US20130327627A1

US20130327627A1 - Catalytic biomass pyrolysis in an auger reactor

Info

Publication number: US20130327627A1
Application number: US13/914,338
Authority: US
Inventors: Daren E. DAUGAARD; Samuel T. Jones; Alexandru PLATON; Kening GONG; Edgar Lotero
Original assignee: Phillips 66 Co
Current assignee: Phillips 66 Co
Priority date: 2012-06-12
Filing date: 2013-06-10
Publication date: 2013-12-12
Also published as: WO2013188404A2; WO2013188515A1; WO2013188404A3

Abstract

The present invention relates generally to the thermal conversion of biomass. Processes are disclosed for converting biomass to condensable vapor intermediates such as pyrolysis oil by means of catalytic pyrolysis in a reactor comprising at least one auger, where the catalyst also comprises a heat carrier. The intermediates produced may be further processed for production of renewable hydrocarbon fuels.

Description

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a non-provisional application which claims benefit under 35 USC §119(e) to U.S. Provisional Application Ser. No. 61/658,513 filed Jun. 12, 2012, entitled CATALYTIC BIOMASS PYROLYSIS IN AN AUGER REACTOR, which is incorporated herein in its entirety.

STATEMENT OF FEDERALLY SPONSORED RESEARCH

None.

FIELD OF THE DISCLOSURE

The present invention relates generally to pyrolytic conversion of biomass in the presence of a catalyst and a heat carrier in a reactor comprising at least one auger.

BACKGROUND

The Renewable Fuels Standards (RFS) enacted by the US Government mandate the increased use of renewable energy sources to reduce emissions of carbon based fuels and provide alternatives to petroleum based energy and feedstock.
One of the alternatives being explored is the use of biomass. Biomass is any carbon containing material derived from living, or recently-living, organisms. The ability to convert biomass derived from plants, animals, and industrial waste provides a direct source for renewable fuels including gasoline, diesel, oils and other products that can substitute for fuel products produced from non-renewable fossil fuels.
Processes to convert renewable resources into transportation fuels usually involve several steps. One approach is to use acids to convert carbohydrates, starches, lignins, and other biomass into sugars such as glucose, lactose, fructose, sucrose, dextrose. Another approach is to utilize pyrolysis to convert biomass solids and liquids into pyrolysis oil, or bio-oil.
Pyrolysis is the chemical decomposition of organic materials by heating in the absence of oxygen or other reagents. Pyrolysis can be used to convert biomass into pyrolysis oil (or bio-oil). Bio-oil is typically produced by heating biomass to a temperature between 250° C. to 1000° C. in a predominantly inert atmosphere for a short time. The bio-oil thereby produced contains molecules derived from the original biomass feedstock, and is consequently a mixture of primarily oxygenated products. Bio-oil typically is thermally unstable, acidic, and not miscible with petroleum feedstocks. Thus, it is normally further processed to create hydrocarbon products that are fungible with current petroleum-based fuels.
A number of methods are known for the pyrolytic conversion of biomass, However, these conventional methods need to be further optimized to reduce the overall costs associated with biofuels production, thereby making the use of these fuels more attractive. What is needed are methods for converting a biomass-derived feedstock to biofuels that can reduce cost, increase throughput, and require less maintenance of process equipment.

