FAME and a portion of the at least partially upgraded bio-oil, the inclusion of the at least partially upgraded bio-oil in the feed stream 202 provides heat to the feed stream 202 thereby reducing the required heat duty of the preheater 206, reducing the heated surface temperatures of the preheater 206, and slowing the reaction of the oxygenated hydrocarbons in the feed stream 202 with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 206 or the hydrodeoxygenation unit 208 or both the preheater 206 and the hydrodeoxygenation unit 208.
In accordance with the bio-oil upgrading system 30 of FIG. 3, the bio-oil is combined with a diluent via lines 302 and 304 thereby forming a feed stream. The diluent can be present in the feed stream 302 in an amount of about 0.5 to about 50, or from about 2 to about 45, or from about 5 to about 40 wt %.
The feed stream is charged to a preheater 306 via line 302 wherein the feed stream is heated to a temperature in the range of from about 20 to about 450° C., or from about 80 to about 430° C., or from about 100 to about 400° C.; thereby forming a heated feed stream. The heated feed stream is charged to a hydrodeoxygenation unit 308 comprising at least two stages via line 309 wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream represented by line 310 comprising partially hydrodeoxygenated bio-oil and an effluent stream 312 comprising the diluent, water, and an at least partially upgraded bio-oil. The at least partially upgraded bio-oil can have a total oxygen content less than about 15, or less than about 10, or less than about 8, or less than about 6, or less than about 4 wt %. The effluent stream is charged to a separator 314 wherein at least a portion of the at least partially upgraded bio-oil is separated from the effluent stream thereby forming a product stream 316 comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil, wherein the at least one inter-stage stream 310 and the product stream 316 are each at a higher temperature than the bio-oil. The product stream can further comprise at least a portion of the diluent. A water-containing stream is also formed and removed from separator 314 via line 318.
Also, a portion of at least one of: i) the at least one inter-stage stream 310, and ii) the product stream 316 are recycled via lines 310, 311, and 316, 317, respectively, to become at least a part of the diluent combined with the bio-oil via line 304.
The diluent can further comprise any material capable of serving as a diluent for a bio-oil feed. More particularly, the diluent can further comprise a component selected from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, and combinations thereof.
A portion of the oxygenated hydrocarbons react with each other in the preheater 306 or the hydrodeoxygenation unit 308 or both the preheater 306 and the hydrodeoxygenation unit 308 forming heavier compounds which are deposited in the preheater 306 or the hydrodeoxygenation unit 308 or both the preheater 306 and the hydrodeoxygenation unit 308. Further, the total amount of heavier compounds deposited in the preheater 306 and the hydrodeoxygenation unit 308 is less than the total amount of heavier compounds deposited in the preheater 306 and the hydrodeoxygenation unit 308 when the feed stream 302 does not contain the diluent. In addition, the diluent provides dilution of the bio-oil in the preheater 306 and the hydrodeoxygenation unit 308 which slows the reaction of the oxygenated hydrocarbons in the feed stream 302 with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 306 or the hydrodeoxygenation unit 308 or both the preheater 306 and the hydrodeoxygenation unit 308.
The inclusion of the recycle stream in the feed stream 302 provides heat to the feed stream 302 thereby reducing the required heat duty of the preheater 306, reducing the heated surface temperatures of the preheater 306, and slowing the reaction of the oxygenated hydrocarbons in the feed stream 302 with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 306 or the hydrodeoxygenation unit 308 or both the preheater 306 and the hydrodeoxygenation unit 308.
In accordance with the bio-oil upgrading system 40 of FIG. 4, the bio-oil is combined with a diluent via lines 402 and 404 thereby forming a first feed stream. The first feed stream is charged to a preheater 406 via line 402 and is heated to a temperature in the range of from about 20 to about 100, or from about 30 to about 90, or from about 40 to about 80° C., thereby forming a heated first feed stream. A recycle stream is combined with the heated first feed stream via lines 408 and 410 thereby forming a second feed stream having a temperature in the range of from about 20 to about 450° C., or from about 80 to about 430° C., or from about 100 to about 400° C. The recycle stream can have a temperature of from about 100 to about 460, or from about 200 to about 430, or from about 250 to about 420° C.
The second feed stream is charged to a hydrodeoxygenation unit 412 comprising at least two stages via line 408 wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream represented by line 414 comprising partially hydrodeoxygenated bio-oil and an effluent stream 416 comprising the diluent, water, and an at least partially upgraded bio-oil. The at least partially upgraded bio-oil can have a total oxygen content less than about 15, or less than about 10, or less than about 8, or less than about 6, or less than about 4 wt %.
The effluent stream 416 is charged to a separator 418 wherein at least a portion of the at least partially upgraded bio-oil is separated from the effluent stream 416 thereby forming a product stream 420 comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil. The product stream 420 can further comprise at least a portion of the diluent. A water-containing stream is also formed and removed from separator 418 via line 422. The at least one inter-stage stream 414 and the product stream 420 are each at a higher temperature than the bio-oil.
Also, a portion of at least one of: i) the at least one inter-stage stream 414, and ii) the product stream 420 are recycled via lines 414, 415, and 420, 421, respectively, as the recycle stream for combination with the heated first feed stream via line 410 thereby forming the second feed stream.
The preheater 406 provides from greater than 0 to about 30, or from greater than about 5 to about 25% of the heat needed to raise the temperature of the second feed stream to a temperature in the range of from about 20 to about 450, or from about 80 to about 430, or from about 100 to about 400° C.
