OA17466A

OA17466A - Processing biomass and energy.

Info

Publication number: OA17466A
Application number: OA1201500344
Authority: OA
Inventors: Marshall Medoff; Thomas Masterman; Solomon I. RODITI
Original assignee: Xyleco, Inc.
Priority date: 2013-03-08
Filing date: 2014-03-07
Publication date: 2016-12-30

Abstract

Biomass feedstocks (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful products, such as fuels, heat and energy.

Description

Many potential lignocellulosic feedstocks are available today, including agricultural residues, woody biomass, municipal waste, oilseeds/cakes and seaweed, to name a few. At présent, these materials are often under-utilized, being used, for example, as animal feed, biocompost materials, bumed in a co-generation facility or even landfilled.

Lignocellulosic biomass includes crystalline cellulose fibrils embedded in a hemicellulose matrix, surrounded by lignin. This produces a compact matrix that is difficult to access by enzymes and other chemical, biochemical and/or biological processes. Cellulosic biomass materials (e.g., biomass material from which the lignin has been removed) is more accessible to enzymes and other conversion processes, but even so, naturally-occurring cellulosic materials often hâve low yields (relative to theoretical yields) when contacted with hydrolyzing enzymes. Lignocellulosic biomass is even more récalcitrant to enzyme attack. Furthermore, each type of lignocellulosic biomass has its own spécifie composition of cellulose, hemicellulose and lignin.

SUMMARY

Many processes are disclosed herein for saccharifying or liquifying a biomass material, e.g., cellulosic, lignocellulosic and/or starchy feedstocks, by converting biomass material to low molecular weight sugars, e.g., saccharifying the feedstock using an enzyme, e.g., one or more cellulase and/or amylase. The invention also relates to converting a feedstock to a product, e.g., by bioprocessing, such as fermentation. The processes include utilizing residues from one or more stages of the process for energy génération.

In one aspect the invention relates to a method of generating energy including combusting a saccharified biomass material to produce energy. Optionally, the energy can be in the form of electric energy, heat energy or combinations of these. The saccharified material can include cells, such as cells selected from the group consisting of yeast cells, bacterial cells, fungal cells and mixtures of these cells. The cells can include whole cells (e.g., living, dormant and/or dead) or parts of cells (e.g., lysed and/or otherwise dead and destroyed cells). In addition or alternatively the saccharified material can include protein material (e.g., an enzyme material, a denatured enzyme material, peptides and/or amino acids). In addition or alternatively, the saccharified material can include inorganic solids, such as inorganic materials selected from the group consisting of diatomaceous earth, celite, silica, pumice, perlite, alumina, zeolites, sand and mixtures of any of these.

In some instances, the saccharified biomass material comprises lignocellulosic residue from lignocellulosic material that has been treated, for example with accelerated électrons from an électron accelerator, to reduce its recalcitrance prior to saccharification. For example, when treated with électrons, the électrons can hâve an average energy between about 0.3 MeV and about 5 MeV, such as between about 0.5 MeV and about 3.5 MeV or between about 0.8 MeV and about 2 MeV. The lignocellulosic biomass can be treated to a total dose between about 10 Mrad and about 100 Mrad, such as between about 15 Mrad and about 50 Mrad, between about 20 Mrad and about 45 Mrad, or between about 25 Mrad and about 40 Mrad. Optionally, the saccharified biomass is collected utilizing a rotary drum filter and/or a centrifuge, such as a decanter centrifuge, prior to combustion.

In some instances, the saccharified biomass material includes less than 60 percent moisture prior to it being combusted, such as less than about 55, 50, 45, 40, 35, 30, 25, 20,15 or even less than about 5 percent moisture. For example, the biomass can be dried so that is has less than about 60 percent moisture prior to combustion (e.g., dried to hâve less than 55, 50, 45, 35, 30, 25, 20, 15 or even less than 5 percent moisture). Optionally, the saccharified biomass material includes less than 35 percent by weight carbohydrates, such as less than 33, 30, 25, 20, 18, 16, 14, 12, 10 or even less than 8 percent on a dry basis. The saccharified material can be combusted and the combustion can produce greater than about 3500 BTU per pound, such as greater than about 4000,4500, 5000, greater than 6000 or even greater than about 7000 BTU per pound. Optionally, the saccharified biomass material has less than 50 percent moisture, such as less than 45 or 40 percent, and the combustion produces greater than about 4000 BTU per pound of the material. The saccharified biomass material can include less than 5 percent ash after combustion, such as less than 4, 3, 2.5, 2.0 or even less than 1.5 percent. In addition or altematively, the saccharified biomass material includes less than 0.5 percent sulfur, such as less than 0.4, 0.3,0.2,0.1 or even less than 0.075 or less than 0.05 percent sulfur.

In some other instances, a boiler is utilized during the combustion, for example, a boiler selected from the group consisting of a stoker grate boiler, a fluidized bed boiler and a co-fired boiler. For example, a co-fired boiler used for co-firing natural gas or coal can be utilized with the biomass. Altematively, during combustion, a gasifier is utilized, such as a fixed bed or a fluidized bed gasifier.

In another aspect the invention relates to a method of processing a biomass material. The method includes processing a first portion of lignocellulosic material into a product and a solid residue and combusting the solid residue in a boiler to produce steam. The method can include coupling the steam with a turbine to produce electricity. The energy produced (e.g., the heat from the steam and/or the electricity from the steam turbine) can be utilized to process a second portion of lignocellulosic material into a product. The processing of the biomass can include irradiating the biomass (e.g., with an électron beam) and optionally, saccharifying the irradiated biomass, for example with an enzyme. The saccharification can produce sugars, for example glucose and/or xylose. Optionally the processing of the lignocellulosic material can include fermentation.

In some instances, the solid residue is dried prior to being combusted, for example, such that the moisture content is reduced to less than about 25 wt.% water, e.g., less than about 20 wt.%, less than 15 wt.%, less than about 10 wt.%, less than about 5 wt.%, less than about 1 wt.% or even less than about 0.01 wt.%. The residue, when in dry form with less than about 5 wt.% water, can hâve an energy content of at least 4000 BTU per pound of residue. Optionally, the solid residue is dried using a screw dryer (e.g., a screw conveyor with a heated flights, shaft and/or trough). Optionally, the residue is combined with a drying agent, for example, a fine biomass material. For example, a dry biomass can be mixed in with the solid residue, wherein the content of dry biomass in the mixture is at least 1 wt.%, at least 2 wt.%, at least 3 wt.%, at least 4 wt.%, at least wt.%, at least 6 wt.%, at least 7 wt.%, at least 8 wt.%, at least 9 wt.%, at least 10 wt.%, at least 15 wt.%, at least 20 wt.% or even between about 20 wt.% and about 30 wt.%.

For example, the dry biomass can hâve a moisture content of less than about 25, 20, 15, 10, 5 or even less than about 1 percent moisture. For example, a fine biomass material can hâve a medium particle size less than about 1 mm, less than about 500 pm or less than about 100 pm. The combination of the residue with the dry biomass (e.g., fine biomass material) can dry or further dry the material. The amount can be added, in addition to, or alternatively to, drying to provide a dry material, such that the moisture content is reduced to less than about 25 wt.% water, e.g., less than about 20 wt.%, less than 15 wt.%, less than about 10 wt.%, less than about 5 wt.%, less than about 1 wt.% or even less than about 0.01 wt.%. The residue can be formed into a cake, pellet, densified shape, powder or combinations of these prior to being combusted (e.g., optionally under pressure, and/or while drying). The residue can include at least 0.1% (e.g., at least 0.2%, at least 0.5% or even at least 1%) nitrogen in the form of a nitrogen(III) compound, for example, the nitrogen compound can be or derived from the group consisting of proteins, denatured proteins, protein residues, amino acids, amino acid residues, urea, ammonia and combinations of these.

The biomass materials used can, for example, be selected from the group consisting of wood, particle board, sawdust, agricultural waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover, switchgrass, alfalfa, hay, coconut hair, seaweed, algae, and combinations and of these.

By utilizing the residues from many of the processes disclosed herein to provide energy (e.g., for co-generation), the cost of the feedstock conversion process can be

significantly reduced, both by reducing energy costs and minimizing the need for waste disposai. In addition, since the residues are biomass derived, the net carbon émissions for the entire process are close to zéro. As a resuit, the économie viability and profitability of the feedstock conversion process can be markedly enhanced. In addition, the residues from the processes hâve a high heat content since there can be a high lignin content in the residue e.g., higher than the feedstock such as a lignocellulosic material. Another advantage of some of the methods described herein is that the residues require little or even no drying since they can be combined with dry biomass such as fines produced in the processing of the biomass. In addition to providing a dryer material to combust, the dried material can be easier to convey. Finally, the methods can be advantageous because in some instances the residues can include organic nitrogen (ΙΠ) compounds that during combustion can react to reduce NOx émissions.

Implémentations of the invention can optionally include one or more of the following summarized features. In some implémentations, the selected features can be applied or utilized in any order while in other implémentations a spécifie selected sequence is applied or utilized. Individual features can be applied or utilized more than once in any sequence and even continuously. In addition, an entire sequence, or a portion of a sequence, of applied or utilized features can be applied or utilized once, repeatedly or continuously in any order. In some optional implémentations, the features can be applied or utilized with different, or where applicable the same, set or varied, quantitative or qualitative parameters as determined by a person skilled in the art For example, parameters of the features such as size, individual dimensions (e.g., length, width, height), location of, degree (e.g., to what extent such as the degree of recalcitrance), duration, frequency of use, density, concentration, intensity and speed can be varied or set, where applicable, as determined by a person of skill in the art.

Features, for example, include: methods of generating energy; generating heat energy; generating electrical energy; combusting a saccharified material to produce energy; combusting a saccharified material that includes cells; combusting a saccharified material that includes yeast cells; combusting a saccharified material that includes fungal cells; combusting a saccharified biomass that includes protein material; combusting a saccharified biomass that includes an enzyme material; combusting a saccharified biomass that includes denatured enzyme material; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated to reduce its recalcitrance prior to saccharification; combusting a saccharified

lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons to reduce its recalcitrance prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons having an average energy between about 0.3 MeV and 5 about 5 MeV prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons having an average energy between about 0.5 MeV and about 3.5 MeV prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons having an average energy between about 0.8 MeV and about 2 MeV prior to saccharification; combusting a saccharide lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons to a total dose between about 10 Mrad and about 100 Mrad prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons to a total dose between about 15 Mrad and about 50 Mrad prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been treated with accelerated électrons to a total dose between about 20 Mrad and about 45 Mrad prior to saccharification; combusting a saccharified lignocellulosic residue derived from lignocellulosic material that has been 20 treated with accelerated électrons to a total dose between about 25 Mrad and about 40

Mrad prior to saccharification; combusting a saccharified material that includes inorganic solids; combusting a saccharified material that includes diatomaceous earth; combusting a saccharified material that includes silica; combusting a saccharified material that includes pumice; combusting a saccharified material that includes perlite;

combusting a saccharified material that includes alumina; combusting a saccharified material that includes zeolites; combusting a saccharified material that includes zeolites; combusting a saccharified material that includes sand; combusting a saccharified material that includes less than 60 percent moisture; combusting a saccharified material that includes less than 50 percent moisture; combusting a saccharified material that includes less than 45 percent moisture; combusting a saccharified material that includes less than 40 percent moisture; combusting a saccharified material that includes less than 30 percent moisture; combusting a saccharified material that includes less than 20 percent moisture; combusting a saccharified material that includes less than 10 percent moisture; combusting a saccharified material that includes less than 5 percent moisture;

combusting a saccharified material that includes less than 0.5 percent sulfur; producing greater than about 3500 BTU of energy per pound by the combustion of a saccharified biomass material; producing greater than about 4000 BTU/lb of energy by the combustion of a saccharified biomass material; producing greater than about 4500 BTU/lb of energy by the combustion of a saccharified biomass material; producing greater than about 5000 BTU/lb of energy by the combustion of a saccharified biomass material; producing greater than about 6000 BTU/lb of energy by the combustion of a saccharified biomass material; producing greater than about 7000 BTU/lb of energy by the combustion of a saccharified biomass material; combusting a saccharified biomass material that includes less than 35 percent by weight carbohydrates on a dry basis; combusting a saccharified biomass material that includes less than 30 percent by weight carbohydrates on a dry basis; combusting a saccharified biomass material that includes less than 25 percent by weight carbohydrates on a dry basis; combusting a saccharified biomass material that includes less than 20 percent by weight carbohydrates on a dry basis; combusting a saccharified biomass material that includes less than 10 percent by weight carbohydrates on a dry basis; combusting a saccharified biomass material utilizing a boiler; combusting a saccharified biomass material utilizing a stoker grate boiler; combusting a saccharified biomass material utilizing a fluidized bed boiler; combusting a saccharified biomass material utilizing a co-fired boiler; utilizing a gasifier while combusting a saccharified biomass material; collecting the solids from a saccharified biomass material using a rotary drum filter and combusting the collected material; collecting the solids of a biomass material using a centrifuge and combusting the collected material.

