LIGNOCELLULOSIC BIOMASS FERMENTATION PROCESS CO- PRODUCT FUEL FOR CEMENT KILN

This application claims the benefit of United States Provisional Applications 61/889061 filed October 10, 2013 and 62/026059, filed July 18, 2014 each of which is incorporated by reference in its entirety.

FIELD OF THE INVENTION

The invention relates to the field of fueling a cement process. More specifically, a fuel prepared from co-products of a lignocellulosic biomass fermentation process is used to fuel a cement kiln.

BACKGROUND OF THE INVENTION

Cement is one of the most important and highly used building materials in the world, being is used in materials such as concrete, mortar, stucco, and many non-specialty grouts. Cement production is highly energy intensive, as a temperature of about 1450 °C is required for the process. The primary fuel used in making cement is coal, with about 120 kg of coal required per ton of cement produced. It has been estimated that about 5% of global carbon dioxide emissions originate from cement production, 50% of which is from the chemical process and 40% of which is from burning fuel. The use of coal as fuel releases to the atmosphere carbon that was sequestered underground, producing a net positive gain of carbon to the earth's atmosphere.

Fuel derived from biomass is renewable and is carbon neutral: the same amount of CO2 is removed from the atmosphere during growth of the biomass as is released to the atmosphere upon burning. Thus in contrast to coal, a biomass or biomass-derived fuel does not increase the atmospheric CO2 burden and so is more environmentally friendly.

A number of waste materials have been used as alternative fuels in cement production such as asphalt, plastics, rubber, petcoke, tires, and waste oils. In addition, agricultural and non-agricultural biomass has been suggested for use as fuel in cement production. There remains a need for a cement kiln fueling process that makes use of a fuel that is renewable and more environmentally friendly than coal, as well as being consistent and reliable.

SUMMARY OF THE INVENTION

The invention relates to the use of a carbon neutral fuel derived from the processing of lignocellulosic biomass to fuel cement kilns which typically are fueled by coal. Accordingly the invention provides a process for fueling a cement process comprising:

a) providing a lignocellulosic filter cake;

b) providing a lignocellulosic syrup;

c) mixing the filter cake of (a) and the syrup of (b) in a filter cake to syrup ratio that is between 1 :1 and 9:1 forming a filter cake and syrup mixture;

d) drying the mixture of (c) producing a filter cake and syrup fuel; and

e) burning the filter cake and syrup fuel in a cement kiln containing cement raw material.

Additionally the invention provides a cement composition comprising ash from burned material selected from the group consisting of filter cake and syrup fuel, filter cake, syrup, and mixtures thereof.

In another aspect the invention provides a concrete composition comprising ash from burned material selected from the group consisting of filter cake and syrup fuel, filter cake, syrup, and mixtures thereof.

In another aspect of the invention a process for the production of cement is provided comprising:

a) providing a limestone composition wherein the limestone

composition optionally comprises one or more of clay, shale, silca, sand bauxite, iron ore, fly ash, and slag;

b) optionally grinding the limestone composition of a); c) heating the limestone composition of a) or b) in a kiln to a temperature of at least about 600 °C wherein fuel is added to the kiln in the presence of the limestone

e composition wherein clinker is produced; and

d) cooling and recovering the clinker from the kiln;

wherein the fuel added to the kiln at step c) is comprised of a lignocellulosic co-product selected from the group consisting of filter cake and syrup fuel, filter cake, syrup, and mixtures thereof.

DETAILED DESCRIPTION

The following definitions and abbreviations are to be used for the interpretation of the claims and the specification.

As used herein, the terms "comprises," "comprising," "includes," "including," "has," "having," "contains" or "containing," or any other variation thereof, are intended to cover a non-exclusive inclusion. For example, a composition, a mixture, process, method, article, or apparatus that comprises a list of elements is not necessarily limited to only those elements but may include other elements not expressly listed or inherent to such composition, mixture, process, method, article, or apparatus.

Further, unless expressly stated to the contrary, "or" refers to an inclusive or and not to an exclusive or. For example, a condition A or B is satisfied by any one of the following: A is true (or present) and B is false (or not present), A is false (or not present) and B is true (or present), and both A and B are true (or present).

The indefinite articles "a" and "an" preceding an element or component of the invention are intended to be nonrestrictive regarding the number of instances (i.e. occurrences) of the element or component. Therefore "a" or "an" should be read to include one or at least one, and the singular word form of the element or component also includes the plural unless the number is obviously meant to be singular.

The term "invention" or "present invention" as used herein is a non- limiting term and is not intended to refer to any single embodiment of the particular invention but encompasses all possible embodiments as described in the specification and the claims.

As used herein, the term "about" modifying the quantity of an ingredient or reactant of the invention employed refers to variation in the numerical quantity that can occur, for example, through typical measuring and liquid handling procedures used for making concentrates or use solutions in the real world; through inadvertent error in these procedures; through differences in the manufacture, source, or purity of the ingredients employed to make the compositions or carry out the methods; and the like. The term "about" also encompasses amounts that differ due to different equilibrium conditions for a composition resulting from a particular initial mixture. Whether or not modified by the term "about", the claims include equivalents to the quantities. In one embodiment, the term "about" means within 10% of the reported numerical value, preferably within 5% of the reported numerical value.

The term "lignocellulosic" refers to a composition comprising both lignin and cellulose. Lignocellulosic material may also comprise

hemicellulose.

The term "cellulosic" refers to a composition comprising cellulose and additional components, including hemicellulose.