The diluent can be any material capable of serving as a diluent for a bio-oil feed. More particularly, the diluent can comprise a component selected from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, and combinations thereof.
A portion of the oxygenated hydrocarbons react with each other in the preheater 406 or the hydrodeoxygenation unit 412 or both the preheater 406 and the hydrodeoxygenation unit 412 forming heavier compounds which are deposited in the preheater 406 or the hydrodeoxygenation unit 412 or both the preheater 406 and the hydrodeoxygenation unit 412. Further, the total amount of heavier compounds deposited in the preheater 406 and the hydrodeoxygenation unit 412 is less than the total amount of heavier compounds deposited in the preheater 406 and the hydrodeoxygenation unit 412 when the diluent and the recycle stream are not combined with the bio-oil. In addition, the diluent provides dilution of the bio-oil in the hydrodeoxygenation unit 412, and in the preheater 406, which slows the reaction of the oxygenated hydrocarbons with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 406 or the hydrodeoxygenation unit 412 or both the preheater 406 and the hydrodeoxygenation unit 412.
The combination of the recycle stream with the heated first feed stream provides heat to the second feed stream thereby reducing the required heat duty of the preheater 406, reducing the heated surface temperatures of the preheater 406, and slowing the reaction of the oxygenated hydrocarbons with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 406 or the hydrodeoxygenation unit 412 or both the preheater 406 and the hydrodeoxygenation unit 412.
The combined total of the diluent and the recycle stream in the second feed stream can be from about 0.5 to about 50, or from about 2 to about 45, or from about 5 to about 40 wt %.
In accordance with the bio-oil upgrading system 50 of FIG. 5, the bio-oil is combined with a diluent via lines 502 and 504 thereby forming a feed stream. A portion of the feed stream is charged as a preheater feed stream to a preheater 506 and heated to a temperature in the range of from about 20 to about 450° C., or from about 80 to about 430° C., or from about 100 to about 400° C. in the preheater 506 thereby forming a heated feed stream.
The heated feed stream is charged to a hydrodeoxygenation unit 508 comprising at least two stages via line 509 wherein at least a portion of the oxygen is removed from the oxygenated hydrocarbons of the bio-oil thereby forming at least one inter-stage stream represented by line 510 comprising partially hydrodeoxygenated bio-oil and an effluent stream 512 comprising the diluent, water, and an at least partially upgraded bio-oil. The at least partially upgraded bio-oil can have a total oxygen content less than about 15, or less than about 10, or less than about 8, or less than about 6, or less than about 4 wt %.
A portion of the feed stream is also charged via line 513 as a quench to at least one of the inter-stage streams 510 to thereby form a quenched inter-stage stream(s) represented by line 514 which can control the temperature of the downstream stages.
The effluent stream 512 is charged to a separator 516 wherein at least a portion of the at least partially upgraded bio-oil is separated from the effluent stream 512 thereby forming a product stream 518 comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil.
The product stream can further comprise at least a portion of the diluent. A water-containing stream is also formed and removed from separator 516 via line 517.
A portion of the oxygenated hydrocarbons react with each other in the preheater 506 or the hydrodeoxygenation unit 508 or both the preheater 506 and the hydrodeoxygenation unit 508 forming heavier compounds which are deposited in the preheater 506 or the hydrodeoxygenation unit 508 or both the preheater 506 and the hydrodeoxygenation unit 508. Further, the total amount of heavier compounds deposited in the preheater 506 and in the hydrodeoxygenation unit 508 is less than the total amount of heavier compounds deposited in the preheater 506 and the hydrodeoxygenation unit 508 when the feed stream does not contain the diluent. In addition, the diluent provides dilution of the bio-oil in the preheater 506 and the hydrodeoxygenation unit 508 which slows the reaction of the oxygenated hydrocarbons in the feed stream with each other minimizing or preventing buildup of carbonaceous deposits in the preheater 506 or the hydrodeoxygenation unit 508 or both the preheater 506 and the hydrodeoxygenation unit 508.
The diluent can be present in the feed stream in an amount of about 0.5 to about 50, or from about 2 to about 45, or from about 5 to about 40 wt %. The diluent can be any material capable of serving as a diluent for a bio-oil feed. More particularly, the diluent can be a renewable diluent selected from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, a recycle stream selected from the group consisting of: i) at least one of the inter-stage streams 510, ii) at least one of the quenched inter-stage streams 514, and iii) the product stream 518, and combinations thereof. Also, the temperature of the recycle stream is higher than the temperature of the bio-oil. The at least one inter-stage stream 510 can be recycled for use as at least a portion of the diluent via lines 510 and 511. The at least one quenched inter-stage stream 514 can be recycled for use as at least a portion of the diluent via lines 514 and 515. The product stream 518 can be recycled for use as at least a portion of the diluent via lines 518 and 519.
When the diluent comprises a FAME and the recycle stream, the inclusion of the recycle stream in the diluent provides heat to the feed stream thereby reducing the required heat duty of the preheater, reducing the heated surface temperatures of the preheater, and slowing the reaction of the oxygenated hydrocarbons with each other in the feed stream minimizing or preventing buildup of carbonaceous deposits in the preheater 506 or the hydrodeoxygenation unit 508 or both the preheater 506 and the hydrodeoxygenation unit 508.
EXAMPLES
Example 1
A low oxygen bio-oil was produced from the conversion of southern yellow pine wood particles by pyrolysis in the presence of a catalyst in a riser reactor operated at a reactor outlet temperature of about 650° C. The resulting bio-oil had an oxygen content of about 12 weight percent, and was distilled to yield more than 25 weight percent of a bio-diesel fraction boiling in the range of less than about 345° C. The composition of the bio-distillate fraction is shown below in Table 1.