BRIEF DESCRIPTION OF THE DISCLOSURE

The present disclosure provides novel processes for converting biomass to bio-oil by means of pyrolysis. In certain embodiments, the process comprises providing a thermal reactor comprising at least one auger and a first mixture comprising at least one catalyst, wherein the catalyst is also a heat carrier capable of rapidly transferring heat to a feedstock. A feedstock comprising biomass is introduced to the thermal reactor and contacted with the first mixture to form a second mixture and convert the feedstock into solids, condensable vapor intermediates, and non-condensable gases via pyrolysis. The at least one catalyst transfers heat to the feedstock and also increases the rate at which the feedstock is converted, while rotation of the at least one auger increases direct contact between the feedstock and the catalyst and increases the rate of heat transfer from the catalyst to the feedstock. The second mixture is conveyed through the reactor for a defined residence time prior to removal from the reactor.
In certain embodiments, the thermal reactor is maintained at a pressure in a range from about 50 psig to about 500 psig and a temperature in a range from about 250° C. to about 1000° C. In certain alternative embodiments, the thermal reactor is maintained at a pressure in a range from about 15 psig to about 50 psig and a temperature in a range from about 350° C. to about 700° C.
In certain embodiments, the catalyst is introduced proximal to a reactor first end and is conveyed by the at least one auger to a point downstream where the feedstock is introduced to combine with the first mixture to form the second mixture. Upon introducing the feedstock to the reactor, the feedstock is heated at a rate from about 100° C. per second, to about 10,000° C. per second.
Generally, the presence of the at least one catalyst increases the rate of pyrolysis, such that the temperature required for pyrolysis is lowered, the required residence time of the feedstock is decreased, or combinations thereof. In certain embodiments, the atmosphere maintained inside the thermal reactor comprises an inert gas and less than 0.5 mol % oxygen gas. In certain alternative embodiments, the atmosphere maintained inside the thermal reactor comprises a reactive gas selected from a group consisting of hydrogen, synthesis gas (i.e., CO+H2), steam/water, ammonia, methane, ethane, propane, butane, pentane, and natural gas, etc., and any combinations of these gases.
In certain embodiments, the catalyst comprises at least one of Co, Ni, Mo, W, Zn, Ga a zeolite, a metal-impregnated zeolite, or combinations of these catalysts. In certain embodiments, the catalyst comprises a solid material capable of both absorbing heat and transferring said heat to the feedstock, wherein the solid material is a member of the group consisting of silica, alumina, magnesium oxide, a zeolite and combinations thereof. In certain embodiments, the solid material is physically linked to, impregnated with or exists as a solid amorphous mixture with at least one member of the group consisting of Co, Ni, Mo, W, Zn, Ga, and combinations thereof.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a simplified flow-chart representing an embodiment of the inventive processes disclosed herein.