The term "lignocellulosic biomass" refers to any lignocellulosic material and includes materials comprising cellulose, hemicellulose, lignin, starch, oligosaccharides and/or monosaccharides. Biomass may also comprise additional components, such as protein and/or lipid. Biomass may be derived from a single source, or biomass can comprise a mixture derived from more than one source; for example, biomass could comprise a mixture of corn cobs and corn stover, or a mixture of grass and leaves. Lignocellulosic biomass includes, but is not limited to, bioenergy crops, agricultural residues, municipal solid waste, industrial solid waste, sludge from paper manufacture, yard waste, wood and forestry waste. Examples of biomass include, but are not limited to, corn cobs, crop residues such as corn husks, corn stover, grasses (including Miscanthus), wheat straw, barley straw, hay, rice straw, switchgrass, waste paper, sugar cane bagasse, sorghum plant material, soybean plant material, components obtained from milling of grains or from using grains in production processes (such as DDGS: dried distillers grains with solubles), woody material such as trees, branches, roots, wood chips, sawdust, shrubs and bushes, leaves, vegetables, fruits, flowers, empty palm fruit bunch, and energy cane.

The term "energy cane" refers to sugar cane that is bred for use in energy production. It is selected for a higher percentage of fiber than sugar.

The term "lignocellulosic biomass hydrolysate" refers to the product resulting from saccharification of lignocellulosic biomass. The biomass may also be pretreated or pre-processed prior to saccharification.

The term "pretreated biomass" means biomass that has been subjected to pretreatment prior to saccharification. The pretreatment may take the form of physical, thermal or chemical means and combinations thereof.

The term "saccharification" refers to the production of fermentable sugars from polysaccharides.

The term "butanol" refers to isobutanol, 1 -butanol, 2-butanol, or combinations thereof.

The term "lignocellulosic biomass hydrolysate fermentation broth" is broth containing product resulting from biocatalyst growth and production in a medium comprising lignocellulosic biomass hydrolysate. This broth includes components of lignocellulosic biomass hydrolysate that are not consumed by the biocatalyst, as well as the biocatalyst itself and product made by the biocatalyst.

The term "slurry" refers to a mixture of insoluble material and a liquid. A slurry may also contain a high level of dissolved solids. Examples of slurries include a saccharification broth, a fermentation broth, and a stillage.

The term "whole stillage" refers to the bottoms of a distillation. The whole stillage contains the high boilers and any solids of a distillation feed stream. Whole stillage is a type of depleted broth. Whole stillage is a type of product depleted fermentation broth.

The term "thin stillage" refers to a liquid fraction resulting from solid/liquid separation of a fermentation broth, or product depleted fermentation broth (such as whole stillage).

The term "product depleted broth" or "depleted broth" refers herein to a lignocellulosic biomass hydrolysate fermentation broth after removal of a product stream.

The term "syrup" means a concentrated product produced from the removal of water, generally by evaporation, from thin stillage.

The term "filter cake" refers to a product remaining after removal of water from fermentation broth, or product depleted fermentation broth (such as whole stillage).

The term "target product" refers to any product that is produced by a microbial production host cell in a fermentation. Target products may be the result of genetically engineered enzymatic pathways in host cells or may be produced by endogenous pathways. Typical target products include but are not limited to acids, alcohols, alkanes, alkenes, aromatics, aldehydes, ketones, biopolymers, proteins, peptides, amino acids, vitamins, antibiotics, and pharmaceuticals.

The term "fermentation" refers broadly to the use of a biocatalyst to produce a target product. Typically the biocatalyst grows in a fermentation broth utilizing a carbon source in the broth, and through its metabolism produces a target product.

The term "solid lignocellulosic fuel composition" refers to a mixture of lignocellulosic syrup and an additional fuel component. It includes an initial mixture of these components, as well as the mixture at any stage following mixing. It thus includes the composition during and after processing to form a readily handled fuel material.

"Solids" refers to soluble solids and insoluble solids. Solids from a lignocellulosic fermentation process contain residue from the

lignocellulosic biomass used to make hydrolysate medium. "Volatiles" refers herein to components that will largely be vaporized in a process where heat is introduced. Volatile content is measured herein by establishing the loss in weight resulting from heating under rigidly controlled conditions to 950 °C (as in ASTM D-3175). Typical volatiles include, but are not limited to, hydrogen, oxygen, nitrogen, acetic acid, and some carbon and sulfur.

"Fixed carbon" refers herein to a calculated percentage made by summing the percent of moisture, percent of ash, and percent of volatile matter, and then subtracting that percent from 100.

"Ash" is the weight of the residue remaining after burning under controlled conditions according to ASTM D-3174.

"Sugars" as referred to in the lignocellulosic syrup composition means a total of monosaccharides and soluble oligosaccharides. Provided herein is a process for fueling a cement process which makes use of a fuel that is renewable and more environmentally friendly than coal. With the growing cellulosic ethanol industry, this fuel will be a consistent and reliable fuel source.

In the process for preparing cement, cement raw material is heated in a cement kiln to very high temperatures. Cement raw material includes any materials that are added to a cement kiln for cement production. The major cement raw material is limestone. Additional materials may be included in the cement raw material in a cement kiln such as clay, shale, sand (typically silica), bauxite, iron ore, fly ash, and/or slag. Typically, a mixture of limestone and one or more additional material is made to provide cement raw material in a cement kiln. In various embodiments the cement raw material contains limestone along with clay, shale, sand (typically silica), bauxite, iron ore, fly ash, slag, or any mixture of these materials. Typically the mixture is ground and fed into the kiln where it is gradually heated by combusting fuel.

A temperature that is above 600 °C is needed for calcination of the limestone, which is the reaction shown in (I).