TABLE 1







wt % in bio-



distillate



















Cyclics/




Aromatics



Cyclic dienes
0.00



BTEX
0.46



Other 1-Ring
0.12



Aromatics



Indanes/Indenes
6.45



Naphthalenes
53.07



3-Ring
2.60



4-Ring
0.00



5-Ring
0.00



6-Ring
0.00



Total
62.70



Nitrogen



Compounds



Indazoles
0.00



Oxygenates



Alcohols
0.00



Ethers
0.98



Carboxylic
0.00



Acids



Aldehydes
0.00



Ketones
0.32



Phenols
7.96



Diols
7.72



Indenols
3.09



BenzoFurans
3.86



Naphthols
13.37



Levoglucosan
0.00



Total
37.30



Total [0] (%)
11.21










As can be seen from the data, the bio-distillate fraction is of high quality, having a low oxygen content, undetectable carboxylic acids, and significant amounts of cyclic/aromatics.
Example 2
A quantity of Hypermer B241 polymer was blended with commercially available Ultra Low Sulfur Diesel (ULSD) to form a first mixture, which was then combined with a quantity of the bio-distillate fraction from Example 1 to form a renewable distillate blend containing 97 weight percent ULSD, 1 weight percent Hypermer B241, and 2 weight percent bio-distillate. Following mixing using an ultra sonic homogenizer, the renewable distillate blend was a single clear phase.
Example 3
Different quantities of a FAME were blended with quantities of the bio-distillate fraction from Example 1 to form mixtures, which were then combined with quantities of ULSD to form renewable distillate blends which were mixed with an ultra sonic homogenizer. Single clear phases were obtained for all of the blends shown in Table 2 below.