DETAILED DESCRIPTION

Pyrolysis is the chemical decomposition of biomass by heating in the absence of oxygen or other reagents. Intermediates produced via pyrolysis may be further processed by one or more refining means for production of renewable hydrocarbon fuels. Pyrolysis has been studied extensively, and a variety of pyrolysis processes and conditions are known. Pyrolysis may be conducted at a variety of temperatures and pressures, in the presence (or absence) of an inert gaseous atmosphere and may be facilitated by a catalyst or a heat-carrier.
The biomass to be pyrolyzed according the methods disclosed herein may be any type of biomass derived from plants or animals. The biomass to be utilized as feedstock is selected according to its pyrolysis characteristics and ash fusion point. Typically, biomass (or a mixture of biomass derived from different sources) with an ash fusion point no less than 700° C. is fed into a pyrolysis reactor after being collected, screened, dried and crushed. The pyrolysis temperature and reaction time are carefully controlled to rapidly decompose the reactant by heat to form a gas, at least a portion of which is condensed to form a liquid intermediate product comprising pyrolysis oil.
Examples of biomass feedstock may include, but are not limited to biomass derived from plants, protists (including micro-algae and macro algae), and animal biomass. Lignocellulosic biomass is commonly utilized as a feedstock for production of biofuels, and may be comprised of cellulose, hemicellulose, and lignin. Cellulose and hemicellulose are carbohydrate polymers. The carbohydrate polymers are tightly bound to the lignin. Lignocellulosic biomass may be grouped into four main categories: (1) agricultural residues, (2) dedicated energy crops, (3) wood residues, and (4) municipal solid waste. The agricultural residues may include, but not limited to, corn stover, wheat straw and sugarcane bagasse. Many energy crops may also be of interest for their ability to provide high yields of biomass and may be harvested multiple times each year. These may include, but not limited to, poplar trees, switchgrass, and miscanthus giganteus. The premier energy crop is sugarcane, which is a source of the readily fermentable sucrose and the lignocellulosic side product bagasse. The wood residues may include, but are not limited to, sawmill and paper mill discards.
In the pyrolysis processes disclosed herein, the feedstock is rapidly heated to produce one or more volatile gases. In certain embodiments, the feedstock is heated in a reactor comprising at least one auger, where the reactor is maintained in a range from about 250° C. to 1000° C. In certain embodiments, the feedstock is heated in a reactor maintained in a range from about 350° C. to about 750° C.
In some embodiments, the feedstock is heated in an atmosphere comprising an inert gas and in the absence of oxygen. The inert gas may be, but is not limited to, nitrogen, argon, helium, or carbon dioxide, or combinations of these gases. In certain embodiments, the feedstock is heated in an atmosphere comprising an inert gas and oxygen, where the concentration of oxygen is in the range from about 0.0 mol % to about 0.5 mol %. In another embodiment, the gaseous atmosphere may comprise oxygen in the range from about 0.5 mol % to about 5 mol %.
Alternatively, the feedstock is heated in the presence of an atmosphere comprising a one or more gaseous compounds that can donate hydrogen. These gases may include, but are not limited to, hydrogen, synthesis gas (i.e., CO+H₂), steam/water, ammonia, methane, ethane, propane, butane, pentane, and natural gas. Certain embodiments may combine one of these gases with an inert gas. Not intending to be bound by theory, it is believed that these various mixtures may create a reducing atmosphere and quench any unstable radical species formed during heating of the feedstock. When using a hydrogen donor compound or hydrocarbon, mass ratios for feedstock to hydrogen donor compound or hydrocarbon may be in the order of 0.1-to-2.
A solid heat carrier material is often utilized to increase the heating rate of the feedstock during pyrolysis, thereby reducing the amount of char formed. Any material capable of absorbing and transferring heat to a biomass feedstock may be utilized in the processes disclosed herein. Materials conventionally utilized as heat carriers include, for example, silica, alumina, a zeolite, and magnesium oxide, although many other solid heat carrier materials may be suitable. In the present disclosure, the heat carrier may also comprise a mixture of one or more heat carrier materials. In certain embodiments, the heat carrier also comprises a catalyst that facilitates the pyrolysis of the biomass feedstock. The heat carrier may be impregnated with the catalyst, may exist as a solid amorphous mixture of heat carrier and catalyst, or may comprise at least one material that functions simultaneously as both heat carrier and catalyst.
One or more catalysts may be utilized for the pyrolysis reaction to promote hydrogenationlhydrogenolysis reactions of the biomass feedstock. The catalyst may comprise, but is not limited to, catalysts conventionally used in hydroprocessing of hydrocarbons, such as, for example, those comprising metals such as Co, Ni, Mo and W. More specific examples of catalysts that have been utilized in catalytic pyrolysis include various zeolites as well as metal-impregnated zeolites, such as, for example HUSY, REY, HZSM-5, Ni—Mo-HUSY, Ni—Mo-REY. The catalyst may be placed on any solid material known to be suitable as a solid catalyst support. In certain embodiments, the solid support is gamma alumina. In certain embodiments, the solid catalyst support serves as the heat carrier and transfers heat to