CaCO ₃ -> CaO + CO ₂ (I) A fusion temperature of about 1 ,450 °C is then needed to sinter the cement raw material into clinker.

Fuel is added into the cement kiln and is burned in the presence of the cement raw material. Any ash produced by burning of the fuel ends up in the clinker as a secondary raw material.

For example in a rotary cement kiln, a flame of burning fuel is in the lower part of a kiln tube which is slightly tilted and slowly rotated. Cement raw material is fed into the upper end of the kiln tube. Rotation of the kiln tube causes the cement raw material to slowly move down towards the lower end where it is heated, undergoing calcination and sintering. Then the produced clinker exits at the lower end into a cooler. Air is drawn through the cooler, where the air temperature is raised by the cooling clinker, then the heated air enters the kiln causing rapid combustion of fuel.

In the present process, the fuel that is burned in a cement kiln containing cement raw material is made from filter cake and syrup co- products produced in a lignocellulosic biomass fermentation process. The lignocellulosic biomass fermentation process is one that uses

lignocellulosic biomass as a source of fermentable sugars which are used as a carbon source for a biocatalyst. The biocatalyst uses the sugars in a fermentation process to produce a target product.

To produce fermentable sugars from lignocellulosic biomass, the biomass is treated to release sugars such as glucose, xylose, and arabinose from the polysaccharides of the biomass. Lignocellulosic biomass may be treated by any method known by one skilled in the art to produce fermentable sugars in a hydrolysate. Typically the biomass is pretreated using physical, thermal and/or chemical treatments, and saccharified enzymatically. Thermo-chemical pretreatment methods include steam explosion or methods of swelling the biomass to release sugars (see for example WO20101 13129; WO20101 13130). Chemical saccharification may also be used. Physical treatments for pre-processing the biomass include, but are not limited to, grinding, milling, and cutting. Physical treatments such as these may be used for particle size reduction prior to further chemical treatment. Chemical treatments include base treatment such as with strong base (ammonia or NaOH), or acid treatment (US8545633; WO2012103220). In one embodiment the biomass is treated with ammonia (US 7932063; US 7781 191 ; US 7998713; US7915017). These treatments release polymeric sugars from the biomass. Particularly useful is a low ammonia pretreatment where biomass is contacted with an aqueous solution comprising ammonia to form a biomass-aqueous ammonia mixture where the ammonia concentration is sufficient to maintain alkaline pH of the biomass-aqueous ammonia mixture but is less than about 12 weight percent relative to dry weight of biomass, and where dry weight of biomass is at least about 15 weight percent solids relative to the weight of the biomass-aqueous ammonia mixture, as disclosed in US 7,932,063 , which is herein incorporated by reference.

Saccharification, which converts polymeric sugars to monomeric sugars, may be either by enzymatic or chemical treatments. The pretreated biomass is contacted with a saccharification enzyme

consortium under suitable conditions to produce fermentable sugars. Prior to saccharification, the pretreated biomass may be brought to the desired moisture content and treated to alter the pH, composition or temperature such that the enzymes of the saccharification enzyme consortium will be active. The pH may be altered through the addition of acids in solid or liquid form. Alternatively, carbon dioxide (CO ₂ ), which may be recovered from fermentation, may be utilized to lower the pH. For example, CO ₂ may be collected from a fermenter and fed into the pretreatment product headspace in the flash tank or bubbled through the pretreated biomass if adequate liquid is present while monitoring the pH, until the desired pH is achieved. The temperature is brought to a temperature that is compatible with saccharification enzyme activity, as noted below. Typically suitable conditions may include temperature between about 40 °C and 50 °C and pH between about 4.8 and 5.8.

Enzymatic saccharification of cellulosic or lignocellulosic biomass typically makes use of an enzyme composition or blend to break down cellulose and/or hemicellulose and to produce a hydrolysate containing sugars such as, for example, glucose, xylose, and arabinose.

Saccharification enzymes are reviewed in Lynd, L. R., et al. (Microbiol. Mol. Biol. Rev., 66:506-577, 2002). At least one enzyme is used, and typically a saccharification enzyme blend is used that includes one or more glycosidases. Glycosidases hydrolyze the ether linkages of di-, oligo- , and polysaccharides and are found in the enzyme classification EC 3.2.1 .x (Enzyme Nomenclature 1992, Academic Press, San Diego, CA with Supplement 1 (1993), Supplement 2 (1994), Supplement 3 (1995, Supplement 4 (1997) and Supplement 5 [in Eur. J. Biochem., 223:1 -5, 1994; Eur. J. Biochem., 232:1 -6, 1995; Eur. J. Biochem., 237:1 -5, 1996; Eur. J. Biochem., 250:1 -6, 1997; and Eur. J. Biochem., 264:610-650 1999, respectively]) of the general group "hydrolases" (EC 3.). Glycosidases useful in saccharification can be categorized by the biomass components they hydrolyze. Glycosidases useful in saccharification may include cellulose-hydrolyzing glycosidases (for example, cellulases,

endoglucanases, exoglucanases, cellobiohydrolases, β-glucosidases), hemicellulose-hydrolyzing glycosidases (for example, xylanases, endoxylanases, exoxylanases, β-xylosidases, arabino-xylanases, mannases, galactases, pectinases, glucuronidases), and starch- hydrolyzing glycosidases (for example, amylases, a-amylases, β- amylases, glucoamylases, a-glucosidases, isoamylases). In addition, it may be useful to add other activities to the saccharification enzyme consortium such as peptidases (EC 3.4.x.y), lipases (EC 3.1 .1 .x and 3.1 .4.x), ligninases (EC 1 .1 1 .1 .x), or feruloyl esterases (EC 3.1 .1 .73) to promote the release of polysaccharides from other components of the biomass. It is known in the art that microorganisms that produce polysaccharide-hydrolyzing enzymes often exhibit an activity, such as a capacity to degrade cellulose, which is catalyzed by several enzymes or a group of enzymes having different substrate specificities. Thus, a