TABLE 2





Bio-Distillate, wt. %
FAME, wt. %
ULSD, wt. %

















0.5
0.5
99.0


1.0
1.0
98.0


1.5
1.5
97.0


2.0
2.0
96.0


2.5
2.5
95.0


18.8
6.2
75.0


12.5
12.5
75.0


20.0
5.0
75.0


21.2
3.8
75.0


25.0
25.0
50.0


37.5
12.5
50.0


40.0
10.0
50.0


42.5
7.5
50.0


45.0
5.0
50.0


47.5
2.5
50.0


60.0
15.0
25.0


63.7
11.3
25.0


67.5
7.5
25.0


71.2
3.8
25.0









Example 4
Quantities of the bio-distillate fraction from Example 1 were blended with ULSD to form a blend of 2% bio-distillate (BD), using 1 wt % Hypermer B246 polymer material, with an HLB of 6; and to form another blend of 40% bio-distillate (BD) using 2.5 wt % FAME acquired from the company Houston Biodiesel located in Houston, Tex. The ULSD and the various blends were tested for various properties/components. The results of such tests are reflected in Table 3 below. Table 3 also includes the specified values of those properties for two types of distillate petroleum products, diesel #2 S500 (D2 S500) and fuel oil #2 (FO#2). The resulting blends were observed to be clear and stable and the blends met the conventional distillate specifications.













TABLE 3






Test
D2 S500

2%
FO#2
40%


Property
Method
Specs
ULSD
BD
Specs
BD





















Kinematic viscosity, mm2/sec 40° C.,








Min
D445
1.9
2.70
2.53
1.9


max

4.1


3.4


Density, (kg/m3 @15° C.), max
D1298



876
922


Ramsbottom carbon residue on
D524


0.14
0.15
0.17


10% distillation residue, wt %, max


Flash Point, ° C., min
D93
52
60
65
38
71.6


Pour Point, ° C., max



−27
−6
−21


Distillation, ° C., v % recovered, T90


Min
D86
282
320
314
282
314


Max

338


338


Water and Sediment, v %, max
D2709
0.05
0
0
0.05
0


Ash wt %, max
D482
0.01

<10−3

<10−3


Copper Strip Corrosion, max
D130
No. 3

No. 1
No. 3
No. 1


Sulfur, ppm
D97
500
0.05

1000
25


Cetane number: one of the following:


(A) Cetane Index, min.
D613
40
44.5


OR


(B) (1) Cetane Index, min.
D76
40
46.3
45


(2) Aromaticity, % vol, max
D1319
35
28.2
25.2

28.5


Lubricity, HFRR @ 60° C., micron,
D6079
520
260
260


max


Conductivity, pS/m, max
D2624
25
~10−4
<1


Other properties


Relative Density @ 60/60° F.





923


PNA Aromatics
D1319

28.2


28.5


Olefins


2.2


1.8


Parafins


69.6


69.7









As can be seen from Table 3 above, the properties of the renewable distillate made by blending bio-distillate, Additive and ULSD fall within the specifications for distillate fuels. The renewable distillate containing 2 wt % biodiesel met specifications for Diesel #2-S500, while the renewable distillate containing 40% biodiesel met Fuel Oil #2 specifications (other than density and Ramsbottom carbon for the 40% BD blend).
Example 5
A low oxygen bio-oil (BO-16) was produced from the conversion of southern yellow pine wood particles by pyrolysis in the presence of a catalyst in a riser reactor operated at a reactor outlet temperature of about 650° C. The resulting bio-oil had an oxygen content of 16.64 weight percent. The composition (in wt %) of the bio-oil is shown below in Table 4.