Features, for example, can also include; processing a biomass material; processing a portion of a lignocellulosic material into a product and a solid residue; combusting a solid residue in a boiler to produce steam; coupling steam to a turbine to produce electricity; using steam and electricity to process a portion of a lignocellulosic material into a product; using steam to process a portion of a lignocellulosic material into a product; using electricity to process a portion of a lignocellulosic material into a product; irradiating a lignocellulosic material; saccharifying a lignocellulosic material; producing glucose by saccharifying a lignocellulosic material; producing xylose by saccharifying a lignocellulosic material; fermenting a lignocellulosic material; drying a solid residue prior to combusting the solid residue; reducing the moisture content of a solid residue to less than about 25 wt.% water prior to combusting the solid; reducing the

moisture content of a solid residue to less than about 20 wt.% water prior to combusting the solid; reducing the moisture content of a solid residue to less than about 15 wt.% water prior to combusting the solid; drying a solid residue using a screw dryer prior to combusting the solid; combining a solid residue with a drying agent prior to combusting the solid residue; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 1 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 2 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 3 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 4 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 5 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 6 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 7 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 8 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 9 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 10 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 15 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is at least 20 wt.%; combining a solid residue with a dry biomass wherein the content of the dry biomass in the mixture is between about 20 wt.% and 30wt.%; combining a solid residue with a dry biomass wherein the dry biomass has a moisture content less than about 25 percent; combining a solid residue with a dry wherein the dry biomass has a moisture content less than about 20 percent; combining a solid residue with a dry wherein the dry biomass has a moisture content less than about 15 percent; combining a solid residue with a dry wherein the dry biomass has a moisture content less than about 10 percent; combining a solid residue with a dry wherein the dry biomass has a moisture content less than about 5 percent; combining a solid residue with a dry wherein the dry biomass has a moisture content less than about 1 percent; combining a solid residue with a fine biomass material prior to combusting the solid residue; a dry biomass can include a fine biomass material; combining a solid residue with a biomass material having a medium particle size of less than about 1 mm prior to combusting the solid residue; combining a solid residue with a biomass material

having a medium particle size of less than about 500 micro meters prior to combusting the solid residue; forming a residue into cakes prior to combusting the residue; forming a residue into pellets prior to combusting the residue; forming a residue into densified shapes prior to combusting the residue; forming a residue into powder prior to combusting the residue; combusting a residue that has an energy content of at least 4000 BTU per pound when it is in a dry form with less than 5 wt.% water; combusting a residue that includes 0.1% nitrogen in the form of a nitrogen(III) compound; combusting a residue that includes 0.1% nitrogen provided from proteins; combusting a residue that includes 0.1% nitrogen provided from protein residues; combusting a residue that includes 0.1% nitrogen provided from amino acids; combusting a residue that includes 0.1% nitrogen provided from amino acid residues; combusting a residue that includes 0.1% nitrogen provided from urea; combusting a residue that includes 0.1% nitrogen provided from ammonia; processing a lignocellulosic material that includes wood; processing a lignocellulosic material that includes particle board; processing a lignocellulosic material that includes sawdust; processing a lignocellulosic material that includes agricultural waste; processing a lignocellulosic material that includes sewage; processing a lignocellulosic material that includes silage; processing a lignocellulosic material that includes grasses; processing a lignocellulosic material that includes rice hulls; processing a lignocellulosic material that includes bagasse; processing a lignocellulosic material that includes cotton; processing a lignocellulosic material that includes jute; processing a lignocellulosic material that includes hemp; processing a lignocellulosic material that includes flax; processing a lignocellulosic material that includes bamboo; processing a lignocellulosic material that includes sisal; processing a lignocellulosic material that includes abaca; processing a lignocellulosic material that includes straw; processing a lignocellulosic material that includes com cobs; processing a lignocellulosic material that includes com stover; processing a lignocellulosic material that includes switchgrass; processing a lignocellulosic material that includes alfalfa; processing a lignocellulosic material that includes hay; processing a lignocellulosic material that includes coconut haïr; processing a lignocellulosic material that includes seaweed; processing a lignocellulosic material that includes algae;

Ail publications, patent applications, patents, and other references mentioned herein or attached hereto are incorporated by reference in their entirety for ail that they contain.

DESCRIPTION OF THE DRAWINGS

FIG. 1 is a flow diagram showing an example of a co-generation process.

FIG. 2 is a diagram illustrating the flow of fuel to the co-generation facility and flow of energy back to various steps in the feedstock conversion process.

DETAILED DESCRIPTION

Using the Systems, equipment and methods described herein, biomass (e.g., plant biomass, animal biomass, paper, and municipal waste biomass) can be processed to produce useful intermediates, products and energy, for example by cogénération..

Cogénération, also known as Combined Heat and Power (CHP) is the simultaneous production of electricity and heat from a single fuel source, or multiple fuel sources in the case of co-firing. Some biomass processing methods and Systems are described in Biomass Technology Review, October 21, 2010, pages 1 to 52 by McHale and Associâtes, Inc. and Biomass Conversion Technologies, by the EPA Combined Heat and Power Partnership accessed by internet on Feb 27, 2013 pages 30 to 61 at www.epa.gov; the entire disclosures of which are herein incorporated by attachment in the appendix. Any process, equipment or system described in this document, attached in the appendix, can be used in/with any process, equipment or system described anywhere herein. For example, Stoker grate underfired stoker boilers can be used to bum saccharified biomass.

FIG. 1 shows an example of a cogénération process. Initially, boiler feed water 10 and fuel sources 20 are fed to one or more boilers 30. The fuel sources include the solid residues discussed herein, and may optionally include other fuels such as natural gas, waste gases generated by the feedstock conversion process, and/or a portion of the feedstock used in the feedstock conversion process. Steam is generated in the boilers, which is input to one or more super heaters 40, which super heat the steam, e.g., to 500 PSIG and 650 DEG F. This steam is then injected into one or more turbines 50, where it tums dises or other turbine éléments, which in turn rotate a shaft generating mechanical energy. This mechanical energy is then input to a generator, where it is converted to electricity 70. Meanwhile, cooled steam exhausted from the turbines, which is still at elevated température and pressure (e.g., 80 PSIG and 310 DEG F), can be utilized in the feedstock conversion plant for heating or other purposes 60. Electrical energy from the generator (e.g., at 4160 Volts) is passed to transformers, e.g., two transformers, where it is stepped down to allow its use in the plant 80 (e.g., to 480 Volts) and/or stepped up for export to the grid 90 (e.g., to 113,000 Volts).

Details of these and other steps in a cogénération process according to one implémentation will now be described.

In some embodiments the materials to be used are dried. The solid residues from the various stages of the feedstock conversion process may in some cases hâve a moisture content of from about 10% to 50% or more. This relatively high moisture content can impact the operation of the boiler, in that some of the energy in the boiler will be consumed in vaporizing the moisture, thus reducing the température and efficiency of the boiler. Thus, in some implémentations, the solid residue is dried prior to being combusted, for example to a moisture content of less than about 60 wt.%, ( e.g., less than about 55 wt.%, less than about 50 wt.%, less than about 45 wt.%, less than , about 40 wt.%, less than about 35 wt.%, less than about 30 wt.%, less than about 25 wt%, less than about 20 wt%, less than about 15 wt.%, less than about 10 wt.%, or even less than about 5 wt.%.

In some implémentations the cogénération System is equipped with a screw type dryer that is used to heat dry the wet residue. For example an indirect heat exchanger may be used to heat bulk biomass solids, filter cakes, paste and/or sludge.

The dryer may be, for example, a Hollow Flite Screw Dryer. In this type of dryer individual particles are heated as they corne in contact with the outer surfaces of hollow flights, shaft and trough which contain a heat transfer material, e.g., a thermal oil. There is no contamination of the material being dried, as it does not corne in contact with the heat transfer material. The product is continuously conveyed in an axial direction by rotating screw flights along a jacketed trough. The dryer uses indirect heat exchange, providing excellent product température control. The heat transfer material is also recycled, minimizing heat losses and increasing efficiency. The thermal energy used to heat the heat transfer fluid is preferably provided by the power produced by the cogénération process.

In other implémentations, the wet residue may be dried by utilizing heat from anywhere and including the boiler and the heating stack. For example hot gases from the boiler can be used, or heat from a stack (e.g., utilizing a heat exchanger).

In addition or alternatively to drying of the residues as described above, the residues can be combined with a drying agent such as a dry biomass. For example, a dry biomass can hâve less water content than the residues, to adjust the total average water content. For example, the dry biomass can, hâve a moisture content of less than about 25, 20, 15, 10, 5 or even less than about 1 percent moisture. The dry biomass can be sourced, for example, from incoming un-processed biomass as well as any biomass that has been processed by the methods described herein (e.g., fines from the comminution step). For example, a dry biomass can be mixed in with a wet residue from processing described herein, wherein the content of dry biomass in the mixture is at least 1 wt.%, at least 2 wt.%, at least 3 wt.%, at least 4 wt.%, at least 5 wt.%, at least 6 wt.%, at least 7 wt.%, at least 8 wt.%, at least 9 wt.%, at least 10 wt.%, at least 15 wt.%, at least 20 wt.% or even between about 20 wt.% and about 30 wt.%. For example, a residue derived from saccharified biomass can be combined with non-saccharified biomass. The fine biomass material can hâve a medium particle size less than about 1mm (e.g., 500 pm or 100 pm). Preferably the drying agent has moisture content lower than that of the wet residue.

Optionally dried material is conveyed to the boiler operations. In some implémentations, solid residues are delivered to the boiler via conveyors that initially deliver the residues into a storage area near the boiler room. In the storage area the biomass is optionally blended with other unused raw biomass and then loaded into a storage bin. The storage bin is fitted with hydraulically driven pusher plates that constantly transport solid fuel to a through-chain conveyor, which supplies fuel to the infeed section of the boiler. The hydraulically driven in-feed conveyor is also fitted with a pusher plate that pushes the fuel into metering “dump bins.” The metering bins dump the fuel into the combustion chamber in the boiler. These dump bins are helpful in delivering wet residues, which may be difficult to feed using a hopper or other typical feeding technique due to their possible agglomération and poor flow properties.

Once the fuel is in the combustion chambers, the biomass is subjected to a thermochemical combustion process under oxygen déficit conditions, leading to the production of hot (>1800 DEG F) gases and the dégradation of the biomass. The biomass (e.g., saccharified biomass) can produce greater than 3500 BTU per pound, such as greater than 4000,4500, 5000, greater than 6000 or even greater than 7000 BTU per pound. The biomass is converted to ash. The ash content of the biomass can be less than 5 wt.%, (e.g., less than about 4 wt.%, less than about 3 wt.%, less than about 2.5 wt.%, less than about 2.0 wt.%, less than about 1.5 w.t.%). The sulfur content of the saccharified biomass can be less than about 0.5 % (e.g., less than about 0.4, 0.3, 0.2,0.1, 0.075 or even less than about 0.05). The resulting hot gases travel to an upper drum in the boiler where the water is vaporized to steam. The steam then passes to the super heater where it is heated further by the hot flue gases. The resulting steam rate from both boilers may be, for example, 103,000 PPH (pounds per hour), at 500 PSIG and 650 DEG F.

To maintain proper operation of the boilers, in some implémentations each boiler is fitted with an economizer and a recuperater to capture ail the waste heat from the flue gas. The economizer heats up the boiler feed water before it enters the upper drum where a water level is always maintained to continuously supply steam; the recuperater also heats up fresh air, which is supplied by a forced draft fan to maintain combustion in the boiler.

The boiler feed water travels around the perimeter of the boiler through inner tubes, and loops around between the upper drum and a lower drum as it is further heated.

Occasionally, a boiler blow down may be performed, during which water from the lower drum is dumped and replaced with fresh boiler feed water. This operation may be done either manually or automatically and is used to remove the dissolved solids and particles entering the boiler through the make-up water.

If the dissolved solids are not removed they will build up and finally the concentration will reach a level where the boiler operation becomes impossible. In addition, if solids are not purged from the boiler they can lead to scale formation, canyover, corrosion, and/or embrittlement

In some embodiments, the flue gas is directed from the super heater, the economizer, and the recuperator to an Electrostatic Precipitator by an induced draft. The Electrostatic Precipitator, discussed below, removes particulate material from the flue gas and may in some cases be more effective than a bag house.

The Electrostatic Precipitator contains six major components: discharge électrodes, collection électrodes, rappers, hoppers, outer shell, and an electric system.

The discharge électrodes release an electric charge, usually négative, to pollutant particles in the gas stream. The collection électrodes, which may be, for example, tubes or plates, collect the charged particles and hâve a charge opposite to that of the discharge électrodes which causes the particles to migrate toward them.

The particles are removed from the électrodes by the rappers, which provide vibration or shock to both the collection and discharge électrodes causing the particles to fall into the hoppers where they are temporarily stored.

The outer shell encloses the eiectrodes and supports the precipitator components. The shell is covered with insulation to conserve heat and prevent corrosion. The outer shell and be made of steel.

The electric System, also called the transformer-rectifier, controls the strength of the electric field between the discharge and collection eiectrodes. The electric System used standard current 480 volts and steps it up to as high as 70,000 volts. The rectifier part of the electric System converts the current from altemating to direct current.

The flue gas exiting the electrostatic precipitator is free or substantially free of particles but can contain NOx compounds. NOx is a generic term for mono-nitrogen 10 oxides (e.g., NO and NO2). These oxides are produced during combustion, especially combustion at high températures. The removal technology of NOx is used universally by the Sélective Catalytic Réduction (SCR) technique. The NOx réduction process includes the injection of ammonia (NH3) into flue gas stream in the presence of catalyst where the NOx reacts selectivity with NH3 and is converted into nitrogen (N2) and water (H2O).

The main reaction is expressed as follows.

4NO + 4NH₃ + 02^ 4N₂ + 6H2O

The flue gas is then passed through continuons monitoring equipment (CEM) before it is discharged to the atmosphère. CEM is a technique for the continuous measurement of pollutants emitted into the atmosphère in exhaust gases from 20 combustion or industrial processes. The EPA has established requirements for the continuous monitoring of SO2, volumétrie flow, NOx, diluent gas, and opacity, for facilities regulated under the Acid Rain Program. In addition, CEM is instrumental in ensuring that procedures for the mandated réductions of SO2 and NOx are followed. After it is monitored by CEM the exhaust gas is then allowed to exit to the atmosphère 25 through an exhaust stack at température between 300F - 400 DEG F range.

High pressure steam at 500 PSIG and 650 DEG F is fed to an extraction condensing steam turbine at a rate of 100,000 PPH. As it passes through the turbine dises or blades, the steam is then extracted at 80 PSIG saturated steam for the use in the feedstock conversion plant. In the condensing cycle, the steam leaves the turbine and 30 flows toward a condenser where it is re-converted into water and directed to a hot well and then to the boiler as feed water.

Meanwhile, the steam energy causes the turbine shaft to spin, which drives an electrical generator. The potential electric power generated may be, for example, between about 4 to 7 Mégawatts.

The electric generator works on the principle of electromagnetic induction, which créâtes a voltage différence between the two ends of a wire or electrical conductor, which in turn causes electric charges to flow, thus generating electric current.

The electric current is fed to electric station switchgear backed up by an uninterruptible power supply, the electric current approx. 4000 volts is stepped-down through a transformer to 480 volts for use in the feedstock conversion plant. Excess electric current at 4000 volts is stepped-up via step-up transformer to 113,000 V for grid export.

An example of flow of fuel (e.g. residues, co-products, waste, impurities from various processes) to a cogénération facility 200 and flow of energy generated from these fuels into a feedstock conversion process is shown in FIG. 2. The figure shows a cogénération plant 200 (e.g., part of a larger bioprocessing plan) surrounded by various processes. The double arrows indicate movement of energy from the co-generation plant to the various processes, and material from the processes to the co-generation plant. Single arrows indicate a possible flow for the processes in the biomass processing plant.

In biomass processing, a comminution step may be advantageous, and can be an initial step in the biomass conversion plant. Comminuting biomass 210, e.g., with one or more of the mechanical treatments discussed herein, can resuit in fine particles that are difficult to process in subséquent processing steps. Rather than discarding these fines, these can be input into the cogénération process, for example, as a drying agent. Comminution also requires a considérable input of energy, some or ail of which can be obtained from the cogénération process.

Other pre-processing steps, e.g., steps used to reduce the recalcitrance of the biomass material 220, may also generate residues that are unusable for the primary processes (e.g., Process 1, 230 or Process 2, 240) but that can be input into the cogénération process. For example, pre-processing can produce lignin, feedstock that has been deleteriously affected by the preprocessing (e.g., decomposed, made toxic, contaminated) and/or fines (e.g., produced during pneumatic/vibratory conveying and collected by a bag house or by other screening). The pre-processing also require energy, e.g., steam heat and/or electricity (e.g., for various power sources such as irradiation equipment and conveying equipment).