"cellulase" from a microorganism may comprise a group of enzymes, one or more or all of which may contribute to the cellulose-degrading activity. Commercial or non-commercial enzyme preparations, such as cellulase, may comprise numerous enzymes depending on the purification scheme utilized to obtain the enzyme. Many glycosyl hydrolase enzymes and compositions thereof that are useful for saccharification are disclosed in WO 201 1/038019. Additional enzymes for saccharification include, for example, glycosyl hydrolases that hydrolyze the glycosidic bond between two or more carbohydrates, or between a carbohydrate and a

noncarbohydrate moiety.

Saccharification enzymes may be obtained commercially. Such enzymes include, for example, Spezyme ^® CP cellulase, Multifect ^® xylanase, Accelerase ^® 1500, Accellerase ^® DUET, and Accellerase ^® Trio™ (Dupont™/ Genencor ^® , Wilmington, DE), and Novozyme-188

(Novozymes, 2880 Bagsvaerd, Denmark). In addition, saccharification enzymes may be unpurified and provided as a cell extract or a whole cell preparation. The enzymes may be produced using recombinant

microorganisms that have been engineered to express one or more saccharifying enzymes. For example, an H3A protein preparation that may be used for saccharification of pretreated cellulosic biomass is an unpurified preparation of enzymes produced by a genetically engineered strain of Trichoderma reesei, which includes a combination of cellulases and hemicellulases and is described in WO 201 1/038019, which is incorporated herein by reference.

Chemical saccharification treatments may be used and are known to one skilled in the art, such as treatment with mineral acids including HCI and H ₂ SO ₄ (US5580389; WO201 1002860).

Sugars such as glucose, xylose and arabinose are released by saccharification of lignocellulosic biomass and these monomeric sugars provide a carbohydrate source for a biocatalyst used in a fermentation process. The sugars are present in a biomass hydrolysate that is used as fermentation medium. The fermentation medium may be composed solely of hydrolysate, or may include components additional to the hydrolysate such as sorbitol or mannitol at a final concentration of about 5 mM as described in US 7,629,156, which is incorporated herein by reference. The biomass hydrolysate typically makes up at least about 50% of the fermentation medium. Typically about 10% of the final volume of fermentation broth is seed inoculum containing the biocatalyst.

The medium comprising hydrolysate is fermented in a fermenter, which is any vessel that holds the hydrolysate fermentation medium and at least one biocatalyst, and has valves, vents, and/or ports used in managing the fermentation process.

Any biocatalyst that produces a target product utilizing glucose and preferably also xylose, either naturally or through genetic engineering, may be used for fermentation of the fermentable sugars in the biomass hydrolysate made from lignocellulosic biomass. Target products that may be produced by fermentation include, for example, acids, alcohols, alkanes, alkenes, aromatics, aldehydes, ketones, biopolymers, proteins, peptides, amino acids, vitamins, antibiotics, and pharmaceuticals.

Alcohols include, but are not limited to methanol, ethanol, propanol, isopropanol, butanol, ethylene glycol, propanediol, butanediol, glycerol, erythritol, xylitol, mannitol, and sorbitol. Acids may include acetic acid, formic acid, lactic acid, propionic acid, 3-hydroxypropionic acid, butyric acid, gluconic acid, itaconic acid, citric acid, succinic acid, 3- hydroxyproprionic acid, fumaric acid, maleic acid, and levulinic acid.

Amino acids may include glutamic acid, aspartic acid, methionine, lysine, glycine, arginine, threonine, phenylalanine and tyrosine. Additional target products include methane, ethylene, acetone and industrial enzymes.

The fermentation of sugars in biomass hydrolysate to target products may be carried out by one or more appropriate biocatalysts, that are able to grow in medium containing biomass hydrolysate, in single or multistep fermentations. Biocatalysts may be microorganisms selected from bacteria, filamentous fungi and yeast. Biocatalysts may be wild type microorganisms or recombinant microorganisms, and may include, for example, organisms belonging to the genera of Escherichia, Zymomonas, Saccharomyces, Candida, Pichia, Streptomyces, Bacillus, Lactobacillus, and Clostridiuma. Typical examples of biocatalysts include recombinant Escherichia coli, Zymomonas mobilis, Bacillus stearothermophilus, Saccharomyces cerevisiae, Clostridia thermocellum, Thermoanaerobacterium saccharolyticum, and Pichia stipitis. To grow well and have high product production in a lignocellulosic biomass hydrolysate fernnentation broth, a biocatalyst may be selected or engineered to have higher tolerance to inhibitors present in biomass hydrolysate such as acetate. For example, the biocatalyst may produce ethanol as a target product, such as production of ethanol by Zymomonas mobilis as described in US 8,247,208, which is incorporated herein by reference.

Fermentation is carried out with conditions appropriate for the particular biocatalyst used. Adjustments may be made for conditions such as pH, temperature, oxygen content, and mixing. Conditions for

fermentation of yeast and bacterial biocatalysts are well known in the art.

In addition, saccharification and fermentation may occur at the same time in the same vessel, called simultaneous saccharification and fermentation (SSF). In addition, partial saccharification may occur prior to a period of concurrent saccharification and fermentation in a process called HSF (hybrid saccharification and fermentation).