TABLE 4







BO-16



















Aldehydes
3.5729



Furans
2.0658



Ketones
5.6386



Carboxylic Acids
1.4571



Phenols
12.994



Indenols
1.5968



Diols
4.7505



Naphthols
0.8184



Hydrocarbons:



BTEX
3.1836



Other PAHs
0.529



Other Benzenes/Toluenes
1.1576



Indenes
1.3873



Indanes
0.1297



Naphthalenes
0.8483



Volatiles + Semivolatiles
40.18



Non-volatiles
59.82










Three separate portions of the bio-oil BO-16 were combined with FAME forming a BF5 blend containing 5 wt % FAME, a BF10 blend containing 10 wt % FAME, and a BF15 blend containing 15 wt % FAME. The thermal stabilities of the bio-oil, BF5, BF10, and BF15 were assessed based on changes in viscosity using an accelerated thermal stability test based on the observations of Czernik et al. as reported in Czernik, S.; Johnson, D. K. and Black, S. Stability of wood fast pyrolysis oil. Biomass and Bioenergy 1994. 7 (1-6), 187-192. Czernik et al. illustrates that viscosity changes for bio-oil stored 12 weeks at 37° C. corresponds to 6 hours at 90° C. and, hence, that viscosity changes for bio-oil stored 1 year at 37° C. corresponds to 24 hours at 90° C. The accelerated thermal stability test used for the bio-oil, BF5, BF10, and BF15 samples in this example comprised heating the samples to 90° C. and holding the samples at that temperature for up to 48 hours. The viscosity was measured using a modified version of ASTM D2983 using a higher temperature than standard due to the high viscosity of bio-oil at low temperature. Viscosity was measured at 40° C. using a Brookfield viscometer. The accelerated aging test correlates well with the chemical changes in the liquid, associated with polymerization or condensation reactions. (See also, Oasmaa, A. and Kuoppala, E. Fast pyrolysis of forestry residue. 3. Storage stability of liquid fuel. Energy and Fuels 2003, 17 (4), 1075-85.) The results of the thermal stability test (expressed as a “Stability Parameter”—SP—which represents the change in viscosity in centipoises (cp) per unit time in hours (h), having the units cp/h and was evaluated as the slope of a plot of viscosity vs. time) are shown in Table 5 below. As can be seen from the data, the SP for the bio-oil/FAME blends BF5, BF10 and BF15 was significantly reduced as compared to the virgin bio-oil.












TABLE 5







Sample
[FAME], wt %
[O], wt %
SP, cp/h





















Bio-oil
0
16.64
0.2372



BF5
5
15.19
0.0997



BF10
10
15.60
0.0685



BF15
15
15.27
0.0359










Example 6
Two different O-containing bio-oil samples were tested in this example. BO-16 and BO-21 are bio-oil samples with 16 wt % and 21 wt % O-content, respectively. Separate portions of each bio-oil were combined with FAME forming blends containing different proportions of each of these components. Light scattering was used to assess the phase segregation stability of these blends using a Turbiscan MA2000 instrument. Turbiscan is an instrument for measuring light scattering in fluids. This system couples light scattering with a scan of the sample length to give a picture of its homogeneity or changes in homogeneity. The overlay of several scans over time enables stability analysis of the sample from 20 to 50 times faster than visual detection. The detected stability during a 16 h scanning experiment is a measure of the fouling propensity of the blend.







TABLE 6







Turbiscan assessed stability













FAME,
Back-scattering Intensity




Bio-oil
wt %
Slope Change (%/hr)
Remarks
















BO-16
0
0.0
Stable




5
0.0
Stable




10
0.0
Stable




15
0.0
Stable




25
0.0
Stable




30
0.0
Stable




40
−0.02
Unstable




90
−1.2
Unstable



BO-21
5
0.0
Stable




10
0.0
Stable




15
0.0
Stable




20
0.0
Stable




25
0.0
Stable




30
−0.1
Unstable




40
−0.3
Unstable




50
−0.9
Unstable




75
−3.0
Unstable




90
−9.0
Unstable










As can be seen, the lower the O-content of the bio-oil, the higher the miscible FAME content to render stable solutions.
The preferred forms of the invention described above are to be used as illustration only, and should not be used in a limiting sense to interpret the scope of the present invention. Modifications to the exemplary embodiments, set forth above, could be readily made by those skilled in the art without departing from the spirit of the present invention.
It is the inventors' intent to rely on the Doctrine of Equivalents to determine and assess the reasonably fair scope of the present invention as it pertains to any processes and systems not materially departing from but outside the literal scope of the invention as set forth in the following claims.