Primary Process 1, 230 (e.g., saccharification) produce a significant amount of solid residues, containing for example lignin, minerais, proteins, fats, enzymes, denatured enzymes, and other components. In addition to being used, for example, as feed or nutrients for animais, plants or organisais, these iesidues, or a subset or portion of these residues, can be input to the cogénération process. The energy from the cogénération process can be used in the saccharification process. For example, steam or heat generated from résistive heating can be used to maintain a desired température of a saccharifying mixture during saccharification. The energy can also be used for mechanical mixing, e.g., using jet mixers and/or other mixers as described herein.

Primary Process 2, 240 (e.g., fermentation) generates solid residues containing, for example, in addition to the materials found in saccharified residues, yeast cells, bacterial cells, fungal cells or mixtures of these cells. In addition to uses as, for example nutrients for animais and organisms, the residues can be input to the cogénération process and the energy utilized to maintain the desired fermentation température.

The saccharified and optionally fermented biomass material as described above can include less than 35 percent by weight carbohydrates, such as less than 33, 30, 25, 20, 18, 16, 14, 12, 10 or even less than 8 percent on a dry basis. Carbohydrate depleted biomass can hâve a high heat content. For example, as described below dry lignin can hâve an energy content of between about 11,000 and 12,500 BTU per pound, compared to 7,000 an 8,000 BTU per pound of holocellulose.

Further processing, including isolation/concentration and or purification 250 of products and or intermediates can also generate by by-products (e.g., waste) that can be used as fuel for the co-generation plant. For example, steps such as by distillation, filtration and centrifugation (e.g., a decanter centrifuge, a continuous centrifuge) can ail generate solids with high energy contents. These processes also require energy, for example heating for distillation, and electricity for centrifugation, that can be tapped from the co-generation plant.

Post processing 260 (e.g., packaging, distribution and/or storage) require energy for various processes. For example electricity may be needed for packing equipment, conveyors (e.g., for distribution), and climate control (e.g., for storage). These processes can also generate some waste, for example expired products, packaging waste that can used as a contribution to fuel the co-generation plant.

The isolated solids/residues can include inorganic materials, for example including diatomaceous earth, such as celite, a glass, such as a silica glass, such as volcanic amorphous glass, such as perlite, a cellulosic or lignocellulosic material, silica, alumina, zeolite, sand or mixtures of any of these filter aids. For example, filter aids used dunng Rotary Vacuum Drum Filtration (RVDF) for removing solid residues after saccharification, fermentation and/or distillation.

Some more details and réitérations of processes for treating a feedstock that can be utilized, for example, with the embodiments already discussed above, or in other embodiments, are described in the following disclosures. In particuiar, the residues discussed herein can be generated, for example, as a resuit of the feedstock treatment and processing steps described in the following sections.

SYSTEMS FOR TREATING A FEEDSTOCK

Processes for conversion of a feedstock to sugars and other products, in which the methods discussed above may be used (e.g., wherein the feedstock for co-generation can be produced and/or wherein the energy produced by co-gen can be utilized), can include, for example, optionally physically pre-treating the feedstock, e.g., to reduce its size, before and/or after this treatment, optionally treating the feedstock to reduce its recalcitrance (e.g., by irradiation), and saccharifying the feedstock to form a sugar solution. Saccharification can be performed by mixing a dispersion of the feedstock in a liquid medium, e.g., water with an enzyme, as will be discussed in detail below. During or after saccharification, the mixture (if saccharification is to be partially or completely performed en route) or solution can be transported, e.g., by pipeline, railcar, truck or barge, to a manufacturing plant. At the plant, the solution can be bioprocessed, e.g., fermented, to produce a desired product or intermediate, which can then be processed further, e.g., by distillation. The individual processing steps, materials used and examples of products and intermediates that may be formed will be described in detail below

RADIATION TREATMENT

The feedstock can be treated with radiation to modify its structure to reduce its recalcitrance. Such treatment can, for example, reduce the average molecular weight of the feedstock, change the crystalline structure of the feedstock, and/or increase the surface area and/or porosity of the feedstock. Radiation can be by, for example électron beam, ion beam, 100 nm to 280 nm ultraviolet (UV) light, gamma or X-ray radiation. Radiation treatments and Systems for treatments are discussed in U.S. Patent 8,142,620,

and U.S. Patent Application Sériés No. 12/417,731, the entire disclosures of which are incorporated herein by reference.

Each form of radiation ionizes the biomass via particular interactions, as determined by the energy of the radiation. Heavy charged particles primarily ionize matter via Coulomb scattering; furthermore, these interactions produce energetic électrons that may further ionize matter. Alpha particles are identical to the nucléus of a hélium atom and are produced by the alpha decay of various radioactive nuclei, such as isotopes of bismuth, polonium, astatine, radon, francium, radium, several actinides, such as actinium, thorium, uranium, neptunium, curium, californium, américium, and o plutonium. Electrons interact via Coulomb scattering and bremsstrahlung radiation produced by changes in the velocity of électrons.

When particles are utilized, they can be neutral (uncharged), positively charged or negatively charged. When charged, the charged particles can bear a single positive or négative charge, or multiple charges, e.g., one, two, three or even four or more charges.

In instances in which chain scission is desired to change the molecular structure of the carbohydrate containing material, positively charged particles may be désirable, in part, due to their acidic nature. When particles are utilized, the particles can hâve the mass of a resting électron, or greater, e.g., 500, 1000, 1500, or 2000 or more times the mass of a resting électron. For example, the particles can hâve a mass of from about 1 atomic unit to about 150 atomic units, e.g., from about 1 atomic unit to about 50 atomic units, or from about 1 to about 25, e.g., 1, 2, 3, 4, 5, 10, 12 or 15 atomic units.

Gamma radiation has the advantage of a significant pénétration depth into a variety of material in the sample.

In embodiments in which the irradiating is performed with electromagnetic radiation, the electromagnetic radiation can hâve, e.g., energy per photon (in électron volts) of greater than 10² eV, e.g., greater than 10³, 10⁴, 10⁵, 10⁶, or even greater than 10⁷eV. In some embodiments, the electromagnetic radiation has energy per photon of between 10⁴ and 10⁷, e.g., between 10⁵ and 10⁶ eV. The electromagnetic radiation can hâve a frequency of, e.g., greater than 10¹⁶ Hz, greater than 10¹⁷ Hz, 10¹⁸, ΙΟ¹⁹, 10²⁰, or even greater than 10²¹ Hz. In some embodiments, the electromagnetic radiation has a frequency of between 10¹⁸ and 10²² Hz, e.g., between 10¹⁹ to 10²¹ Hz.

Electron bombardment may be performed using an électron beam device that has a nominal energy of less than 10 MeV, e.g., less than 7 MeV, less than 5 MeV, or less

than 2 MeV, e.g., from about 0.5 to 1.5 MeV, from about 0.8 to 1.8 MeV, or from about 0.7 to 1 MeV. In some implémentations the nominal energy is about 500 to 800 keV.

The électron beam may hâve a relatively high total beam power (the combined beam power of ail accelerating heads, or, if multiple accelerators are used, of ail accelerators and ail heads), e.g., at least 25 kW, e.g., at least 30, 40, 50, 60, 65, 70, 80, 100, 125, or 150 kW. In some cases, the power is even as high as 500 kW, 750 kW, or even 1000 kW or more. In some cases the électron beam has a beam power of 1200 kW or more, e.g., 1400, 1600,1800, or even 3000 kW.

This high total beam power is usually achieved by utilizing multiple accelerating heads. For example, the électron beam device may include two, four, or more accelerating heads. The use of multiple heads, each of which has a relatively low beam power, prevents excessive température rise in the material, thereby preventing buming of the material, and also increases the uniformity of the dose through the thickness of the layer of material.

It is generally preferred that the bed of biomass material has a relatively uniform thickness. In some embodiments the thickness is less than about 1 inch (e.g., less than about 0.75 inches, less than about 0.5 inches, less than about 0.25 inches, less than about 0.1 inches, between about 0.1 and 1 inch, between about 0.2 and 0.3 inches).

It is désirable to treat the material as quickly as possible. In general, it is preferred that treatment be performed at a dose rate of greater than about 0.25 Mrad per second, e.g., greater than about 0.5, 0.75, 1, 1.5, 2, 5, 7, 10, 12, 15, or even greater than about 20 Mrad per second, e.g., about 0.25 to 2 Mrad per second. Higher dose rates allow a higher throughput for a target (e.g., the desired) dose. Higher dose rates generally require higher line speeds, to avoid thermal décomposition of the material. In one implémentation, the accelerator is set for 3 MeV, 50 mA beam current, and the line speed is 24 feet/minute, for a sample thickness of about 20 mm (e.g., comminuted com cob material with a bulk density of 0.5 g/cm³).

In some embodiments, électron bombardment is performed until the material receives a total dose of at least 0.1 Mrad, 0.25 Mrad, 1 Mrad, 5 Mrad, e.g., at least 10, 20, 30 or at least 40 Mrad. In some embodiments, the treatment is performed until the material receives a dose of from about 10 Mrad to about 50 Mrad, e.g., from about 20 Mrad to about 40 Mrad, or from about 25 Mrad to about 30 Mrad. In some implémentations, a total dose of 25 to 35 Mrad is preferred, applied ideally over a couple of passes, e.g., at 5 Mrad/pass with each pass being applied for about one second.

Cooling methods, Systems and equipment can be used before, during, after and in between radiations, for example utilizing a cooling screw conveyor and/or a cooled vibratory conveyor.

Using multiple heads as discussed above, the material can be treated in multiple passes, for example, two passes at 10 to 20 Mrad/pass, e.g., 12 to 18 Mrad/pass, separated by a few seconds of cool-down, or three passes of 7 to 12 Mrad/pass, e.g., 5 to 20 Mrad/pass, 10 to 40 Mrad/pass, 9 to 11 Mrad/pass. As discussed herein, treating the material with several relatively low doses, rather than one high dose, tends to prevent overheating of the material and also increases dose uniformity through the thickness of the material. In some implémentations, the material is stirred or otherwise mixed during or after each pass and then smoothed into a uniform layer again before the next pass, to further enhance treatment uniformity.

In some embodiments, électrons are accelerated to, for example, a speed of greater than 75 percent of the speed of light, e.g., greater than 85, 90, 95, or 99 percent of 15 the speed of light.

In some embodiments, any processing described herein occurs on lignocellulosic material that remains dry as acquired or that has been dried, e.g., using heat and/or reduced pressure. For example, in some embodiments, the cellulosic and/or lignocellulosic material has less than about 25 wL % retained water, measured at 25°C and at fifty percent relative humidity (e.g., less than about 20 wt.%, less than about 15 wt.%, less than about 14 wt.%, less than about 13 wt.%, less than about 12 wt.%, less than about 10 wt.%, less than about 9 wt.%, less than about 8 wt.%, less than about 7 wt.%, less than about 6 wt.%, less than about 5 wt.%, less than about 4 wt.%, less than about 3 wt.%, less than about 2 wt.%, less than about 1 wt.%, or less than about 0.5

Wt.%.

In some embodiments, two or more ionizing sources can be used, such as two or more électron sources. For example, samples can be treated, in any order, with a beam of électrons, followed by gamma radiation and UV light having wavelengths from about

100 nm to about 280 nm. In some embodiments, samples are treated with three ionizing radiation sources, such as a beam of électrons, gamma radiation, and energetic UV light.

The biomass is conveyed through the treatment zone where it can be bombarded with électrons.

It may be advantageous to repeat the treatment to more thoroughly reduce the recalcitrance of the biomass and/or further modify the biomass. In particular the process parameters can be adjusted after a first (e.g., second, third, fourth or more) pass depending on the recalcitrance of the material. In some embodiments, a conveyor can be used which includes a circular system where the biomass is conveyed multiple times through the various processes described above. In some other embodiments, multiple treatment devices (e.g., électron beam generators) are used to treat the biomass multiple (e.g., 2, 3, 4 or more) times. In yet other embodiments, a single électron beam generator may be the source of multiple beams (e.g., 2, 3, 4 or more beams) that can be used for treatment of the biomass.

The effectiveness in changing the molecular/supermolecular structure and/or reducing the recalcitrance of the carbohydrate-containing biomass dépends on the électron energy used and the dose applied, while exposure time dépends on the power and dose. In some embodiments, the dose rate and total dose are adjusted so as not to destroy (e.g., char or bum) the biomass material. For example, the carbohydrates should not be damaged in the processing so that they can be released from the biomass intact, e.g. as monomeric sugars.

In some embodiments, the treatment (with any électron source or a combination of sources) is performed until the material receives a dose of at least about 0.05 Mrad, e.g., at least about 0.1, 0.25,0.5,0.75, 1.0, 2.5, 5.0, 7.5, 10.0, 15, 20, 25, 30, 40, 50, 60, 70, 80, 90, 100, 125, 150, 175, or 200 Mrad. In some embodiments, the treatment is performed until the material receives a dose of between 0.1-100 Mrad, 1-200, 5-200, 10200, 5-150, 50-150 Mrad, 5-100, 5-50, 5-40, 10-50, 10-75, 15-50, 20-35 Mrad.

In some embodiments, relatively low doses of radiation are utilized, e.g., to increase the molecular weight of a cellulosic or lignocellulosic material (with any radiation source or a combination of sources described herein). For example, a dose of at least about 0.05 Mrad, e.g., at least about 0.1 Mrad or at least about 0.25, 0.5,0.75. 1.0, 1.5, 2.0, 2.5, 3.0, 3.5,4.0, or at least about 5.0 Mrad. In some embodiments, the irradiation is performed until the material receives a dose of between 0.1 Mrad and 2.0 Mrad, e.g., between 0.5rad and 4.0 Mrad or between 1.0 Mrad and 3.0 Mrad.

It also can be désirable to irradiate from multiple directions, simultaneously or sequentially, in order to achieve a desired degree of pénétration of radiation into the material. For example, depending on the density and moisture content of the material, such as wood, and the type of radiation source used (e.g., gamma or électron beam), the maximum pénétration of radiation into the material may be only about 0.75 inch. In such a cases, a thicker section (up to 1.5 inch) can be irradiated by first irradiating the material

from one side, and then turning the material over and irradiating from the other side. Irradiation from multiple directions can be particularly useful with électron beam radiation, which irradiâtes faster than gamma radiation but typically does not achieve as great a pénétration depth.