Additional examples of zeolites suitable for use as catalysts for the inventive processes disclosed herein include, but are not limited to, those disclosed in Kirk-Othmer Encyclopedia of Chemical Technology, third edition, volume 15, pages 638-669 (John Wiley & Sons, New York, 1981). Generally, zeolites useful in the present invention have a constraint index (as defined in U.S. Pat. No. 4,097,367, incorporated herein by reference) in the range of from about 0.4 to about 12, and preferably in the range of from about 2 to about 9. In addition, the molar ratio of SiO₂to Al₂O₃in the crystalline framework of the zeolite is at least about 5:1 and can range up to infinity. In one embodiment of the present invention, the molar ratio of SiO₂to Al₂O₃in the crystalline framework of the zeolite is in the range of from about 8:1 to about 200:1. In another embodiment of the present invention, SiO₂to Al₂O₃in the crystalline framework of the zeolite is in the range of from about 12:1 to about 100:1. Zeolites useful in the present invention include but are not limited to ZSM-5, ZSM-8, ZSM-11, ZSM-12, ZSM-35, ZSM-38 and combinations thereof. Some of these zeolites are also known as “MFI” or “Pentasil” zeolites. In one embodiment of the present invention, the zeolite is ZSM-5. Modified zeolites can also be used. Modified zeolites can include zeolites modified by metal cations, such as, for example, zinc, gallium, or nickel. Zeolites can also be modified by steam treatment and/or acid treatment. In addition, zeolites of the present invention may be combined with a clay, promoter, and/or a binder. Zeolites useful in the present invention may also contain an inorganic binder (also referred to as matrix material) selected from the group consisting of alumina, silica, alumina-silica, aluminum phosphate, clays (such as bentonite), and combinations thereof. The type of zeolite used will cause the final product to vary considerably.
The conventional pyrolysis of biomass is often conducted in fluidized bed reactors. A heated carrier gas is mixed with the biomass feedstock, and bubbles through the biomass to cause mixing, thereby facilitating heart transfer through the feedstock. The methods described herein instead utilize a reactor comprising at least one mechanical auger (hereby termed “auger reactor”) to mechanically mix the feedstock (or a mixture of feedstock and a heat-carrier) to facilitate a high rate of heat transfer to the feedstock. This requires that only moderate temperatures be maintained within the reactor to effectively promote pyrolysis of the feedstock, while also preventing premature devolatilization of the feedstock.
FIG. 1 provides a general flow diagram for one embodiment of the inventive processes disclosed herein. A first mixture 101 comprising a particulate solid material that functions as both heat carrier and as pyrolysis catalyst is heated in an oven until the solid material reaches a desired temperature. The first mixture 101 is then introduced near a first end of a reactor 125 that comprises at least one auger 150 (auger reactor). As the at least one auger rotates, the first mixture is conveyed through the auger reactor away from the first end to a point downstream from the entry point of the first mixture, where a biomass feedstock 175 is introduced to the auger reactor and combines with the first mixture to produce a second mixture. The feedstock is introduced at a ratio of first mixture to feedstock of between about 1:1 and about 50:1. Rotation of the at least one auger mechanically mixes the first mixture with the biomass feedstock, thereby producing a second mixture and assuring rapid and even heat transfer from heat carrier/catalyst to the feedstock. In certain alternative embodiments, the feedstock may be introduced upstream from the first mixture (not depicted). In such cases, a portion of the heating of the feedstock may occur inside the reactor immediately after the feedstock enters the auger reactor, but prior to contacting the first mixture.
In certain embodiments, the conditions maintained within the auger reactor 125 include a temperature of between about 250° C. and about 1000° C. Preferably, the auger reactor is maintained at a temperature of between about 350° C. and about 700° C. Upon introduction to the reactor, the biomass feedstock is rapidly heated at a rate in the range of about 100° C. sec⁻¹to about 10,000° C. sec⁻¹. Heating of the biomass feedstock may be performed by heat transfer from a carrier gas, through direct contact with the rector walls, through contact with a solid material comprising both heat carrier and catalyst functionalities (as discussed above). Pressure within the reactor is generally maintained between about atmospheric pressure to about 500 psig, and in certain embodiments maintained at a pressure of between about 15 psig to about 50 psig. The total residence time of the feedstock within the reactor is kept in a range between about 0.1 sec and about 10 sec, while in certain embodiments, the total residence time within the reactor is kept between 1 sec and about 40 sec.
One advantage of the processes disclosed herein are believed to facilitate rapid and even heating of the feedstock while also continuously moving the first and second mixture downstream toward the second end of the reactor, thereby assuring a constant residence time for the second mixture within the reactor. The residence time can be adjusted by adjusting the rotational speed of the auger. An additional advantage is that as the biomass feedstock enters the pyrolysis reactor, it always contacts either fresh, or freshly-regenerated, solid material functioning as both heat carrier/catalyst. This allows more efficient catalytic pyrolysis, thereby improving the quality of the produced bio-oil and decreasing the formation of char and coke. More efficient pyrolysis enabled by the presence of a dual function heat carrier/catalyst potentially allows a lower temperature to be maintained in the reactor, a higher throughput of feedstock by decreasing required residence time, or combinations of these benefits.