For large scale fermentations, typically a smaller culture of the biocatalyst is first grown, which is called a seed culture. The seed culture is added to the fermentation medium as an inoculum typically in the range from about 2% to about 20% of the final volume.

Typically fermentation by the biocatalyst produces a fermentation broth containing the target product made by the biocatalyst. For example, in an ethanol process the fermentation broth may be a beer containing from about 6% to about 10% ethanol. In addition to target product, the fermentation broth contains water, solutes, and solids from the hydrolysate medium and from biocatalyst metabolism of sugars in the hydrolysate medium. Typically the target product is isolated from the fermentation broth producing a depleted broth, which may be called whole stillage. For example, when ethanol is the product, the broth is distilled, typically using a beer column, to generate an ethanol product stream and a whole stillage. Distillation may be using any conditions known to one skilled in the art including at atmospheric or reduced pressure. The distilled ethanol is further passed through a rectification column and molecular sieve to recover an ethanol product. The target product may alternatively be removed in a later step such as from a solid or liquid fraction after separation of fermentation broth.

The syrup and filter cake co-products of a lignocellulosic biomass fermentation process are produced from the fermentation broth or depleted fermentation broth. An example of syrup production is disclosed in US 8,721 ,794, which is incorporated herein by reference. The broth or depleted broth, such as whole stillage, is separated into solid and liquid streams, where the liquid stream is called thin stillage. Various filtration devices may be used such as a belt filter, belt press, screw press, drum filter, disc filter, Nutsche filter, filter press or filtering centrifuge. Filtration may be aided such as by application of vacuum, pressure, or centrifugal force. To improve efficiency of filtration, a heat treatment may be used as disclosed in commonly owned and co-pending US20120178976, which is incorporated herein by reference.

A product stream may be removed following liquid/solid filtration of a lignocellulosic biomass hydrolysate fermentation broth. For example, the liquid stream may be extracted or distilled to generate a product stream, such as distillation to produce an ethanol product stream and a remaining liquid.

Following liquid/solid separation of a lignocellulosic biomass hydrolysate fermentation broth or depleted broth the liquid fraction is further purified by evaporation producing water that may be recycled and a syrup. Prior to evaporation, a portion of the liquid fraction may be recycled for use as back set, which may be added at any point in the process where water is needed, such as in pretreatment, saccharification, or biocatalyst seed production. Evaporation may be in any evaporation system, such as falling film, rising film, forced circulation, plate or mechanical and thermal vapor recompression systems. Evaporation may be continuous or batch and may use a multi-effect evaporator. The evaporated water may be recycled in the overall lignocellulosic biomass hydrolysate fermentation process. The remaining material after evaporation is a syrup which is the present lignocellulosic syrup. The lignocellulosic syrup composition contains from about 40% to about 70% solids (may have about 40%, 45%, 50%, 55%, 60%, 65%, or 70% solids), from about 10 g/l to 30 g/l of acetamide, at least about 40 g/l of sugars, a density of about 1 to about 2 g/cm ³ , and viscosity less than 500 SSU at 100 °F (38 °C). "SSU" is Saybolt Universal Viscosity in Seconds (Burger VL, Encycl. Ind. Chem. Anal. (1966), Volume 3, 768-74). When biomass is treated with ammonia, the lignocellulosic syrup contains at least about 5 g/l of ammonia.

Following liquid/solid separation of a lignocellulosic biomass hydrolysate fermentation broth or depleted broth (such as whole stillage) the solids fraction is the present lignocellulosic filter cake (also called wetcake). The wet lignocellulosic filter cake composition contains from about 35% to 65% moisture, or from about 40% to about 60% moisture (may have about 35%, 40%, 45%, 50%, 55%, 60%, or 65% moisture), from about 20% to about 75% volatiles or about 20% to about 40% volatiles (may have about 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, or 75% volatiles), from about 35% to 65% solids or from about 40% to about 60% solids (may have about 35%, 40%, 45%, 50%, 55%, 60%, or 65% solids), from about 1 % to about 30% ash, or from about 3% to about 30% ash (may have about 1 %, 3%, 5%, 10%, 15%, 20%, 25%, or 30% ash), from about 5% to about 20% fixed carbon, and it has an energy value of about 2,000 to about 9,000 BTU/lb (may have about 2,000, 2,500, 3,000, 3,500, 4,000, 4,500, 5,000, 5,500, 6,000, 6,500, 7,000, 7,500, 8,000, 8,500, or 9,000 BTU/lb ). The volatile content is measured by establishing the loss in weight resulting from heating under rigidly controlled conditions to 950 °C (as in ASTM D-3175). Typical volatiles include hydrogen, oxygen, nitrogen, acetic acid, and some carbon and sulfur. Ash is determined by weighing the residue remaining after burning under controlled conditions according to ASTM D-3174. The amount of fixed carbon is calculated by adding the percentages of moisture, ash, and volatiles, and then subtracting from 100. The full upper range of BTU/lb is typically achieved with drying. The present fuel is produced by mixing lignocellulosic filter cake and lignocellulosic syrup in a ratio that is between about 1 :1 and about 9:1 forming a filter cake and syrup mixture. The ratio may be 1 :1 . 1 .5:1 , 2:1 , 2.5:1 , 3:1 , 3.5:1 , 4:1 , 4.5:1 , 5:1 , 5.5:1 , 6:1 , 6.5:1 , 7:1 , 7.5:1 , 8:1 , 8.5:1 , or 9:1 . The filter cake may be size reduced prior to mixing with syrup. For example, a delumper may be used to reduce the size of clumps of filter cake. Typically the components are added together slowly or in

increments while mixing to avoid clumping. Any type of mixer that accommodates wet feed may be used such as a paddle mixer, a screw mixer, or a mixer truck.