RADIATION OPAQUE MATERIALS

The invention can include processing the material (e.g., for some of the o processing steps) in a vault and/or bunker that is constructed using radiation opaque materials. In some implémentations, the radiation opaque materials are selected to be capable of shielding the components from X-rays with high energy (short wavelength), which can penetrate many materials. One important factor in designing a radiation shielding enclosure is the atténuation length of the materials used, which will détermine the required thickness for a particular material, blend of materials, or layered structure. The atténuation length is the pénétration distance at which the radiation is reduced to approximately 1/e (e = Euler’s number) times that of the incident radiation. Although virtually ail materials are radiation opaque if thick enough, materials containing a high compositional percentage (e.g., density) of éléments that hâve a high Z value (atomic number) hâve a shorter radiation atténuation length and thus if such materials are used a thinner, lighter shielding can be provided. Examples of high Z value materials that are used in radiation shielding are tantalum and lead. Another important parameter in radiation shielding is the halving distance, which is the thickness of a particular material that will reduce gamma ray intensity by 50%. As an example for X-ray radiation with an energy of 0.1 MeV the halving thickness is about 15.1 mm for concrète and about 2.7 mm for lead, while with an X-ray energy of 1 MeV the halving thickness for concrète is about 44.45 mm and for lead is about 7.9 mm. Radiation opaque materials can be materials that are thick or thin so long as they can reduce the radiation that passes through to the other side. Thus, if it is desired that a particular enclosure hâve a low wall thickness, e.g., for light weight or due to size constraints, the material chosen should hâve a sufficient Z value and/or atténuation length so that its halving length is less than or equal to the desired wall thickness of the enclosure.

In some cases, the radiation opaque material may be a layered material, for example having a layer of a higher Z value material, to provide good shielding, and a

layer of a lower Z value material to provide other properties (e.g., structural integrity, impact résistance, etc.). In some cases, the layered material may be a graded-Z laminate, e.g., including a laminate in which the layers provide a gradient from high-Z through successively lower-Z éléments. In some cases the radiation opaque materials can be interlocking blocks, for example, lead and/or concrète blocks can be supplied by NELCO Worldwide (Burlington, MA), and reconfigurable vaults can be utilized.

A radiation opaque material can reduce the radiation passing through a structure (e.g., a wall, door, ceiling, enclosure, a sériés of these or combinations of these) formed of the material by about at least about 10 %, (e.g., at least about 20%, at least about 30%, at least about 40%, at least about 50%, at least about 60%, at least about 70%, at least about 80%, at least about 90%, at least about 95%, at least about 96%, at least about 97%, at least about 98%, at least about 99%, at least about 99.9%, at least about 99.99%, at least about 99.999%) as compared to the incident radiation. Therefore, an enclosure made of a radiation opaque material can reduce the exposure of equipment/system/components by the same amount. Radiation opaque materials can include stainless steel, metals with Z values above 25 (e.g., lead, iron), concrète, dirt, sand and combinations thereof. Radiation opaque materials can include a barrier in the direction of the incident radiation of at least about 1mm (e.g., 5 mm, 10mm, 5 cm, 10 cm, 100cm, lm, 10m).

RADIATION SOURCES

The type of radiation détermines the kinds of radiation sources used as well as the radiation devices and associated equipment. The methods, Systems and equipment described herein, for example for treating materials with radiation, can utilized sources as described herein as well as any other useful source.

Sources of gamma rays include radioactive nuclei, such as isotopes of cobalt, calcium, technetium, chromium, gallium, indium, iodine, iron, krypton, samarium, sélénium, sodium, thallium, and xénon.

Sources of X-rays include électron beam collision with métal targets, such as tungsten or molybdenum or alloys, or compact light sources, such as those produced commercially by Lyncean.

Alpha particles are identical to the nucléus of a hélium atom and are produced by the alpha decay of various radioactive nuclei, such as isotopes of bismuth, polonium, astatine, radon, francium, radium, several actinides, such as actinium, thorium, uranium, neptunium, curium, californium, américium, and plutonium.

Sources for ultraviolet radiation include deuterium or cadmium lamps.

Sources for infrared radiation include sapphire, zinc, or selenide window ceramic lamps.

Sources for microwaves include klystrons, Slevin type RF sources, or atom beam sources that employ hydrogen, oxygen, or nitrogen gases.

Accelerators used to accelerate the particles (e.g., électrons or ions) can be DC (e.g., electrostatic DC or electrodynamic DC), RF linear, magnetic induction linear or continuous wave. For example, various irradiating devices may be used in the methods disclosed herein, including field ionization sources, electrostatic ion separators, field ionization generators, thermionic émission sources, microwave discharge ion sources, recirculating or static accelerators, dynamic linear accelerators, van de Graaff accelerators, Cockroft Walton accelerators (e.g., PELLETRON® accelerators), LINACS, Dynamitrons (e.g., DYNAMITRON® accelerators), cyclotrons, synchrotrons, betatrons, transformer-type accelerators, microtrons, plasma generators, cascade accelerators, and folded tandem accelerators. For example, cyclotron type accelerators are available from EBA, Belgium, such as the RHODOTRON™ system, while DC type accelerators are available from RDI, now IBA Industrial, such as the DYNAMITRON®. Other suitable accelerator Systems include, for example: DC insulated core transformer (ICT) type Systems, available from Nissin High Voltage, Japan; S-band LINACs, available from L3PSD (USA), Linac Systems (France), Mevex (Canada), and Mitsubishi Heavy Industries (Japan); L-band LINACs, available from Iotron Industries (Canada); and ILU-based accelerators, available from Budker Laboratoires (Russia). Ions and ion accelerators are discussed in Introductory Nuclear Physics, Kenneth S. Krane, John Wiley & Sons, Inc. (1988), Krsto Prelec, FIZIKA B 6 (1997) 4, 177-206, Chu, William T., “Overview of Light-Ion Beam Therapy”, Columbus-Ohio, ICRU-IAEA Meeting, 18-20 March 2006, Iwata, Y. et al., “Altemating-Phase-Focused IH-DTL for Heavy-Ion Medical Accelerators”, Proceedings of EPAC 2006, Edinburgh, Scotland, and Leitner, C.M. et al., “Status of the Superconducting ECR Ion Source Venus”, Proceedings of EPAC 2000, Vienna, Austria. Some particle accelerators and their uses are disclosed, for example, in U.S. Pat. No. 7,931,784 to Medoff, the complété disclosure of which is incorporated herein by reference.

Electrons may be produced by radioactive nuclei that undergo beta decay, such as isotopes of iodine, césium, technetium, and iridium. Alternatively, an électron gun can be used as an électron source via thermionic émission and accelerated through an accelerating potential. An électron gun generates électrons, which are then accelerated through a large potential (e.g., greater than about 500 thousand, greater than about lmillion, greater than about 2 million, greater than about 5 million, greater than about 6 million, greater than about 7 million, greater than about 8 million, greater than about 9 million, or even greater than 10 million volts) and then scanned magnetically in the x-y plane, where the électrons are initially accelerated in the z direction down the accelerator 10 tube and extracted through a foil window. Scanning the électron beams is useful for increasing the irradiation surface when irradiating materials, e.g., a biomass, that is conveyed through the scanned beam. Scanning the électron beam also distributes the thermal load homogenously on the window and helps reduce the foil window rupture due to local heating by the électron beam. Window foil rupture is a cause of significant down-time due to subséquent necessary repairs and re-starting the électron gun.

Various other irradiating devices may be used in the methods disclosed herein, including field ionization sources, electrostatic ion separators, field ionization generators, thermionic émission sources, microwave discharge ion sources, recirculating or static accelerators, dynamic linear accelerators, van de Graaff accelerators, and folded tandem 20 accelerators. Such devices are disclosed, for example, in U.S. Pat. No. 7,931,784 to Medoff, the complété disclosure of which is incorporated herein by reference.

A beam of électrons can be used as the radiation source. A beam of électrons has the advantages of high dose rates (e.g., 1, 5, or even 10 Mrad per second), high throughput, less containment, and less confinement equipment. Electron beams can also 25 hâve high electrical efficiency (e.g., 80%), allowing for lower energy usage relative to other radiation methods, which can translate into a lower cost of operation and lower greenhouse gas émissions corresponding to the smaller amount of energy used. Electron beams can be generated, e.g., by electrostatic generators, cascade generators, transformer generators, low energy accelerators with a scanning System, low energy accelerators with 30 a linear cathode, linear accelerators, and pulsed accelerators.

Electrons can also be more efficient at causing changes in the molecular structure of carbohydrate-containing materials, for example, by the mechanism of chain scission. In addition, électrons having energies of 0.5-10 MeV can penetrate low density materials, such as the biomass materials described herein, e.g., materials having a bulk

density of less than 0.5 g/cm³, and a depth of 0.3-10 cm. Electrons as an ionizing radiation source can be useful, e.g., for relatively thin piles, layers or beds of materials, e.g., less than about 0.5 inch, e.g., less than about 0.4 inch, 0.3 inch, 0.25 inch, or less than about 0.1 inch. In some embodiments, the energy of each électron of the électron beam is from about 0.3 MeV to about 2.0 MeV (million électron volts), e.g., from about 0.5 MeV to about 1.5 MeV, or from about 0.7 MeV to about 1.25 MeV. Methods of irradiating materials are discussed in U.S. Pat. App. Pub. 2012/0100577 Al, filed October 18, 2011, the entire disclosure of which is herein incorporated by reference.

Electron beam irradiation devices may be procured commercially or builL For example, éléments or components such inductors, capacitors, casings, power sources, cables, wiring, voltage control Systems, current control éléments, insulating material, microcontrollers and cooling equipment can be purchased and assembled into a device. Optionally, a commercial device can be modified and/or adapted. For example, devices and components can be purchased from any of the commercial sources described herein including Ion Beam Applications (Louvain-la-Neuve, Belgium), Wasik Associâtes Inc. (Dracut, MA), NHV Corporation (Japan), the Titan Corporation (San Diego, CA), Vivirad High Voltage Corp (Billerica, MA) and/or Budker Laboratoires (Russia). Typical électron energies can be 0.5 MeV, 1 MeV, 2 MeV, 4.5 MeV, 7.5 MeV, or 10 MeV. Typical électron beam irradiation device power can be 1 kW, 5 kW, 10 kW, 20 kW, 50 kW, 60 kW, 70 kW, 80 kW, 90 kW, 100 kW, 125 kW, 150 kW, 175 kW, 200 kW, 250 kW, 300 kW, 350 kW, 400 kW, 450 kW, 500 kW, 600 kW, 700 kW, 800 kW, 900 kW or even 1000 kW. Accelerators that can be used include NHV irradiators medium energy sériés EPS-500 (e.g., 500 kV accelerator voltage and 65, 100 or 150 mA beam current), EPS-800 (e.g., 800 kV accelerator voltage and 65 or 100 mA beam current), or EPS-1000 (e.g., 1000 kV accelerator voltage and 65 or 100 mA beam current). Also, accelerators from NHV’s high energy sériés can be used such as EPS1500 (e.g., 1500 kV accelerator voltage and 65 mA beam current), EPS-2000 (e.g., 2000 kV accelerator voltage and 50 mA beam current), EPS-3000 (e.g., 3000 kV accelerator voltage and 50 mA beam current) and EPS-5000 (e.g., 5000 and 30 mA beam current).

Tradeoffs in considering électron beam irradiation device power spécifications include cost to operate, capital costs, dépréciation, and device footprint. Tradeoffs in considering exposure dose levels of électron beam irradiation would be energy costs and environment, safety, and health (ESH) concems. Typically, generators are housed in a vault, e.g., of lead or concrète, especially for production from X-rays that are generated in the process. Tradeoffs in considering électron energies include energy costs.

The électron beam irradiation device can produce either a fixed beam or a scanning beam. A scanning beam may be advantageous with large scan sweep length and high scan speeds, as this would effectively replace a large, fixed beam width. Further, available sweep widths of 0.5 m, 1 m, 2 m or more are available. The scanning beam is preferred in most embodiments described herein because of the larger scan width and reduced possibility of local heating and failure of the Windows.

ELECTRON GUNS - WINDOWS

The extraction System for an électron accelerator can include two window foils. The cooling gas in the two foil window extraction system can be a purge gas or a mixture, for example air, or a pure gas. In one embodiment the gas is an inert gas such as nitrogen, argon, hélium and or carbon dioxide. It is prefeiTed to use a gas rather than a liquid since energy losses to the électron beam are minimized. Mixtures of pure gas can also be used, either pre-mixed or mixed in line prior to impinging on the Windows or in the space between the Windows. The cooling gas can be cooled, for example, by using a heat exchange system (e.g., a chiller) and/or by using boil off from a condensed gas (e.g., liquid nitrogen, liquid hélium). Window foils are described in PCT/US2013/64332 filed October 10, 2013 the full disclosure of which is incorporated by reference herein.

HEATING AND THROUGHPUT DURING RADIATION TREATMENT

Several processes can occur in biomass when électrons from an électron beam interact with matter in inelastic collisions. For example, ionization of the material, chain scission of polymers in the material, cross linking of polymers in the material, oxidation of the material, génération of X-rays (“Bremsstrahlung”) and vibrational excitation of molécules (e.g., phonon génération). Without being bound to a particular mechanism, the réduction in recalcitrance can be due to several of these inelastic collision effects, for example ionization, chain scission of polymers, oxidation and phonon génération. Some of the effects (e.g., especially X-ray génération), necessitate shielding and engineering barriers, for example, enclosing the irradiation processes in a concrète (or other radiation opaque material) vault. Another effect of irradiation, vibrational excitation, is équivalent

to heating up the sample. Heating the sample by irradiation can help in recalcitrance réduction, but excessive heating can destroy the material, as will be explained below.

The adiabatic température lise (ΔΤ) from adsorption of ionizing radiation is given by the équation: ΔΤ = D/Cp: where D is the average dose in kGy, Cp is the heat capacity 5 in J/g °C, and ΔΤ is the change in température in °C. A typical dry biomass material will hâve a heat capacity close to 2. Wet biomass will hâve a higher heat capacity dépendent on the amount of water since the heat capacity of water is very high (4.19 J/g °C). Metals hâve much lower heat capacities, for example 304 stainless steel has a heat capacity of 0.5 J/g °C. The température change due to the instant adsorption of radiation in a biomass and stainless steel for various doses of radiation is shown in Table 1. In practice, the higher températures cause décomposition of the biomass leading to extreme déviation from theory.

Table 1 : Calculated Température increase for biomass and stainless steel.

Dose (Mrad)	Estimated Biomass ΔΤ (°C)	Steel ΔΤ (°C)
10	50	200
50	250 (decomposed)	1000
100	500 (decomposed)	2000
150	750 (decomposed)	3000
200	1000 (decomposed)	4000

High températures can destroy and or modify the biopolymers in biomass so that the polymers (e.g., cellulose) are unsuitable for further processing. A biomass subjected to high températures can become dark, sticky and give off odors indicating décomposition. The stickiness can even make the material hard to convey. The odors can 20 be unpleasant and be a safety issue. In fact, keeping the biomass below about 200°C has been found to be bénéficiai in the processes described herein (e.g., below about 190°C, below about 180°C, below about 170°C, below about 160°C, below about 150°C, below about 140°C, below about 130°C, below about 120°C, below about 110°C, between about 60°C and 180°C, between about 60°C and 160°C, between about 60°C and 150°C, 25 between about 60°C and 140°C, between about 60°C and 130°C, between about 60°C and 120°C, between about 80°C and 180°C, between about 100°C and 180°C, between about 120°C and 180°C, between about 140°C and 180°C, between about 160°C and 180°C, between about 100°C and 140°C, between about 80°C and 120°C).