Additional benefits of the processes disclosed herein include a decreased requirement for carrier gas (i.e., inert carrier gas or reactive carrier gas) to be mixed with the feedstock prior to entering the pyrolysis reactor, because the auger reactor does not utilize carrier gas as the method of primary heat transfer. Instead, an auger reactor facilitates efficient heat transfer via constant mechanical mixing via the at least one auger. The decreased requirement for carrier gas also allows for easier collection of the liquid intermediate product.
Again referring to FIG. 1, upon reaching the second end of the auger reactor 125, the solid material functioning as both heat carrier and catalyst, along with any char and ash remaining after pyrolysis of the biomass are removed from the reactor and collected 190. The char and ash may then be separated from the heat carrier/catalyst by conventional methods. The char may be further separated and used for combustion (not depicted), while the solid material functioning as heat carrier and catalyst may be conveyed to a regeneration reactor (not depicted) for regeneration of the catalyst at a temperature generally ranging from 400° C. to 1200° C. in the presence of oxygen, such that any coke deposits on the solid material comprising heat carrier/catalyst are removed by combustion. Such techniques are conventional and understood by those having skill in the art. Regeneration of the solid material produces the first mixture, which is then conveyed to an oven that maintains the temperature of the first mixture at a temperature that is optimized for catalytic pyrolysis of the biomass feedstock. In embodiments where the solid material is relatively inexpensive to obtain or synthesize, regeneration may not be cost-effective. In these embodiments, the solid material may be discarded and replaced with fresh solid material functioning as both heat carrier and catalyst. In certain embodiments, oxygen gas utilized in the regeneration reactor may be at least partially purged/replaced (or largely replaced) by an inert gas atmosphere prior to introducing the first mixture to the auger reactor.
Again referring to FIG. 1, the volatile gases created during pyrolysis are conveyed from the reactor, and are rapidly quenched. At least a portion of the vapors are condensed to generate a mixture of hydrocarbons and oxygenates 215. The mixture generated by condensation of these volatile gases is generally termed as bio-oil. In certain embodiments, the quenching may be carried out at a pressure in the range from about 1.4 psig to about 100 psig and at a temperature in a range from about −20° C. to about 80° C.
Depending on the degree of deoxygenation achieved and the components of the heating atmosphere, three or four product phases are obtained, i.e., solid, liquid and gas. The solid phase is composed mainly of char and used catalyst, if the latter is used. The gas phase contains mainly carbon oxides and light hydrocarbons. The liquid phase may be one or two phases. When two phases are formed, one phase is mainly aqueous with some polar organics dissolved. The other phase has a lower concentration of water and is mainly a mixture of organic compounds, such as those named above. Separation of the organic phase can be carried out by decantation when two separated liquid phases are obtained. The recovered gases produced during catalytic pyrolysis can optionally be used for hydrogen production using conventional technologies as described in that art.
The processes disclosed herein result in the production of a bio-oil (pyrolysis oil), which is a mixed liquid product derived from biomass pyrolyzed by heating in the absence (or near absence) of O₂. Bio-oil components vary relative to the composition of the original biomass. Typically, bio-oil contains molecules derived from the cellulose, hemicellulose, lignin and other biological molecules in the biomass feedstock, and is consequently a mixture of a variety of oxygenated products. The bio-oil comprises a mixture of several organic compounds, including hydrocarbons, sugar and derivatives, alcohols or polyols (such as glycerol, sorbitol, xylitol, for example), esters, alcohols, ketones, aldehydes, carboxylic acids, phenolics and polymers, along with tars, oils and water-insoluble solids. Bio-oil is thermally unstable, acidic, and is not typically miscible with petroleum feedstocks.
The bio-oil produced by the catalytic pyrolysis processes described herein may be further processed by one or more refining means to produce biofuels or hydrocarbons that can be used in blends with conventional fuels such as gasoline and diesel. The one or more refining means may include, but are not limited to, hydro-treating, fluidized catalytic cracking, hydro-cracking and coking. These are all conventional methods understood by one having skill in the art. The refining may be carried by any conventional methods and the scope of the present invention should not be limited to the examples provided herein.
The following example is provided by way to better explain one or more of the various embodiments, and should not be interpreted as limiting, or defining the scope of the invention.