Pre-dried material may be included in the filter cake and syrup mixture. Pre-dried material may be filter cake that is previously dried, or filter cake and syrup mixture that is previously dried. Pre-dried filter cake may have a moisture content of about 20% or less.

The mixture of filter cake, syrup, and optionally pre-dried material is dried to achieve a moisture content of from about 8% to about 20% using any suitable type of dryer, to form a filter cake and syrup fuel. For example, the moisture content may be 8%, 9%, 10%, 1 1 %, 12%, 13%, 14%, 16%, 17%, 18%, 19%, or 20%. Any dryer system may be used that accommodates wet feed. For example, a cage mill flash dryer, rotary drum dryer, or ring flash dryer may be used. The resulting dried filter cake and syrup fuel is collected from the dryer and cooled.

In various embodiments, one or more of the following specific method steps may be applied. A delumper is used to reduce the size of filter cake clumps to about 0.5 inch (1 .427 cm) or less. Filter cake and syrup are fed separately to a mixing apparatus. Feeding is through spray nozzles. Pre-dried material (either dried filter cake or dried filter cake and syrup mixture) is fed to the mixing apparatus either prior to or concurrently with feeding of filter cake and syrup. The mixed filter cake and syrup passes to a dryer. The filter cake and syrup mixture is flash dried in a flash dryer. The dryer gas entering the dryer has a temperature of between about 225°C and 350°C. Dryer gas is used in the dryer that is

recompressed, reheated, and recycled to the dryer. The resulting dried filter cake and syrup fuel is separated from the dryer gas stream, cooled, and conveyed to bulk storage. A portion of the dried filter cake and syrup fuel is added to initial filter cake and syrup feed streams or to the mixing apparatus prior to addition of the filter cake and syrup.

The filter cake and syrup fuel is burned in a cement kiln containing cement raw material to produce the temperatures needed for cement production. The fuel may be burned in any type of cement kiln used in the cement production process, such as a precalciner, a calciner, and a rotary kiln.

The filter cake and syrup fuel may be used in combination with any other fuel that is used in the cement production process. Examples of other fuels that may be in a mixture with the filter cake and syrup fuel include coal, petroleum coke, and waste materials.

The material produced in the cement kiln is calcined clinker. This clinker is collected, cooled, and ground producing cement. Additives may be mixed with the cement to modify its properties such as gypsum, accelerators, dispersants, strength modifiers, retarders, extenders, weighting agents, fluid-loss control agents, antifoam agents, corrosion inhibitors, and combinations thereof.

An additional material that may be added to cement is ash residue from burned filter cake and syrup fuel. The filter cake and syrup fuel may be burned in any appropriate burning furnace to produce the ash, such as a steam boiler, hot water boiler, process furnace, or other industrial or commercial combustion process with suitable emissions controls. The ash may be used to alter the properties of the cement mixture. In addition, syrup or filter cake that is burned separately produces ash that may be added to cement. In various embodiments, ash from burned filter cake and syrup fuel, filter cake, syrup, or any mixture of these materials is added to cement. In one embodiment a cement composition contains ash from burned filter cake and syrup fuel, filter cake, syrup, or any mixture of these materials.

Concrete is typically a mixture of cement, water, and aggregate. In addition, ash residue from burned filter cake and syrup fuel may be used as a supplemental cementitious material in concrete or other cement containing materials. In addition, ash residue from burned filter cake or syrup may be used as a supplemental cementitious material in concrete or other cement containing materials. The ash from burned filter cake and syrup fuel, filter cake, or syrup may be added in addition to cement, or it may partially replace cement in concrete or other cement containing materials. In various embodiments, ash from burned filter cake and syrup fuel, filter cake, syrup, or any mixture of these materials is added to a concrete mixture. In one embodiment a concrete composition contains ash from burned filter cake and syrup fuel, filter cake, syrup or any mixture of these materials.

EXAMPLES

The present invention is further defined in the following Examples. It should be understood that these Examples, while indicating preferred embodiments of the invention, are given by way of illustration only. From the above discussion and these Examples, one skilled in the art can ascertain the essential characteristics of this invention, and without departing from the spirit and scope thereof, can make various changes and modifications of the invention to adapt it to various uses and conditions.

The meaning of abbreviations used is as follows: "s" is second, "min" means minute(s), "h" of "hr" means hour(s), "μΙ_" or "μΙ" means microliter(s), "mL" or "ml" means milliliter(s), "L" or "I" means liter(s), "m" is meter, "nm" means nanometer(s), "mm" means millimeter(s), "cm" means centimeter(s), "μηη" means micrometer(s), "mM" means millimolar, "M" means molar, "mmol" means millimole(s), "μιτιοΐβ" means micromole(s), "g" means gram(s), " g" means microgram(s), "mg" means milligram(s), "kg" is kilogram, "rpm" means revolutions per minute, "C" is Centigrade, "ppm" means parts per million, "cP" is centipoise, "g/l" means grams per liter, "SSU" is Saybolt Universal Viscosity in Seconds. Saccharification enzymes

Accellerase® 1500 (A1500) and Multifect® Xylanase are obtained from Danisco U.S. Inc., Genencor, International (Rochester, NY). Cellulase and Hemicellulase Production Strain

Strain 229: A Trichoderma reesei strain, derived from RL-P37 (Sheir- Neiss and Montenecourt, 1984, Appl. Microbiol. Biotechnol. 20:46-53) through mutagenesis and selection for high cellulase production, was co- transformed with the β-glucosidase expression cassette (cbhl promoter, T. reesei β-glucosidasel gene, cbhl terminator, and amdS marker), and the endoxylanase expression cassette (cbhl promoter, T. reesei xyn3, and cbhl terminator) using PEG mediated transformation (Penttila et al., 1987, Gene 61 (2):155-64). Numerous transformants were isolated and examined for β-glucosidase and endoxylanase production. One transformant, referred to as T. reesei strain #229, was used in certain studies described herein.