It has been found that irradiation above about 10 Mrad is désirable for the processes described herein (e.g., réduction of recalcitrance). A high throughput is also désirable so that the irradiation does not become a bottle neck in processing the biomass. The treatment is govemed by a Dose rate équation: M = FP/D'time, where M is the mass of irradiated material (Kg), F is the fraction of power that is adsorbed (unit less), P is the emitted power (kW=Voltage in MeV x Current in mA), time is the treatment time (sec) and D is the adsorbed dose (kGy). In an exemplary process where the fraction of adsorbed power is fixed, the Power emitted is constant and a set dosage is desired, the throughput (e.g., M, the biomass processed) can be increased by increasing the irradiation time. However, increasing the irradiation time without allowing the material to cool, can excessively heat the material as exemplified by the calculations shown above. Since biomass has a low thermal conductivity (less than about 0.1 Wm-1K-1), heat dissipation is slow, unlike, for example metals (greater than about 10 Wm-1K-1) which can dissipate energy quickly as long as there is a heat sink to transfer the energy to.

ELECTRON GUNS - BEAM STOPS

In some embodiments the Systems and methods include a beam stop (e.g., a shutter). For example, the beam stop can be used to quickly stop or reduce the irradiation of material without powering down the électron beam device. Alternatively the beam stop can be used while powering up the électron beam, e.g., the beam stop can stop the électron beam until a beam current of a desired level is achieved. The beam stop can be placed between the primary foil window and a secondary foil window. For example the beam stop can be mounted so that it is movable, that is, so that it can be moved into and out of the beam path. Even partial coverage of the beam can be used, for example, to control the dose of irradiation. The beam stop can be mounted to the floor, to a conveyor for the biomass, to a wall, to the radiation device (e.g., at the scan hom), or to any structural support. Preferably the beam stop is fixed in relation to the scan hom so that the beam can be effectively controlled by the beam stop. The beam stop can incorporate a hinge, a rail, wheels, slots, or other means allowing for its operation in moving into and out of the beam. The beam stop can be made of any material that will stop at least 5% of the électrons, e.g., at least 10%, 20%, 30%, 40%, 50%, 60%, 70%, at

least 80%, 85%, 90%, 91%, 92%, 93%, 94%, 95%, 96%, 97%, 98%, 99% or even about 100% of the électrons.

The beam stop can be made of a métal including, but not limited to, stainless steel, lead, iron, molybdenum, silver, gold, titanium, aluminum, tin, or alloys of these, or 5 laminates (layered materials) made with such metals (e.g., metal-coated ceramic, metalcoated polymer, metal-coated composite, multilayered métal materials).

The beam stop can be cooled, for example, with a cooling fluid such as an aqueous solution or a gas. The beam stop can be partially or completely hollow, for example, with cavities. Interior spaces of the beam stop can be used for cooling fluids 10 and gases. The beam stop can be of any shape, including fiat, curved, round, oval, square, rectangular, beveled and wedged shapes.

The beam stop can hâve perforations so as to allow some électrons through, thus controlling (e.g., reducing) the levels of radiation across the whole area of the window, or in spécifie régions of the window. The beam stop can be a mesh formed, for example, 15 from fibers or wires. Multiple beam stops can be used, together or independently, to control the irradiation. The beam stop can be remotely controlled, e.g., by radio signal or hard wired to a motor for moving the beam into or out of position.

BEAM DUMPS

The embodiments dîsclosed herein can also include a beam dump when utilizing a radiation treatment A beam dump’s purpose is to safely absorb a beam of charged particles. Like a beam stop, a beam dump can be used to block the beam of charged particles. However, a beam dump is much more robust than a beam stop, and is intended 25 to block the full power of the électron beam for an extended period of time. They are often used to block the beam as the accelerator is powering up.

Beam dumps are also designed to accommodate the heat generated by such beams, and are usually made from materials such as copper, aluminum, carbon, béryllium, tungsten, or mercury. Beam dumps can be cooled, for example, using a 30 cooling fluid that can be in thermal contact with the beam dump.

BIOMASS MATERIALS

Lignocellulosic materials, such as can be used in the methods and equipment described herein include, but are not limited to, wood, particle board, forestry wastes (e.g., sawdust, aspen wood, wood chips), grasses, (e.g., switchgrass, miscanthus, cord grass, reed canary grass), grain residues, (e.g., rice hulls, oat hulls, wheat chaff, barley hulls), agricultural waste (e.g., silage, canola straw, wheat straw, barley straw, oat straw, rice straw, jute, hemp, flax, bamboo, sisal, abaca, com cobs, com stover, soybean stover, com fiber, alfalfa, hay, coconut hair), sugar processing residues (e.g., bagasse, beet pulp, agave bagasse), algae, seaweed, manure, sewage, and mixtures of any of these.

In some cases, the lignocellulosic material includes comcobs. Giound or hammermilled comcobs can be spread in a layer of relatively uniform thickness for irradiation, and after irradiation are easy to disperse in the medium for further processing. To facilitate harvest and collection, in some cases the entire com plant is used, including the com stalk, com kernels, and in some cases even the root System of the plant.

Advantageously, no additional nutrients (other than a nitrogen source, e.g., urea or ammonia) are required during fermentation of comcobs or cellulosic or lignocellulosic materials containing significant amounts of comcobs.

Comcobs, before and after comminution, are also easier to convey and disperse, and hâve a lesser tendency to form explosive mixtures in air than other cellulosic or lignocellulosic materials such as hay and grasses.

Cellulosic materials include, for example, paper, paper products, paper waste, paper pulp, pigmented papers, loaded papers, coated papers, filled papers, magazines, printed matter (e.g., books, catalogs, manuals, labels, calendars, greeting cards, brochures, prospectuses, newsprint), printer paper, polycoated paper, card stock, cardboard, paperboard, materials having a high α-cellulose content such as cotton, and mixtures of any of these. For example, paper products as described in U.S. App. No. 13/396,365 (“Magazine Feedstocks” by Medoff et al., filed Februaiy 14, 2012), the full disclosure of which is incorporated herein by reference.

Cellulosic materials can also include lignocellulosic materials which hâve been partially or fully de-lignified.

In some instances other biomass materials can be utilized, for example starchy materials. Starchy materials include starch itself, e.g., corn starch, wheat starch, potato starch or rice starch, a dérivative of starch, or a material that includes starch, such as an edible food product or a crop. For example, the starchy material can be arracacha, buckwheat, banana, barley, cassava, kudzu, ocra, sago, sorghum, regular household potatoes, sweet potato, taro, yams, or one or more beans, such as favas, lentils or peas. Blends of any two or more starchy materials are also starchy materials. Mixtures of starchy, cellulosic and or lignocellulosic materials can also be used. For example, a biomass can be an entire plant, a part of a plant or different parts of a plant, e.g., a wheat plant, cotton plant, a corn plant, rice plant or a tree. The starchy materials can be treated by any of the methods described herein.

Microbial materials that can be used as feedstock can include, but are not limited to, any naturally occurring or genetically modified microorganism or organism that contains or is capable of providing a source of carbohydrates (e.g., cellulose), for example, protists, e.g., animal protists (e.g., protozoa such as flagellâtes, amoeboids, ciliates, and sporozoa) and plant protists (e.g., algae such alveolates, chlorarachniophytes, cryptomonads, euglenids, glaucophytes, haptophytes, red algae, stramenopiles, and viridaeplantae). Other examples include seaweed, plankton (e.g., macroplankton, mesoplankton, microplankton, nanoplankton, picoplankton, and femptoplankton), phytoplankton, bacteria (e.g., gram positive bacteria, gram négative bacteria, and extremophiles), yeast and/or mixtures of these. In some instances, microbial biomass can be obtained from natural sources, e.g., the océan, lakes, bodies of water, e.g., sait water or fresh water, or on land. Altematively or in addition, microbial biomass can be obtained from culture Systems, e.g., large scale dry and wet culture and fermentation Systems.

In other embodiments, the biomass materials, such as cellulosic, starchy and lignocellulosic feedstock materials, can be obtained from transgenic microorganisms and plants that hâve been modified with respect to a wild type variety. Such modifications may be, for example, through the itérative steps of sélection and breeding to obtain desired traits in a plant. Furthermore, the plants can hâve had genetic material removed, modified, silenced and/or added with respect to the wild type variety. For example, genetically modified plants can be produced by recombinant DNA methods, where genetic modifications include introducing or modifying spécifie genes from parental varieties, or, for example, by using transgenic breeding wherein a spécifie gene or genes

are introduced to a plant from a different species of plant and/or bacteria. Another way to create generic variation is through mutation breeding wherein new alleles are artificially created from endogenous genes. The artificial genes can be created by a variety of ways including treating the plant or seeds with, for example, chemical mutagens (e.g., using alkylating agents, epoxides, alkaloids, peroxides, formaldéhyde), irradiation (e.g., X-rays, gamma rays, neutrons, beta particles, alpha particles, protons, deuterons, UV radiation) and température shocking or other extemal stressing and subséquent sélection techniques. Other methods of providing modified genes is through error prone PCR and DNA shuffling followed by insertion of the desired modified DNA into the desired plant or seed. Methods of introducing the desired genetic variation in the seed or plant include, for example, the use of a bacterial carrier, biolistics, calcium phosphate précipitation, electroporation, gene splicing, gene silencing, lipofection, microinjection and viral carriers. Additional genetically modified materials hâve been described in U.S. Application Serial No 13/396,369 filed February 14, 2012 the full disclosure of which is incorporated herein by reference.

Any of the methods described herein can be practiced with mixtures of any biomass materials described herein.

OTHER MATERIALS

Other materials (e.g., natural or synthetic materials), for example polymers, can be treated and/or made utilizing so of the methods, equipment and Systems described hererin. For example, energy produced by the methods described herein can be used to process materials. For example polyethylene (e.g., linear low density ethylene and high 25 density polyethylene), polystyrènes, sulfonated polystyenes, poly (vinyl chloride), polyesters (e.g., nylons, DACRON™, KODEL™), polyalkylene esters, poly vinyl esters, polyamides (e.g., KEVLAR™), polyethylene terephthalate, cellulose acetate, acetal, poly acrylonitrile, polycarbonates (e.g., LEXAN™), acrylics [e.g., poly (methyl méthacrylate), poly(methyl méthacrylate), polyacrylonitriles, Poly urethanes, polypropylene, poly butadiene, polyisobutylene, polyacrylonitrile, polychloroprene (e.g. neoprene), poly(cis-l,4-isoprene) [e.g., natural rubber], poly(trans-l,4-isoprene) [e.g., gutta percha], phénol formaldéhyde, melamine formaldéhyde, epoxides, polyesters, poly amines, polycarboxylic acids, polylactic acids, polyvinyl alcohols, polyanhydrides, poly fluoro carbons (e.g., TEFLON™), silicons (e.g., silicone rubber), polysilanes, poly ethers

(e.g., polyethylene oxide, polypropylene oxide), waxes, oils and mixtures of these . Also included are plastics, rubbers, elastomers, fibers, waxes, gels, oils, adhesives, thermoplastics, thermosets, biodégradable polymers, resins made with these polymers, other polymers, other materials and combinations thereof. The polymers can be made by any useful method including cationic polymerization, anionic polymerization, radical polymerization, metathesis polymerization, ring opening polymerization, graft polymerization, addition polymerization. In some cases the treatments disclosed herein can be used, for example, for radically initiated graft polymerization and cross linking. Composites of polymers, for example with glass, metals, biomass (e.g., fibers, particles), ceramics can also be treated and/or made.

Other materials that can be treated by using the methods, Systems and equipment disclosed herein are ceramic materials, minerais, metals, inorganic compounds. For example, silicon and germanium crystals, silicon nitrides, métal oxides, semiconductors, insulators, cements and or conductors.

In addition, manufactured multipart or shaped materials (e.g., molded, extruded, welded, riveted, layered or combined in any way) can be treated, for example cables, pipes, boards, enclosures, integrated semiconductor chips, circuit boards, wires, tires, Windows, laminated materials, gears, belts, machines, combinations of these. For example, treating a material by the methods described herein can modify the surfaces, for example, making them susceptible to further functionalization, combinations (e.g., welding) and/or treatment can cross link the materials.

BIOMASS MATERIAL PREPARATION - MECHANICAL TREATMENTS

The biomass can be in a dry form (e.g., as described previously), for example with less than about 35% moisture content (e.g., less than about 20 %, less than about 15 %, less than about 10 % less than about 5 %, less than about 4%, less than about 3 %, less than about 2 % or even less than about 1 %). The biomass can also be delivered in a wet state, for example as a wet solid, a slurry or a suspension with at least about 10 wt% solids (e.g., at least about 20 wt.%, at least about 30 wt. %, at least about 40 wt.%, at least about 50 wt.%, at least about 60 wt.%, at least about 70 wt.%).

The processes disclosed herein can utilize low bulk density materials, for example cellulosic or lignocellulosic feedstocks that hâve been physically pretreated to hâve a bulk density of less than about 0.75 g/cm3, e.g., less than about 0.7, 0.65, 0.60,

0.50,0.35, 0.25,0.20, 0.15,0.10, 0.05 or less, e.g., less than about 0.025 g/cm³. Bulk density is determined using ASTM D1895B. Briefly, the method involves filling a measuring cylinder of known volume with a sample and obtaining a weight of the sample. The bulk density is calculated by dividing the weight of the sample in grams by the known volume of the cylinder in cubic centimeters. If desired, low bulk density materials can be densified, for example, by methods described in U.S. Pat. No. 7,971,809 published July 5, 2011, the entire disclosure of which is hereby incorporated by reference.

In some cases, the pre-treatment processing includes screening of the biomass material. Screening can be through a mesh or perforated plate with a desired opening size, for example, less than about 6.35 mm (1/4 inch, 0.25 inch), (e.g., less than about 3.18 mm (1/8 inch, 0.125 inch), less than about 1.59 mm (1/16 inch, 0.0625 inch), is less than about 0.79 mm (1/32 inch, 0.03125 inch), e.g., less than about 0.51 mm (1/50 inch, 0.02000 inch), less than about 0.40 mm (1/64 inch, 0.015625 inch), less than about 0.23 mm (0.009 inch), less than about 0.20 mm (1/128 inch, 0.0078125 inch), less than about 0.18 mm (0.007 inch), less than about 0.13 mm (0.005 inch), or even less than about 0.10 mm (1/256 inch, 0.00390625 inch)). In one configuration the desired biomass falls through the perforations or screen and thus biomass larger than the perforations or screen are not irradiated. These larger materials can be re-processed, for example, by comminuting, or they can simply be removed from processing. In another configuration material that is larger than the perforations is irradiated and the smaller material is removed by the screening process or recycled. In this kind of a configuration, the conveyor, such as a vibratory conveyor, itself (for example, a part of the conveyor) can be perforated or made with a mesh. For example, in one particular embodiment the biomass material may be wet and the perforations or mesh allow water to drain away from the biomass before irradiation.