## Claims

1. A process for upgrading bio-oil, comprising:
a) combining a bio-oil and a diluent to form a feed stream, the bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt %;
b) charging the feed stream to a preheater and heating the feed stream to a temperature in a range of from about 20 to about 450° C., thereby forming a heated feed stream;
c) charging the heated feed stream to a hydrodeoxygenation unit operated at a temperature in a range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the bio-oil, thereby forming an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil; and
d) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream, thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil,
wherein the diluent is: (i) present in the feed stream in an amount ranging from about 0.5 to about 24.5 wt %; and (ii) selectred from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, a recycled portion of the at least partially upgraded bio-oil, and combinations thereof.

2. The process of claim 1, wherein a portion of the oxygenated hydrocarbons in the feed stream react with each other in at least one of the preheater and the hydrodeoxygenation unit, thereby forming heavier compounds which are deposited in at least one of the preheater and the hydrodeoxygenation unit; and wherein the total amount of heavier compounds deposited in the preheater and in the hydrodeoxygenation unit is less than the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit when the feed stream does not contain the diluent.

3. The process of claim 2, wherein the diluent dilutes the bio-oil in the preheater and the hydrodeoxygenation unit, thereby slowing the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

4. The process of claim 2, wherein the temperature of the upgraded bio-oil is higher than the temperature of the bio-oil, and wherein the diluent comprises a FAME and a portion of the at least partially upgraded bio-oil; and wherein the inclusion of the at least partially upgraded bio-oil in the feed stream provides heat to the feed stream, thereby: reducing the required heat duty of the preheater, reducing the heated surface temperatures of the preheater, and slowing the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

5. The process of claim 1, wherein the diluent is present in the feed stream in an amount ranging from about 0.5 to about 10 wt %.

6. The process of claim 1, wherein the product stream further comprises at least a portion of the diluent.

7. A process for upgrading bio-oil, comprising:
a) combining a bio-oil and a diluent to form a feed stream, the bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt %;
b) charging the feed stream to a preheater and heating the feed stream to a temperature in a range of from about 20 to about 450° C., thereby forming a heated feed stream;
c) charging the heated feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in a range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the bio-oil, thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
d) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream, thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil, wherein the at least one inter-stage stream and the product stream are each at a higher temperature than the bio-oil; and
e) utilizing as the diluent at least one of (I) a recycle stream comprising a portion of at least one of: i) the at least one inter-stage stream, and ii) the product stream; (II) a fatty acid methyl ester (FAME); (Ill) biodiesel; and (IV) biomass-derived diesel, and wherein the diluent is present in the feed stream in an amount ranging from about 0.5 to 24.5 wt %.

8. The process of claim 7, wherein the product stream further comprises at least a portion of the diluent.

9. The process of claim 7, wherein a portion of the oxygenated hydrocarbons react with each other in at least one of the preheater and the hydrodeoxygenation unit forming heavier compounds which are deposited in at least one of the preheater and the hydrodeoxygenation unit; and wherein the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit is less than the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit when the feed stream does not contain the diluent.

10. The process of claim 9, wherein the diluent dilutes the bio-oil in the preheater and the hydrodeoxygenation unit, which slows the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the build up of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

11. The process of claim 9, wherein the inclusion of the recycle stream in the feed stream provides heat to the feed stream, thereby: reducing the required heat duty of the preheater, reducing the heated surface temperatures of the preheater, and slowing the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the build up of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

12. The process of claim 7, wherein the diluent is present in the feed stream in an amount from about 0.5 to about 10 wt %.

13. A process for upgrading bio-oil, comprising:
a) combining a bio-oil and a diluent to form a first feed stream, the bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt %, wherein the diluent is selected from the group consisting of a fatty acid methyl ester (FAME), biodiesel, biomass-derived diesel, and combinations thereof;
b) charging the first feed stream to a preheater and heating the first feed stream to a temperature in a range of from about 20 to about 100° C., thereby forming a heated first feed stream;
c) combining a recycle stream having a temperature of from about 100 to about 460° C. with the heated first feed stream thereby forming a second feed stream having a temperature in the range of from about 20 to about 450° C., wherein the combined total of the diluent and the recycle stream in the second feed stream is in an amount ranging from about 0.5 to about 24.5 wt %;
d) charging the second feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in a range of from about 300 to about 500° C. wherein at least a portion of the oxygen is removed from the bio-oil, thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
e) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream, thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil, wherein the at least one inter-stage stream and the product stream are each at a higher temperature than the bio-oil; and
f) utilizing as the recycle stream a portion of at least one of: i) the at least one inter-stage stream, and ii) the product stream.