Strain H3A: T. reesei strain #229 was co-transformed with the β- xylosidase Fv3A expression cassette (cbhl promoter, Fv3A gene, cbhl terminator, and alsR marker), the β-xylosidase Fv43D expression cassette (egl1 promoter, Fv43D gene, native Fv43D terminator), and the Fv51A a- arabinofuranosidase expression cassette (egl1 promoter, Fv51A gene, Fv51A native terminator) using electroporation. Transformants were selected on Vogels agar plates containing chlorimuron ethyl. Numerous transformants were isolated and examined for β-xylosidase and L-a- arabinofuranosidase production. T. reesei integrated expression strain H3A, which recombinantly expresses T. reesei β-glucosidase 1 , T. reesei xyn3, Fv3A, Fv51A, and Fv43D was isolated."

Extra cellular protein produced during fermentation of strain H3A was separated from the cell mass by centrifugation, concentrated by membrane-ultrafiltration through a Millipore 10 kD molecular cut off weight membrane and pH adjusted to 4.8. Total protein was determined using a modified Biuret method as modified by Weichselbaum and Gornall using Bovine Serum Albumin as a calibrator (Weichselbaum, 1960, Amer. J. Clin. Path. 16:40; Gornall et al., 1949 J. Biol. Chem 177:752). This H3A extracellular protein preparation, called herein H3A protein, was used as a combination cellulase and hemicellulase preparation effecting complex carbohydrate hydrolysis during SSF.

Biocatalvst And Inoculum Preparation

Origin of the Zymomonas mobilis strains for Fermentation

A lignocellulosic biomass hydrolysate fermentation broth may be made using alternative biocatalysts. Exemplary strains are are described below. As an alternative, strain ZW658, deposited as ATCC #PTA-7858, may be used to produce a lignocellulosic biomass hydrolysate

fermentation broth for processing.

Zymomonas mobilis strain ZW705 was produced from strain

ZW801 -4 by the methods detailed in US 8,247,208, which is herein incorporated by reference, as briefly restated here. Cultures of Z. mobilis strain ZW801 -4 were grown under conditions of stress as follows. ZW801 - 4 is a recombinant xylose-utilizing strain of Z. mobilis that was described in US 7,741 ,1 19, which is herein incorporated by reference. Strain ZW801 -4 was derived from strain ZW800, which was derived from strain ZW658, all as described in US 7,741 ,1 19. ZW658 was constructed by integrating two operons, PgapxylAB and Pgaptaltkt, containing four xylose-utilizing genes encoding xylose isomerase, xylulokinase, transaldolase and transketolase, into the genome of ZW1 (ATCC #31821 ) via sequential transposition events, and followed by adaptation on selective media containing xylose. ZW658 was deposited as ATCC #PTA-7858. In ZW658, the gene encoding glucose-fructose oxidoreductase was insertionally-inactivated using host-mediated, double-crossover, homologous recombination and spectinomycin resistance as a selectable marker to create ZW800. The spectinomycin resistance marker, which was bounded by loxP sites, was removed by site specific recombination using Cre recombinase to create ZW801 -4. A continuous culture of ZW801 -4 was run in 250 ml stirred, pH and temperature controlled fermentors (Sixfors; Bottmingen, Switzerland). The basal medium for fermentation was 5 g/L yeast extract, 15 mM ammonium phosphate, 1 g/L magnesium sulfate, 10 mM sorbitol, 50 g/L xylose and 50 g/L glucose. Adaptation to growth in the presence of high concentrations of acetate and ammonia was effected by gradually increasing the concentration of ammonium acetate added to the above continuous culture media while maintaining an established growth rate as measured by the specific dilution rate over a period of 97 days. Ammonium acetate was increased to a concentration of 160 mM. Further increases in ammonium ion concentration were achieved by addition of ammonium phosphate to a final total ammonium ion concentration of 210 mM by the end of 139 days of continuous culture. Strain ZW705 was isolated from the adapted population by plating to single colonies and amplification of one chosen colony.

Strain AR3 7-31 was produced from strain ZW705 by further adaptation for growth in corn cob hydrolysate medium as disclosed in U.S. 8,476,048, which is incorporated herein by reference. ZW705 was grown in a turbidostat (US 6,686,194; Heurisko USA, Inc. Newark, DE), which is a continuous flow culture device where the concentration of cells in the culture was kept constant by controlling the flow of medium into the culture, such that the turbidity of the culture was kept within specified narrow limits. Two media were available to the growing culture in the continuous culture device, a resting medium (Medium A) and a challenge medium (Medium B). A culture was grown on resting medium in a growth chamber to a turbidity set point and then was diluted at a dilution rate set to maintain that cell density. Dilution was performed by adding media at a defined volume once every 10 minutes. When the turbidostat entered a media challenge mode, the choice of adding challenge medium or resting medium was made based on the rate of return to the set point after the previous media addition. The steady state concentration of medium in the growth chamber was a mix of Medium A and Medium B, with the proportions of the two media dependent upon the rate of draw from each medium that allowed maintenance of the set cell density at the set dilution rate. A sample of cells representative of the population in the growth chamber was recovered from the outflow of the turbidostat (in a trap chamber) at weekly intervals. The cell sample was grown once in

MRM3G6 medium and saved as a glycerol stock at -80 °C.