Screening of material can also be by a manual method, for example by an operator or mechanoid (e.g., a robot equipped with a color, reflectivity or other sensor) that removes unwanted material. Screening can also be by magnetic screening wherein a magnet is disposed near the conveyed material and the magnetic material is removed magnetically.

Optional pre-treatment processing can include heating the material (e.g., in addition to for drying or for the purpose of drying the material). For example, a portion of a conveyor conveying the biomass or other material can be sent through a heated zone. The heated zone can be created, for example, by IR radiation, microwaves, combustion (e.g., gas, coal, oil, biomass), résistive heating and/or inductive coils. The heat can be applied from at least one side or more than one side, can be continuous or periodic and can be for only a portion of the material or ail the material. For example, a portion of the conveying trough can be heated by use of a heating jacket. Heating can be, for example, for the purpose of drying the material. In the case of drying the material, this can also be facilitated, with or without heating, by the movement of a gas (e.g., air, oxygen, nitrogen, He, CO2, Argon) over and/or through the biomass as it is being conveyed.

Optionally, pre-treatment processing can include cooling the material. Cooling material is described in U.S. Pat. No. 7,900,857 published March 8, 2011, the disclosure of which in incorporated herein by reference. For example, cooling can be by supplying a cooling fluid, for example, water (e.g., with glycerol), or nitrogen (e.g., liquid nitrogen) to the bottom of the conveying trough. Altematively, a cooling gas, for example, chilled nitrogen can be blown over the biomass materials or under the conveying system.

Another optional pre-treatment processing method can include adding a material to the biomass or other feedstocks. The additional material can be added by, for example, by showering, sprinkling and or pouring the material onto the biomass as it is conveyed. Materials that can be added include, for example, metals, ceramics and/or ions as described in U.S. Pat. App. Pub. 2010/0105119 Al (filed October 26, 2009) and U.S. Pat. App. Pub. 2010/0159569 Al (filed December 16, 2009), the entire disclosures of which are incorporated herein by reference. Optional materials that can be added include acids and bases. Other materials that can be added are oxidants (e.g., peroxides, chlorates), polymers, polymerizable monomers (e.g., containing unsaturated bonds), water, catalysts, enzymes and/or organisms. Materials can be added, for example, in pure form, as a solution in a solvent (e.g., water or an organic solvent) and/or as a solution. In some cases the solvent is volatile and can be made to evaporate e.g., by heating and/or blowing gas as previously described. The added material may form a uniform coating on the biomass or be a homogeneous mixture of different components (e.g., biomass and additional material). The added material can modulate the subséquent irradiation step by increasing the efficiency of the irradiation, damping the irradiation or changing the effect of the irradiation (e.g., from électron beams to X-rays or heat). The method may hâve no impact on the irradiation but may be useful for further downstream

processing. The added material may help in conveying the material, for example, by lowering dust levels.

Biomass can be delivered to conveyor (e.g., vibratory conveyors that can be used in the vaults herein described) by a belt conveyor, a pneumatic conveyor, a screw conveyor, a hopper, a pipe, manually or by a combination of these. The biomass can, for example, be dropped, poured and/or placed onto the conveyor by any of these methods. In some embodiments the material is delivered to the conveyor using an enclosed material distribution system to help maintain a low oxygen atmosphère and/or control dust and fines. Lofted or air suspended biomass fines and dust are undesirable because these can form an explosion hazard or damage the window foils of an électron gun (if such a device is used for treating the material).

The material can be leveled to form a uniform thickness between about 0.0312 and 5 inches (e.g., between about 0.0625 and 2.000 inches, between about 0.125 and 1 inches, between about 0.125 and 0.5 inches, between about 0.3 and 0.9 inches, between about 0.2 and 0.5 inches between about 0.25 and 1.0 inches, between about 0.25 and 0.5 inches, 0.100 +/- 0.025 inches, 0.150 +/- 0.025 inches, 0.200 +/- 0.025 inches, 0.250 +/0.025 inches, 0.300 +/- 0.025 inches, 0.350 +/- 0.025 inches, 0.400 +/- 0.025 inches, 0.450 +/- 0.025 inches, 0.500 +/- 0.025 inches, 0.550 +/- 0.025 inches, 0.600 +/- 0.025 inches, 0.700 +/- 0.025 inches, 0.750 +/- 0.025 inches, 0.800 +/- 0.025 inches, 0.850 +/20 0.025 inches, 0.900 +/- 0.025 inches, 0.900 +/- 0.025 inches.

Generally, it is preferred to convey the material as quickly as possible through the électron beam to maximize throughput. For example the material can be conveyed at rates of at least 1 ft/min, e.g., at least 2 ft/min, at least 3 ft/min, at least 4 ft/min, at least 5 ft/min, at least 10 ft/min, at least 15 ft/min, 20, 25, 30, 35,40, 45, 50 ft/min. The rate of conveying is related to the beam current, for example, for a % inch thick biomass and

100 mA, the conveyor can move at about 20 ft/min to provide a useful irradiation dosage, at 50 mA the conveyor can move at about 10 ft/min to provide approximately the same irradiation dosage.

After the biomass material has been conveyed through the radiation zone, optional post-treatment processing can be done. The optional post-treatment processing can, for example, be a process described with respect to the pre-irradiation processing. For example, the biomass can be screened, heated, cooled, and/or combined with additives. Uniquely to post-irradiation, quenching of the radicals can occur, for example, quenching of radicals by the addition of fluids or gases (e.g., oxygen, nitrous oxide,

ammonia, liquids), using pressure, neat, and/or the addition of radical scavengers. For example, the biomass can be conveyed out of the enclosed conveyor and exposed to a gas (e.g., oxygen) where it is quenched, forming carboxylated groups. In one embodiment the biomass is exposed during irradiation to the reactive gas or fluid. Quenching of biomass that has been irradiated is described in U.S. Pat No. 8,083,906 published Dec 27, 2011, the entire disclosure of which is incorporate herein by reference.

If desired, one or more mechanical treatments can be used in addition to irradiation to further reduce the recalcitrance of the carbohydrate-containing material. These processes can be applied before, during and or after irradiation.

In some cases, the mechanical treatment may include an initial préparation of the feedstock as received, e.g., size réduction of materials, such as by comminution, e.g., cutting, grinding, shearing, pulverizing or chopping. For example, in some cases, loose feedstock (e.g., recycled paper, starchy materials, or switchgrass) is prepared by shearing or shredding. Mechanical treatment may reduce the bulk density of the carbohydratecontaining material, increase the surface area of the carbohydrate-containing material and/or decrease one or more dimensions of the carbohydrate-containing material.

Altematively, or in addition, the feedstock material can be treated with another treatment, for example chemical treatments, such as with an acid (HCl, H2SO4, H3PO4), a base (e.g., KOH and NaOH), a chemical oxidant (e.g., peroxides, chlorates, ozone), irradiation, steam explosion, pyrolysis, sonication, oxidation, chemical treatment. The treatments can be in any order and in any sequence and combinations. For example, the feedstock material can first be physically treated by one or more treatment methods, e.g., chemical treatment including and in combination with acid hydrolysis (e.g., utilizing HCl, H2SO4, H3PO4), radiation, sonication, oxidation, pyrolysis or steam explosion, and then mechanically treated. This sequence can be advantageous since materials treated by one or more of the other treatments, e.g., irradiation or pyrolysis, tend to be more brittle and, therefore, it may be easier to further change the structure of the material by mechanical treatment. As another example, a feedstock material can be conveyed through ionizing radiation using a conveyor as described herein and then mechanically treated. Chemical treatment can remove some or ail of the lignin (for example chemical pulping) and can partially or completely hydrolyze the material. The methods also can be used with pre-hydrolyzed material. The methods also can be used with material that has not been pre hydrolyzed The methods can be used with mixtures of hydrolyzed and non-hydrolyzed materials, for example with about 50% or more non-hydrolyzed matenal, with about 60% or more non- hydrolyzed material, with about 70% or more non-hydrolyzed material, with about 80% or more non-hydrolyzed material or even with 90% or more non-hydrolyzed material.

In addition to size réduction, which can be performed initially and/or later in processing, mechanical treatment can also be advantageous for “opening up,” “stressing,” breaking or shattering the carbohydrate-containing materials, making the cellulose of the materials more susceptible to chain scission and/or disruption of crystalline structure during the physical treatment.

Methods of mechanically treating the carbohydrate-containing material include, for example, milling or grinding. Milling may be performed using, for example, a hammer mill, bail mill, colloid mill, conical or cône mill, disk mill, edge mill, Wiley mill, grist mill or other mill. Grinding may be performed using, for example, a cutting/impact type grinder. Some exemplary grinders include stone grinders, pin grinders, coffee grinders, and burr grinders. Grinding or milling may be provided, for example, by a reciprocating pin or other element, as is the case in a pin mill. Other mechanical treatment methods include mechanical ripping or tearing, other methods that apply pressure to the fibers, and air attrition milling. Suitable mechanical treatments further include any other technique that continues the disruption of the internai structure of the material that was initiated by the previous processing steps.

Mechanical feed préparation Systems can be configured to produce streams with spécifie characteristics such as, for example, spécifie maximum sizes, spécifie length-towidth, or spécifie surface areas ratios. Physical préparation can increase the rate of reactions, improve the movement of material on a conveyor, improve the irradiation profile of the material, improve the radiation uniformity of the material, or reduce the processing time required by opening up the materials and making them more accessible to processes and/or reagents, such as reagents in a solution.

The bulk density of feedstocks can be controlled (e.g., increased). In some situations, it can be désirable to préparé a low bulk density material, e.g., by densifying the material (e.g., densification can make it easier and less costly to transport to another site) and then reverting the material to a lower bulk density state (e.g., after transport). The material can be densified, for example from less than about 0.2 g/cc to more than about 0.9 g/cc (e.g., less than about 0.3 to more than about 0.5 g/cc, less than about 0.3 to more than about 0.9 g/cc, less than about 0.5 to more than about 0.9 g/cc, less than about 0.3 to more than about 0.8 g/cc, less than about 0.2 to more than about 0.5 g/cc). For

example, the material can be densified by the methods and equipment disclosed in U.S. Pat. No. 7,932,065 to Medoff and International Publication No. WO 2008/073186 (which was filed October 26, 2007, was published in English, and which designated the United States), the full disclosures of which are incorporated herein by reference.

Densified materials can be processed by any of the methods described herein, or any material processed by any of the methods described herein can be subsequently densified.

In some embodiments, the material to be processed is in the form of a fibrous material that includes fibers provided by shearing a fiber source. For example, the o shearing can be performed with a rotaiy knife cutter.

For example, a fiber source, e.g., that is récalcitrant or that has had its recalcitrance level reduced, can be sheared, e.g., in a rotary knife cutter, to provide a first fibrous material. The first fibrous material is passed through a first screen, e.g., having an average opening size of 1.59 mm or less (1/16 inch, 0.0625 inch), provide a second fibrous material. If desired, the fiber source can be eut prior to the shearing, e.g., with a shredder. For example, when a paper is used as the fiber source, the paper can be first eut into strips that are, e.g., 1/4- to 1/2-inch wide, using a shredder, e.g., a counterrotating screw shredder, such as those manufactured by Munson (Utica, N.Y.). As an alternative to shredding, the paper can be reduced in size by cutting to a desired size using a guillotine cutter. For example, the guillotine cutter can be used to eut the paper into sheets that are, e.g., 10 inches wide by 12 inches long.

In some embodiments, the shearing of the fiber source and the passing of the resulting first fibrous material through a first screen are performed concurrently. The shearing and the passing can also be performed in a batch-type process.

For example, a rotary knife cutter can be used to concurrently shear the fiber source and screen the first fibrous material. A rotary knife cutter includes a hopper that can be loaded with a shredded fiber source prepared by shredding a fiber source.

In some implémentations, the feedstock is physically treated prior to saccharification and/or fermentation. Physical treatment processes can include one or more of any of those described herein, such as mechanical treatment, chemical treatment, irradiation, sonication, oxidation, pyrolysis or steam explosion. Treatment methods can be used in combinations of two, three, four, or even ail of these technologies (in any order). When more than one treatment method is used, the methods can be applied at the same time or at different times. Other processes that change a molecular structure of a

biomass feedstock may also be used, alone or in combination with the processes disclosed herein.

Mechanical treatments that may be used, and the characteristics of the mechanically treated carbohydrate-containing materials, are described in further detail in U.S. Pat. App. Pub. 2012/0100577 Al, filed October 18,2011, the full disclosure of which is hereby incorporated herein by reference.

SONICATION, PYROLYSIS, OXIDATION, STEAM EXPLOSION

If desired, one or more sonication, pyrolysis, oxidative, or steam explosion processes can be used instead of or in addition to irradiation to reduce or further reduce the recalcitrance of the carbohydrate-containing material. For example, these processes can be applied before, during and or after irradiation. These processes are described in detail in U.S. Pat. No. 7,932,065 to Medoff, the full disclosure of which is incorporated herein by reference.

INTERMEDIATES AND PRODUCTS

Using the processes described herein, the biomass material can be converted to one or more products, such as energy (e.g., in addition to co-generation as described herein), fuels, foods and materials. For example, intermediates and products such as organic acids, salts of organic acids, anhydrides, esters of organic acids and fuels, e.g., fuels for internai combustion engines or feedstocks for fuel cells can be produced. Systems and processes are described herein that can use as feedstock cellulosic and/or lignocellulosic materials that are readily available, but often can be difficult to process, e.g., municipal waste streams and waste paper streams, such as streams that include newspaper, Kraft paper, corrugated paper or mixtures of these.

Spécifie examples of products include, but are not limited to, hydrogen, sugars (e.g., glucose, xylose, arabinose, mannose, galactose, fructose, disaccharides, oligosaccharides and polysaccharides), alcohols (e.g., monohydric alcohols or dihydric alcohols, such as éthanol, n-propanol, isobutanol, sec-butanol, tert-butanol or n-butanol), hydrated or hydrous alcohols (e.g., containing greater than 10%, 20%, 30% or even greater than 40% water), biodiesel, organic acids, hydrocarbons (e.g., methane, ethane, propane, isobutene, pentane, n-hexane, biodiesel, bio-gasoline and mixtures thereof), co17466 products (e.g., proteins, such as cellulolytic proteins (enzymes) or single cell proteins), and mixtures of any of these in any combination or relative concentration, and optionally in combination with any additives (e.g., fuel additives). Other examples include carboxylic acids, salts of a carboxylic acid, a mixture of carboxylic acids and salts of carboxylic acids and esters of carboxylic acids (e.g., methyl, ethyl and n-propyl esters), ketones (e.g., acetone), aldéhydes (e.g., acetaldehyde), alpha and beta unsaturated acids (e.g., acrylic acid) and olefins (e.g., ethylene). Other alcohols and alcohol dérivatives include propanol, propylene glycol, 1,4-butanediol, 1,3-propanediol, sugar alcohols (e.g., erythritol, glycol, glycerol, sorbitol threitol, arabitol, ribitol, mannitol, dulcitol, fucitol, iditol, isomalt, maltitol, lactitol, xylitol and other polyols), and methyl or ethyl esters of any of these alcohols. Other products include methyl acrylate, methylmethacrylate, Dlactic acid, L-lactic acid, pyruvic acid, poly lactic acid, citric acid, formic acid, acetic acid, propionic acid, butyric acid, succinic acid, valeric acid, caproic acid, 3hydroxypropionic acid, palmitic acid, stearic acid, oxalic acid, malonic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, gamma-hydroxybutyric acid, and mixtures thereof, salts of any of these acids, mixtures of any of the acids and their respective salts.