Example 1

Either micro-algal or lignin biomass was dried at 70° C. for 12 hours, and then pyrolyzed with and without zeolite catalyst in inert (He) atmosphere. Pyrolysis was conducted at 475° C. pyrolysis temperature, heating rate ˜10,000° C./s and a 5:1 catalyst ratio (when used). Vapors were analyzed by gas chromatography/mass spectrometry (GC/MS). Char was measured by gravimetric difference. All yields are on a mass basis.
The data (see Tables 1 and 2) show a greater than 60% yield of condensable vapors from both micro-algal (Table 1) and lignin (Table 2) biomass in un-catalyzed pyrolysis and 50% or greater yield during catalyzed pyrolysis. Adding a zeolite catalyst improved yield of hydrocarbons in the vapor phase, while also increasing char yield.

TABLE I

Yield of pyrolysis products from dried, whole microalgae.

	Yield %,	Yield %,
Product	no catalyst	zeolite catalyst

Noncondensable gas*	6	17
Char*	19	28
Condensable vapors*	74	55
Hydrocarbons in vapor**	9	44

*Yield based on total biomass
**Yield based on condensable vapors only

TABLE II

Yield of pyrolysis products using lignin
from corn stover hydrolysate:

	Yield %,	Yield %,
Product	no catalyst	zeolite catalyst

Noncondensable gas*	2	6
Char*	37	44
Condensable vapors*	61	50
Hydrocarbons in vapor**	3	40

*Yield based on total biomass
**Yield based on condensable vapors only

As used herein, the term “auger reactor” is defined as any cylindrical, oval, or frusto-conically shaped reactor comprising at least one auger, which in turn, comprises a shaft passing axially therethrough, wherein each shaft is attached to one edge of a continuous blade having a non-perpendicular angle, or pitch, relative to the shaft, wherein rotation of the shaft causes the continuous blade to rotate, such that a material fed into one end of the reactor is mechanically conveyed through the reactor by the screw-like movement of at least one blade. Certain embodiments of an auger reactor may comprise multiple augers, wherein the augers may act in concert to mechanically mix the material passed through the reactor.
In closing, it should be noted that the discussion of any reference is not an admission that it is prior art to the present invention, in particular references that have a publication date after the priority date of this application. The claims listed below are hereby incorporated into this detailed description or specification as additional embodiments of the present inventive disclosure.
Although the systems and processes described herein have been described in detail, it should be understood that various changes, substitutions, and alterations can be made without departing from the spirit and scope of the invention as defined by the following claims. Those skilled in the art may be able to study the disclosed embodiments and identify other ways to practice the invention that are not exactly as described herein, but are equivalent. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims while the description, abstract and drawings are not to be used to limit the scope of the invention.

REFERENCES

All of the references cited herein are expressly incorporated by reference. The discussion of any reference is not an admission that it is prior art to the present invention, especially any reference that may have a publication data after the priority date of this application. Incorporated references are listed again here for convenience:

1. US Ser. No. 7,578,927, US Ser. No. 2008/0053870, WO2008/027699, Marker, et al., “Gasoline And Diesel Production From Pyrolytic Lignin Produced From Pyrolysis Of Cellulosic Waste,” UOP L.L.C. (2006).
2. U.S. Ser. No. 13/274,754, Lotero Alegria, et al., “Hydrocarbons From Pyrolysis Oil,” ConocoPhillips Company (2011).
3. U.S. Ser. No. 13/280,982, Gong, et al., “Process For Producing High Quality Pyrolysis Oil From Biomass,” ConocoPhillips Company (2011).
4. U.S. Ser. No. 61/411,531, Gong, et al., “Heat Integrated Process For Producing High Quality Pyrolysis Oil From Biomass,” ConocoPhillips Company (2010).
5. U.S. Ser. No. 61/427,270, Gong, et al., “Integrated FCC Biomass Pyrolysis/Upgrading,” ConocoPhillips Company (2010).
6. Lu, Changbo, et al. “Kinetics of Biomass Catalytic Pyrolysis” Biotech Advances 27 (2009) 583-587.