ZW705 was grown to an arbitrary turbidity set point that dictated that the culture use all of the glucose and approximately half of the xylose present in the incoming media to meet the set point cell density at the set dilution rate. Using resting medium that was 50% HYAc/YE and 50% MRM3G6.5X4.5NH ₄ Ac12.3 and challenge medium that was HYAc/YE. A strain isolated after 3 weeks was used in another round of turbidostat adaptation using HYAc/YE as the resting medium and HYAc/YE + 9 weight% ethanol as the challenge medium. Strain AR3 7-31 was isolated after 2 weeks and was characterized as a strain with improved xylose and glucose utilization, as well as improved ethanol production, in hydrolysate medium. By sequence analysis, AR3 7-31 was found to have a mutation in the Zymomonas mobilis genome ORF encoding a protein having characteristics of a membrane transport protein, and annotated as encoding a fusaric acid resistance protein.

Media

MRM3 contains per liter: yeast extract (10 g), KH ₂ PO (2 g) and MgSO ₄ .7H ₂ O (1 g)

MRM3G6 contains is MRM3 containing 60 g/L glucose

MRM3G6.5X4.5NH ₄ Ac12.3 is MRM3 containing 65 g/L glucose, 45 g/L xylose, 12.3 g/L ammonium acetate

HYAc/YE contains cob hydrolysate from which solids were removed by centrifugation and that was filter sterilized containing 68 g/L glucose, 46 g/L xylose and 5 g/L acetate, supplemented with 6.2 g/L ammonium acetate and 0.5% yeast extract, adjusted to pH5.8.

Liqnocellulosic biomass processing and fermentation Corn stover is milled to 3/8" (0.95 cm). Pretreatment is at 140 °C with 12% NH ₃ and 65% solids for 60 min. Saccharification is at 47 °C, pH 5.3, with 7.8 mg / g glucan+xylan of an enzyme consortium, for 96 hr. Saccharification enzymes are a mix of cellulases and hemicellulases expressed in a Trichoderma reesei strain H3A as described above. The resulting hydrolysate is used in fermentation. 10 mM sorbitol is added to the hydrolysate making the fermentation medium, and the pH is adjusted to 5.8.

For the seed, first frozen strain Zymomonas mobilis AR3 7-31 stock is grown in MRM3G6 (10 g/L BBL yeast extract, 2 g/L KH ₂ PO ₄ , 1 g/L MgSO ₄ ^* 7H ₂ O, 60 g/L glucose) at 33°C, without shaking for 8 hr as a revival culture. MRM3G10 medium (same as MRM3G6 but with 100 g/L glucose) is inoculated with revival culture, and incubated at 33 °C with shaking for 14 - 16 hr. Growth is to an OD ₆ oo between 1 .5 and 3.1 . The entire culture is used to inoculate a seed fermenter to an initial OD ₆ oo of approximately 0.05.

The seed fermentation is carried out in 10 g/L yeast extract, 2 g/L KH ₂ PO ₄ , 5 g/L MgSO ₄ ^* 7H ₂ O, 10 mM sorbitol, and 150 g/L glucose. Seed fermentation is performed at 33 °C and pH 5.5. Seed is harvested after first observation of glucose reduction to less than 50 g/L, with glucose measured by using a YSI 2700 SELECT™ Biochemistry Analyzer (YSI Life Sciences; Yellow Springs, OH).

The seed is added to the hydrolysate medium in the fermenter. Fermentations are carried out at 30 °C-33°C for 48-72 hr.

Lignocellulosic syrup and filter cake

The fermentation broth is distilled to recover ethanol and the remaining whole stillage is filtered using a membrane filter press. The liquid fraction is passed through a multi-effect evaporator train removing overhead water, and producing a lignocellulosic syrup. The solids fraction is a lignocellulosic filter cake.

Example 1 Preparation of filter cake and syrup fuel

Filter cake and syrup that were prepared as described in General Methods were combined in a mixer/dryer system that provides wet feed conditioning and flash drying capabilities for the filter cake and syrup co- products. The filter cake had a moisture content of about 45%. The syrup had a moisture content of about 45%-50%. The filter cake was size reduced in a delumper to a size of 0.5 inch (2.54 cm) or less. Pre-dried filter cake and syrup mixture with moisture content of 9.5%-17%, filter cake, and syrup were fed separately to a paddle mixer from spray nozzles. Filter cake was fed at 135-250 Ib/hr. Syrup was fed at 90-182 Ib/hr, and dried filter cake was fed at 1070-2645 Ib/hr.

After mixing, the contents were passed to a cage mill flash dryer and flash dried using dryer gas at about 225 °C to 250 °C to a moisture content between about 9.5% and 17%. The dried filter cake and syrup fuel product was then separated from the dryer gas stream. The gas was recompressed and reheated for recycle. A portion of the dryer gas was purged and treated for VOC reduction. A portion of the dried filter cake and syrup was separated to use as recycle solids (pre-dried filter cake and syrup mixture) in additional runs instead of pre-dried filter cake. The dried filter cake and syrup fuel product was cooled and conveyed to bulk storage.

Example 2 - prophetic

Fueling a cement process using filter cake and syrup fuel

Filter cake and syrup fuel prepared as described in Example 1 is transported, and delivered to the fuel handling system at a cement making facility, where it is stored. The fuel is metered from the storage bin and conveyed pneumatically to feed points in a pre-calciner, calciner or cement kiln and burned as fuel in the cement production process. Use of this fuel offsets use of fossil fuel or other alternative fuels to provide heat input required for cement production.