Any combination of the above products with each other, and/or of the above products with other products, which other products may be made by the processes described herein or otherwise, may be packaged together and sold as products. The products may be combined, e.g., mixed, blended or co-dissolved, or may simply be packaged or sold together.

Any of the products or combinations of products described herein may be sanitized or sterilized prior to selling the products, e.g., after purification or isolation or even after packaging, to neutralize one or more potentially undesirable contaminants that could be présent in the product(s). Such sanitation can be done with électron bombardment, for example, by at a dosage of less than about 20 Mrad, e.g., from about 0.1 to 15 Mrad, from about 0.5 to 7 Mrad, or from about 1 to 3 Mrad.

The processes described herein can produce various by-product streams useful for generating steam and electricity to be used in other parts of the plant (co-generation) or sold on the open market (e.g., as previously described herein). For example, steam generated from buming by-product streams can be used in a distillation process. As another example, electricity generated from buming by-product streams can be used to power électron beam generators used in pretreatment.

The by-products used to generate steam and electricity are derived from a number of sources throughout the process. For example, anaérobie digestion of wastewater can produce a biogas high in methane and a small amount of waste biomass (sludge). As another example, post-saccharification and/or post-distillate solids (e.g., unconverted lignin, cellulose, and hemicellulose remaining from the pretreatment and primary processes) can be used, e.g., bumed, as a fuel.

Other intermediates and products, including food and pharmaceutical products, are described in U.S. Pat. App. Pub. 2010/0124583 Al, published May 20,2010, to Medoff, the full disclosure of which is hereby incoiporated by reference herein.

LIGNIN DERIVED PRODUCTS

The spent biomass (e.g., spent lignocellulosic material) from lignocellulosic processing by the methods described are expected to hâve a high lignin content and in addition to being useful for producing energy through combustion in a Co-Generation plant, may hâve uses as other valuable products. For example, the lignin can be used as captured as a plastic, or it can be synthetically upgraded to other plastics. In some instances, it can also be converted to lignosulfonates, which can be utilized as binders, dispersants, emulsifiers or séquestrants.

When used as a binder, the lignin or a lignosulfonate can, e.g., be utilized in coal briquettes, in ceramics, for binding carbon black, for binding fertilizers and herbicides, as a dust suppressant, in the making of plywood and particle board, for binding animal feeds, as a binder for fiberglass, as a binder in linoléum paste and as a soil stabilizer.

When used as a dispersant, the lignin or lignosulfonates can be used, e.g., concrète mixes, clay and ceramics, dyes and pigments, leather tanning and in gypsum board.

When used as an emulsifier, the lignin or lignosulfonates can be used, e.g., in asphalt, pigments and dyes, pesticides and wax émulsions.

When used as a séquestrant, the lignin or lignosulfonates can be used, e.g., in micro-nutrient Systems, cleaning compounds and water treatment Systems, e.g., for boiler and cooling Systems.

For energy production lignin generally has a higher energy content than holocellulose (cellulose and hemicellulose) since it contains more carbon than homocellulose. For example, dry lignin can hâve an energy content of between about

11,000 and 12,500 BTU per pound, compared to 7,000 an 8,000 BTU per pound of holocellulose. As such, lignin can be densified and converted into briquettes and pellets for buming. For example, the lignin can be converted into pellets by any method described herein. For a slower buming pellet or briquette, the lignin can be crosslinked, such as applying a radiation dose of between about 0.5 Mrad and 5 Mrad. Crosslinking can make a slower buming form factor. The form factor, such as a pellet or briquette, can be converted to a “synthetic coal” or charcoal by pyrolyzing in the absence of air, e.g., at between 400 and 950 DEG C. Prior to pyrolyzing, it can be désirable to crosslink the lignin to maintain structural integrity.

SACCHARIFICATION

As previously described, in order to convert the feedstock to a form that can be readily processed the glucan- or xylan-containing cellulose in the feedstock can be 15 hydrolyzed to low molecular weight carbohydrates, such as sugars, by a saccharifying agent, e.g., an enzyme or acid, a process referred to as saccharification. The low molecular weight carbohydrates can then be used, for example, in an existing manufacturing plant, such as a single cell protein plant, an enzyme manufacturing plant, or a fuel plant, e.g., an éthanol manufacturing facility.

As previously dîsclosed, the feedstock can be hydrolyzed using an enzyme, e.g., by combining the materials and the enzyme in a solvent, e.g., in an aqueous solution.

Altematively, the enzymes can be supplied by organisms that break down biomass, such as the cellulose and/or the lignin portions of the biomass, contain or manufacture various cellulolytic enzymes (cellulases), ligninases or various small molécule biomass-degrading métabolites. These enzymes may be a complex of enzymes that act synergistically to dégradé crystalline cellulose or the lignin portions of biomass. Examples of cellulolytic enzymes include: endoglucanases, cellobiohydrolases, and cellobiases (beta-glucosidases).

During saccharification a cellulosic substrate can be initially hydrolyzed by endoglucanases at random locations producing oligomeric intermediates. These intermediates are then substrates for exo-splitting glucanases such as cellobiohydrolase to produce cellobiose from the ends of the cellulose polymer. Cellobiose is a watersoluble 1,4-linked dimer of glucose. Finally, cellobiase cleaves cellobiose to yield

glucose. The efficiency (e.g., time to hydrolyze and/or completeness of hydrolysis) of this process dépends on the recalcitrance of the cellulosic material.

Therefore, the treated biomass materials can be saccharified, by combining the material and a cellulase enzyme in a fluid medium, e.g., an aqueous solution. In some cases, the material is boiled, steeped, or cooked in hot water prior to saccharification, as described in U.S. Pat. App. Pub. 2012/0100577 Al by Medoff and Masterman, published on April 26, 2012, the entire contents of which are incorporated herein.

The saccharification process can be partially or completely performed in a tank (e.g., a tank having a volume of at least 4000, 40,000, or 500,000 L) in a manufacturing plant, and/or can be partially or completely performed in transit, e.g., in a rail car, tanker truck, or in a supertanker or the hold of a ship. The time required for complété saccharification will dépend on the process conditions and the carbohydrate-containing material and enzyme used. If saccharification is performed in a manufacturing plant under controlled conditions, the cellulose may be substantially entirely converted to sugar, e.g., glucose in about 12-96 hours. If saccharification is performed partially or completely in transit, saccharification may take longer.

It is generally preferred that the tank contents be mixed during saccharification, e.g., using jet mixing as described in International App. No. PCT/US2010/035331, filed May 18, 2010, which was published in English as WO 2010/135380 and designated the United States, the full disclosure of which is incorporated by reference herein.

The addition of surfactants can enhance the rate of saccharification. Examples of surfactants include non-ionic surfactants, such as a TWEEN® 20 or TWEEN® 80 polyethylene glycol surfactants, ionic surfactants, or amphoteric surfactants.

It is generally preferred that the concentration of the sugar solution resulting from saccharification be relatively high, e.g., greater than 40%, or greater than 50, 60, 70, 80, 90 or even greater than 95% by weight. Water may be removed, e.g., by évaporation, to increase the concentration of the sugar solution. This reduces the volume to be shipped, and also inhibits microbial growth in the solution.

Alternatively, sugar solutions of lower concentrations may be used, in which case it may be désirable to add an antimicrobial additive, e.g., a broad spectrum antibiotic, in a low concentration, e.g., 50 to 150 ppm. Other suitable antibiotics include amphotericin B, ampicillin, chloramphenicol, ciprofloxacin, gentamicin, hygromycin B, kanamycin, neomycin, penicillin, puromycin, streptomycin. Antibiotics will inhibit growth of microorganisms during transport and storage, and can be used at appropriate

concentrations, e.g., between 15 and 1000 ppm by weight, e.g., between 25 and 500 ppm, or between 50 and 150 ppm. If desired, an antibiotic can be included even if the sugar concentration is relatively high. Altematively, other additives with anti-microbial of preservative properties may be used. Preferably the antimicrobial additive(s) are food5 grade.

A relatively high concentration solution can be obtained by limiting the amount of water added to the carbohydrate-containing material with the enzyme. The concentration can be controlled, e.g., by controlling how much saccharification takes place. For example, concentration can be increased by adding more carbohydrate10 containing material to the solution. In order to keep the sugar that is being produced in solution, a surfactant can be added, e.g., one of those discussed above. Solubîlity can also be increased by încreasing the température of the solution. For example, the solution can be maintained at a température of 40-50 DEG C, 60-80 DEG C, or even higher.

SACCHARIFYING AGENTS

Suitable cellulolytic enzymes include cellulases from species in the généra Bacillus, Coprinus, Myceliophthora, Cephalosporium, Scytalidium, Pénicillium,

Aspergillus, Pseudomonas, Humicola, Fusarium, Thielavia, Acremonium, Chrysosporium and Trichoderma, especially those produced by a strain selected from the species Aspergillus (see, e.g., EP Pub. No. 0 458 162), Humicola insolens (reclassified as Scytalidium thermophilum, see, e.g., U.S. Pat. No. 4,435,307), Coprinus cinereus, Fusarium oxysporum, Myceliophthora thermophila, Meripilus giganteus, Thielavia terrestris, Acremonium sp. (including, but not limited to, A. persicinum, A. acremonium, A. brachypenium, A. dichromosporum, A. obclavatum, A. pinkertoniae, A. roseogriseum, A. incoloratum, and A. furatum). Preferred strains include Humicola insolens DSM 1800, Fusarium oxysporum DSM 2672, Myceliophthora thermophila CBS 117.65, Cephalosporium sp. RYM-202, Acremonium sp. CBS 478.94, Acremonium sp.

CBS 265.95, Acremonium persicinum CBS 169.65, Acremonium acremonium AHU 9519, Cephalosporium sp. CBS 535.71, Acremonium brachypenium CBS 866.73, Acremonium dichromosporum CBS 683.73, Acremonium obclavatum CBS 311.74, Acremonium pinkertoniae CBS 157.70, Acremonium roseogriseum CBS 134.56, Acremonium incoloratum CBS 146.62, and Acremonium furatum CBS 299.70H.

Cellulolytic enzymes may also be obtained from Chrysosporium, preferably a strain of Chrysosporium lucknowense. Additional strains that can be used include, but are not limited to, Trichoderma (particularly T. viride, T. reesei, and T. koningii), alkalophilic Bacillus (see, for example, U.S. Pat. No. 3,844,890 and EP Pub. No. 0 458 162), and

Streptomyces (see, e.g., EP Pub. No. 0 458 162).

In addition to or in combination to enzymes, acids, bases and other chemicals (e.g., oxidants) can be utilized to saccharify lignocellulosic and cellulosic materials. These can be used in any combination or sequence (e.g., before, after and/or during addition of an enzyme). For example strong minerai acids can be utilized (e.g. HCl,

H2SO4, H3PO4) and strong bases (e.g., NaOH, KOH).

SUGARS

In the processes described herein, for example after saccharification, sugars (e.g., 15 glucose and xylose) can be isolated and/or purified. For example sugars can be isolated and/or purified by précipitation, crystallization, chromatography (e.g., simulated moving bed chromatography, high pressure chromatography), electrodialysis, centrifugation, extraction, any other isolation method known in the art, and combinations thereof.

HYDROGENATION AND OTHER CHEMICAL TRANSFORMATIONS

The processes described herein can include hydrogénation. For example glucose and xylose can be hydrogenated to sorbitol and xylitol respectively. Hydrogénation can be accomplished by use of a catalyst (e.g., Pt/gamma-A12O3, Ru/C, Raney Nickel, or 25 other catalysts know in the art) in combination with H2 under high pressure (e.g., 10 to 12000 psi). Other types of chemical transformation of the products from the processes described herein can be used, for example production of organic sugar derived products (e.g., furfural and furfural-derived products). Chemical transformations of sugar derived products are described in USSN 13/934,704 filed July 3,2013, the entire disclosure of which is incorporated herein by reference in its entirety.

FERMENTATION

Yeast and Zymomonas bacteria, for example, can be used for fermentation or conversion of sugar(s) to alcohol(s). Other microorganisms are discussed below. The optimum pH for fermentations is about pH 4 to 7. For example, the optimum pH for yeast is from about pH 4 to 5, while the optimum pH for Zymomonas is from about pH 5 to 6. Typical fermentation times are about 24 to 168 hours (e.g., 24 to 96 hrs) with températures in the range of 20°C to 40°C (e.g., 26°C to 40°C), however thermophilic microorganisms prefer higher températures.

In some embodiments, e.g., when anaérobie organisms are used, at least a portion of the fermentation is conducted in the absence of oxygen, e.g., under a blanket of an inert gas such as N2, Ar, He, CO2 or mixtures thereof. Additionally, the mixture may hâve a constant purge of an inert gas flowing through the tank during part of or ail of the fermentation. In some cases, anaérobie condition, can be achieved or maintained by carbon dioxide production during the fermentation and no additional inert gas is needed.

In some embodiments, ail or a portion of the fermentation process can be interrupted before the low molecular weight sugar is completely converted to a product (e.g., éthanol). The intermediate fermentation products include sugar and carbohydrates in high concentrations. The sugars and carbohydrates can be isolated via any means known in the art. These intermediate fermentation products can be used in préparation of food for human or animal consumption. Additionally or alternatively, the intermediate fermentation products can be ground to a fine particle size in a stainless-steel laboratory mill to produce a flour-like substance. Jet mixing may be used during fermentation, and in some cases saccharification and fermentation are performed in the same tank.

Nutrients for the microorganisms may be added during saccharification and/or fermentation, for example the food-based nutrient packages described in U.S. Pat App. Pub. 2012/0052536, filed July 15, 2011, the complété disclosure of which is incorporated herein by reference.

“Fermentation” includes the methods and products that are disclosed in application Nos. PCT/US2012/71093 published June 27,2013, PCT/ US2012/71907 published June 27, 2012, and PCT/US2012/71083 published June 27, 2012 the contents of which are incorporated by reference herein in their entirety.