Claims

1. A process comprising:

(a) providing a thermal reactor comprising at least one auger, and a first mixture comprising at least one catalyst, wherein the at least one catalyst functions as both a heat carrier and catalyst;

(b) introducing a feedstock comprising biomass to the thermal reactor and contacting therein with the first mixture to produce a second mixture

c) pyrolyzing the feedstock in the second mixture thereby producing solids, condensable vapor intermediates, and non-condensable gases,

wherein the at least one catalyst transfers heat to the feedstock and also increases the rate at which the feedstock is converted,

wherein rotation of the auger increases direct contact between the feedstock and the catalyst and increases the rate of heat transfer from the catalyst to the feedstock,

(c) conveying the second mixture through the reactor for a defined residence time prior to removal from the reactor.

2. The process of claim 1, wherein said thermal reactor is maintained at a pressure in a range from about 50 psig to about 500 psig and a temperature in a range from about 250° C. to about 1000° C.

3. The process of claim 1, wherein said thermal reactor is maintained at a pressure in a range from about 15 psig to about 50 psig and a temperature in a range from about 350° C. to about 700° C.

4. The process of claim 1, wherein upon introducing the feedstock to the reactor, the feedstock is heated by the catalyst at a rate from about 100° C. per second to about 10,000° C. per second.

5. The process of claim 1, wherein the first mixture is introduced a first location that is proximal to a reactor first end and is conveyed by the at least one auger to a second location that is located downstream, wherein the feedstock is introduced at the second point and combines with the first mixture to form a second mixture.

6. The process of claim 1, wherein the feedstock is introduced at a first location that is proximal to a reactor first end and is conveyed by the at least one auger to a second location located downstream, wherein the first mixture is introduced to the reactor at the second point and combines with the feedstock to form a second mixture.

7. The process of claim 1, wherein the defined residence time is decreased as a result of step (b)

8. The process of claim 1, wherein the at least one catalyst increases the rate of pyrolysis, such that the temperature required for pyrolysis is decreased, the required residence time of the feedstock is decreased, or combinations thereof.

9. The process of claim 1, wherein the feedstock is converted in an atmosphere comprising an inert gas and less than 0.5 mol % oxygen gas.

10. The process of claim 1, wherein the feedstock is converted to condensable vapor intermediates in the presence of a reactive gas selected from a group consisting of hydrogen, synthesis gas (i.e., CO+H2), steam/water, ammonia, methane, ethane, propane, butane, pentane, and natural gas, etc., and any combinations thereof.

11. The process of claim 1, wherein rotation of the at least one auger increases contact between the at least one catalyst and the feedstock, thereby increasing the heating rate of the feedstock.

12. The process of claim 1, wherein rotation of the at least one auger increases contact between the at least one catalyst and the feedstock to increase the catalytic pyrolysis of the feedstock.

13. The process of claim 1, wherein the catalyst comprises at least one of Co, Ni, Mo, W, Zn, Ga, a zeolite, a metal-impregnated zeolite, and combinations thereof.

14. The process of claim 1, wherein the catalyst comprises a solid material capable of both absorbing heat and transferring said heat to the feedstock, wherein the solid material is a member of the group consisting of silica, alumina, magnesium oxide, a zeolite and combinations thereof.

15. The process of claim 13, wherein the solid material is physically linked to, impregnated with or exists as a solid amorphous mixture with at least one member of the group consisting of Co, Ni, Mo, W, Zn, Ga, and combinations thereof.

16. A process comprising:

wherein the at least one catalyst comprises a solid material capable of both absorbing heat and transferring said heat to the feedstock, wherein the solid material is a member of the group consisting of silica, alumina, magnesium oxide, a zeolite and combinations thereof,

wherein the solid material is physically linked to, impregnated with or exists as a solid amorphous mixture with at least one member of the group consisting of Co, Ni, Mo, W, Zn, Ga, and combinations thereof.