14. The process of claim 13, wherein the preheater provides from greater than 0 to about 30 % of the heat needed to raise the temperature of the second feed stream to a temperature in the range of from about 20 to about 450° C.

15. The process of claim 13, wherein the product stream further comprises at least a portion of the diluent.

16. The process of claim 13, wherein a portion of the oxygenated hydrocarbons react with each other in at least one of the preheater and the hydrodeoxygenation unit, thereby forming heavier compounds which are deposited in at least one of the preheater and the hydrodeoxygenation unit; and wherein the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit is less than the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit when the diluent and the recycle stream are not combined with the bio-oil.

17. The process of claim 16, wherein the diluent dilutes the bio-oil in the hydrodeoxygenation unit and the preheater, which slows the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

18. The process of claim 13, wherein the combination of the recycle stream and the heated first feed stream provides heat to the second feed stream, thereby: reducing the required heat duty of the preheater, reducing the heated surface temperatures of the preheater, and slowing the reaction of the oxygenated hydrocarbons with each other such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

19. The process of claim 13, wherein the combined total of the diluent and the recycle stream in the second feed stream is from about 0.5 to about 10 wt %.

20. A process for upgrading bio-oil, comprising:
a) combining a bio-oil and a diluent to form a feed stream, the bio-oil comprising oxygenated hydrocarbons and having a total oxygen content greater than about 5 wt %;
b) charging a portion of the feed stream as a preheater feed stream to a preheater and heating the preheater feed stream to a temperature in a range of from about 20 to about 450° C., thereby forming a heated feed stream;
c) charging the heated feed stream to a hydrodeoxygenation unit comprising at least two stages and operated at a temperature in a range of from about 300 to about 500° C., wherein at least a portion of the oxygen is removed from the bio-oil, thereby forming at least one inter-stage stream comprising partially hydrodeoxygenated bio-oil and an effluent stream comprising the diluent, water, and an at least partially upgraded bio-oil;
d) charging a portion of the feed stream as a quench to at least one of the inter-stage streams to form a quenched inter-stage stream and control the temperature of the downstream stages; and
e) separating at least a portion of the at least partially upgraded bio-oil from the effluent stream, thereby forming a product stream comprising the at least partially upgraded bio-oil having a total oxygen content lower than the total oxygen content of the bio-oil,
wherein the diluent is (I) present in the feed stream in an amount ranging from about 0.5 to 24.5 wt %; and (II) selected from the group consisting of (i) a fatty acid methyl ester (FAME), (ii) biodiesel, (iii) biomass-derived diesel, (iv) a recycle stream selected from the group consisting of: at least one of the inter-stage streams, at least one of the quenched inter-stage streams, the product stream, and combinations thereof, and (v) combinations thereof.

21. The process of claim 20, wherein a portion of the oxygenated hydrocarbons react with each other in at least one of the preheater and the hydrodeoxygenation unit, thereby forming heavier compounds which are deposited in at least one of the preheater and the hydrodeoxygenation unit; and wherein the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit is less than the total amount of heavier compounds deposited in the preheater and the hydrodeoxygenation unit when the feed stream does not contain the diluent.

22. The process of claim 21, wherein the diluent dilutes the bio-oil in the preheater and the hydrodeoxygenation unit, which slows the reaction of the oxygenated hydrocarbons in the feed stream with each other such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

23. The process of claim 20, wherein the diluent is present in the feed stream in an amount of from about 0.5 to about 10 wt %.

24. The process of claim 20, wherein the temperature of the recycle stream is higher than the temperature of the bio-oil, and wherein the diluent comprises a FAME and the recycle stream; and wherein the inclusion of the recycle stream in the diluent provides heat to the feed stream, thereby: reducing the required heat duty of the preheater, reducing the heated surface temperatures of the preheater, and slowing the reaction of the oxygenated hydrocarbons with each other in the feed stream such that the buildup of carbonaceous deposits in at least one of the preheater and the hydrodeoxygenation unit is minimized or prevented.

25. The process of claim 20, wherein the product stream further comprises at least a portion of the diluent.