Mobile fermentera can be utilized, as described in International App. No. PCT/US2007/074028 (which was filed July 20, 2007, was published in English as WO 2008/011598 and designated the United States) and has a US issued Patent No. 8,318,453, the contents of which are incorporated herein in its entirety. Similarly, the saccharification equipment can be mobile. Further, saccharification and/or fermentation may be performed in part or entirely during transit.

FERMENTATION AGENTS

The microorganism(s) used in fermentation can be naturally-occurring microorganisms and/or engineered microorganisms. For example, the microorganism can be a bacterium (încluding, but not limited to, e.g., a cellulolytic bacterium), a fungus, (încluding, but not limited to, e.g., a yeast), a plant, a protist, e.g., a protozoa or a funguslike protest (încluding, but not limited to, e.g., a slime mold), or an alga. When the organisme are compatible, mixtures of organisais can be utilized.

Suitable fermenting microorganisms hâve the ability to convert carbohydrates, such as glucose, fructose, xylose, arabinose, mannose, galactose, oligosaccharides or polysaccharides into fermentation products. Fermenting microorganisms include strains of the genus Saccharomyces spp. (încluding, but not limited to, S. cerevisiae (baker’s yeast), S. distaticus, S. uvarum), the genus Kluyveromyces, (încluding, but not limited to, K. marxianus, K. fragilis), the genus Candida (încluding, but not limited to, C. pseudotropicalis, and C. brassicae), Pichia stipitis (a relative of Candida shehatae), the genus Clavispora (încluding, but not limited to, C. lusitaniae and C. opuntiae), the genus Pachysolen (încluding, but not limited to, P. tannophilus), the genus Bretannomyces (încluding, but not limited to, e.g., B. clausenii (Philippidis, G. P., 1996, Cellulose bioconversion technology, in Handbook on Bioethanol: Production and Utilization, Wyman, C.E., ed., Taylor & Francis, Washington, DC, 179-212)). Other suitable microorganisms include, for example, Zymomonas mobilis, Clostridium spp. (încluding, but not limited to, C. thermocellum (Philippidis, 1996, supra), C. saccharobutylacetonicum, C. tyrobutyricum C. saccharobutylicum, C. Puniceum, C. beijernckii, and C. acetobutylicum), Moniliella spp. (încluding but not limited to M. pollinis.M. tomentosa, M. madida, M. nigrescens, M. oedocephali, M. megachiliensis), Yarrowia lipolytica, Aureobasidium sp., Trichosporonoides sp., Trigonopsis variabilis, Trichosporon sp., Moniliellaacetoabutans sp., Typhula variabilis, Candida magnoliae,

Ustilaginomycetes sp., Pseudozyma tsukubaensis, yeast species of généra Zygosaccharomyces, Debaryomyces, Hansenula and Pichia, and fungi of the dematioid genus Torula (e.g., T.corallina).

Additîonal microorganisms include the Lactobacillus group. Examples include

Lactobacillus casei, Lactobacillus rhamnosus, Lactobacillus delbrueckii, Lactobacillus plantarum, Lactobacillus coryniformis, e.g., Lactobacillus coryniformis subspecies torquens, Lactobacillus pentosus, Lactobacillus brevis. Other microorganisms include Pediococus penosaceus, Rhizopus oryzae.

Several organisms, such as bacteria, yeasts and fungi, can be utilized to ferment biomass derived products such as sugars and alcohols to succinic acid and similar products. For example, organisms can be selected from,· Actinobacillus succinogenes, Anaerobiospirillum succiniciproducens, Mannheimia succiniciproducens, Ruminococcus flaverfaciens, Ruminococcus albus, Fibrobacter succinogenes, Bacteroides fragilis, Bacteroides ruminicola, Bacteroides amylophilus.Bacteriodes succinogenes,

Mannheimia succiniciproducens, Corynebacterium glutamicum, Aspergillus niger, Aspergillus fumigatus, Byssochlamys nivea, Lentinus de gene r, Paecilomyces varioti, Pénicillium viniferum, Saccharomyces cerevisiae, Enterococcus faecali, Prevotella ruminicolas, Debaryomyces hansenii, Candida catenulata VKM Y-5, C. mycoderma VKM Y-240, C. rugosa VKM Y-67, C. paludigena VKM Y-2443, C. utilis VKM Y-74,

C. utilis 766, C. zeylanoides VKM Y-6, C. zeylanoides VKM Y-14, C. zeylanoides VKM Y-2324, C. zeylanoides VKM Y-1543, C. zeylanoides VKM Y-2595, C. valida VKM Y934, Kluyveromyces wickerhamii VKM Y-589, Pichia anomala VKM Y-118, P. besseyi VKM Y-2084, P. media VKM Y-1381, P. guilliermondii H-P-4, P. guilliermondii 916, P. inositovora VKM Y-2494, Saccharomyces cerevisiae VKM Y-381, Torulopsis candida 127, T. candida 420, Yarrowia lipolytica 12a, Y. lipolytica VKM Y-47, Y. lipolytica 69, Y. lipolytica VKM Y-57, Y. lipolytica 212, Y. lipolytica 374/4, Y. lipolytica 585, Y. lipolytica 695, Y. lipolytica 704, and mixtures of these organisms.

Many such microbial strains are publicly available, either commercially or through depositories such as the ATCC (American Type Culture Collection, Manassas, 30 Virginia, USA), the NRRL (Agricultural Research Service Culture Collection, Peoria, Illinois, USA), or the DSMZ (Deutsche Sammlung von Mikroorganismen und Zellkulturen GmbH, Braunschweig, Germany), to name a few.

Commercially available yeasts include, for example, RED STAR®/Lesaffre Ethanol Red (available from Red Star/Lesaffre, USA), FALI® (available from

Fleischmann’s Yeast, a division of Bums Philip Food Inc., USA), SUPERSTART® (available from Alltech, now Lalemand), GERT STRAND® (available from Gert Strand AB, Sweden) and FERMOL® (available from DSM Specialties).

DISTILLATION

As previously described, after fermentation, the resulting fluids can be distilled using, for example, a “beer column” to separate éthanol and other alcohols from the majority of water and residual solids. The vapor exiting the beer column can be, e.g., 35% by weight éthanol and can be fed to a rectification column. A mixture of nearly azeotropic (92.5%) éthanol and water from the rectification column can be purified to pure (99.5%) éthanol using vapor-phase molecular sieves. The beer column bottoms can be sent to the first effect of a three-effect evaporator. The rectification column reflux condenser can provide heat for this first effect. After the first effect, solids can be separated using a centrifuge and dried in a rotary diyer. A portion (25%) of the centrifuge effluent can be recycled to fermentation and the rest sent to the second and third evaporator effects. Most of the evaporator condensate can be retumed to the process as fairly clean condensate with a small portion split off to waste water treatment to prevent build-up of low-boiling compounds.

HYDROCARBON-CONTAINING MATERIALS

In other embodiments utilizing the methods and Systems described herein, hydrocarbon-containing materials, for example, mixed with biomass can be processed. For example, the energy generated in a cogénération plant can be used to process hydrocarbon containing materials, or hydrocarbon containing materials can used in producing energy by providing fuel for a boiler. Some of the process described herein can be used to treat any hydrocarbon-containing material herein described. “Hydrocarbon-containing materials,” as used herein, is meant to include oil sands, oil shale, tar sands, coal dust, coal slurry, bitumen, various types of coal, and other naturally-occurring and synthetic materials that include both hydrocarbon components and solid matter. The solid matter can include rock, sand, clay, stone, silt, drilling slurry, or other solid organic and/or inorganic matter. The term can also include waste products such as drilling waste and by-products, refining waste and by-products, or other waste

products containing hydrocarbon components, such as asphalt shingling and covering, asphalt pavement, etc.

CONVEYING SYSTEMS

Various conveying Systems can be used to convey the biomass material, for example, as discussed, to a vault, and under an électron beam in a vault. Exemplary conveyors are belt conveyors, pneumatic conveyors, screw conveyors, caris, trains, trains or caris on rails, elevators, front loaders, backhoes, crânes, various scrapers and shovels, o trucks, and throwing devices can be used. For example, vibratory conveyors can be used in various processes described herein. Vibratory conveyors are described in PCT/US2013/64289 flled October 10, 2013 the full disclosure of which is incorporated by reference herein.

Vibratory conveyors are particularly useful for spreading the material and producing a uniform layer on the conveyor trough surface. For example the initial feedstock can form a pile of material that can be at least four feet high (e.g., at least about 3 feet, at least about 2 feet, at least about 1 foot, at least about 6 inches, at least about 5 inches, at least about, 4 inches, at least about 3 inches, at least about 2 inches, at least about 1 inch, at least about Vi inch) and spans less than the width of the conveyor (e.g., less than about 10%, less than about 20%, less than about 30%, less than about

40%, less than about 50%, less than about 60%, less than about 70%, less than about 80%, less than about 90%, less than about 95%, less than about 99%). The vibratory conveyor can spread the material to span the entire width of the conveyor trough and hâve a uniform thickness, preferably as discussed above. In some cases, an additional spreading method can be useful. For example, a spreader such as a broadcast spreader, a drop spreader (e.g., a CHRISTY SPREADER™) or combinations thereof can be used to drop (e.g., place, pour, spill and/or sprinkle) the feedstock over a wide area. Optionally, the spreader can deliver the biomass as a wide shower or curtain onto the vibratory conveyor. Additionally, a second conveyor, upstream from the first conveyor (e.g., the first conveyor is used in the irradiation of the feedstock), can drop biomass onto the first conveyor, where the second conveyor can hâve a width transverse to the direction of conveying smaller than the first conveyor. In particular, when the second conveyor is a vibratory conveyor, the feedstock is spread by the action of the second and first conveyor. In some optional embodiments, the second conveyor ends in a bias cross eut

discharge (e.g., a bias eut with a ratio of 4:1) so that the material can be dropped as a wide curtain (e.g., wider than the width of the second conveyor) onto the first conveyor. The initial drop area of the biomass by the spreader (e.g., broadcast spreader, drop spreader, conveyor, or cross eut vibratory conveyor) can span the entire width of the first vibratory conveyor, or it can span part of this width. Once dropped onto the conveyor, the material is spread even more uniformly by the vibrations of the conveyor so that, preferably, the entire width of the conveyor is covered with a uniform layer of biomass. In some embodiments combinations of spreaders can be used. Some methods of spreading a feed stock are described in U.S. Patent No. 7,153,533, filed July 23, 2002 and published December 26, 2006, the entire disclosure of which is incorporated herein by reference.

Generally, it is preferred to convey the material as quickly as possible through an électron beam to maximize throughput. For example, the material can be conveyed at rates of at least 1 ft/min, e.g., at least 2 ft/min, at least 3 ft/min, at least 4 ft/min, at least 5 ft/min, at least 10 ft/min, at least 15 ft/min, at least 20 ft/min, at least 25 ft/min, at least 30 ft/min, at least 40 ft/min, at least 50 ft/min, at least 60 ft/min, at least 70 ft/min, at least 80 ft/min, at least 90 ft/min. The rate of conveying is related to the beam current and targeted irradiation dose, for example, for a % inch thick biomass spread over a 5.5 foot wide conveyor and 100 mA, the conveyor can move at about 20 ft/min to provide a useful irradiation dosage (e.g. about 10 Mrad for a single pass), at 50 mA the conveyor can move at about 10 ft/min to provide approximately the same irradiation dosage.

The rate at which material can be conveyed dépends on the shape and mass of the material being conveyed, and the desired treatment. Flowing materials e.g., particulate materials, are particularly amenable to conveying with vibratory conveyors. Conveying speeds can, for example be, at least 100 lb/hr (e.g., at least 500 lb/hr, at least 1000 lb/hr, at least 2000 lb/hr, at least 3000 lb/hr, at least 4000 lb/hr, at least 5000 lb/hr, at least 10,000 lb/hr, at least 15, 000 lb/hr, or even at least 25,000 lb/hr). Some typical conveying speeds can be between about 1000 and 10,000 lb/hr, (e.g., between about 1000 lb/hr and 8000 lb/hr, between about 2000 and 7000 lb/hr, between about 2000 and 6000 lb/hr, between about 2000 and 50001b/hr, between about 2000 and 4500 lb/hr, between about 1500 and 5000 lb/hr, between about 3000 and 7000 lb/hr, between about 3000 and 6000 lb/hr, between about 4000 and 6000 lb/hr and between about 4000 and 5000 lb/hr). Typical conveying speeds dépend on the density of the material. For example, for a biomass with a density of about 35 lb/ft³, and a conveying speed of about 5000 lb/hr, the material is conveyed at a rate of about 143 ft³/hr, if the material is 14” thick and is in a trough 5.5 ft wide, the material is conveyed at a rate of about 1250 ft/hr (about 21 ft/min). Rates of conveying the material can therefore vary greatly. Preferably, for example, a U” thick layer of biomass, is conveyed at speeds of between about 5 and 100 ft/min (e.g. between about 5 and 100 ft/min, between about 6 and 100 ft/min, between about 7 and 100 ft/min, between about 8 and 100 ft/min, between about 9 and 100 ft/min, between about 10 and 100 ft/min, between about 11 and 100 ft/min, between about 12 and 100 ft/min, between about 13 and 100 ft/min, between about 14 and 100 ft/min, between about 15 and 100 ft/min, between about 20 and 100 ft/min, between about 30 and 100 ft/min, between about 40 and 100 ft/min, between about 2 and 60 ft/min, between about 3 and 60 ft/min, between about 5 and 60 ft/min, between about 6 and 60 ft/min, between about 7 and 60 ft/min, between about 8 and 60 ft/min, between about 9 and 60 ft/min, between about 10 and 60 ft/min, between about 15 and 60 ft/min, between about 20 and 60 ft/min, between about 30 and 60 ft/min, between about 40 and 60 ft/min, between about 2 and 50 ft/min, between about 3 and 50 ft/min, between about 5 and 50 ft/min, between about 6 and 50 ft/min, between about 7 and 50 ft/min, between about 8 and 50 ft/min, between about 9 and 50 ft/min, between about 10 and 50 ft/min, between about 15 and 50 ft/min, between about 20 and 50 ft/min, between about 30 and 50 ft/min, between about 40 and 50 ft/min). It is préférable that the material be conveyed at a constant rate, for example, to help maintain a constant irradiation of the material as it passes under the électron beam (e.g., shower, field).

The vibratory conveyors described can include screens used for sieving and sorting materials. Port openings on the side or bottom of the troughs can be used for sorting, selecting or removing spécifie materials, for example, by size or shape. Some conveyors hâve counterbalances to reduce the dynamic forces on the support structure. Some vibratory conveyors are configured as spiral elevators, are designed to curve around surfaces and/or are designed to drop material from one conveyor to another (e.g., in a step, cascade or as a sériés of steps or a stair). Along with conveying materials conveyors can be used, by themselves or coupled with other equipment or Systems, for screening, separating, sorting, classifying, distributing, sizing, inspection, picking, métal removing, freezing, blending, mixing, orienting, heating, cooking, drying, dewatering, cleaning, washing, leaching, quenching, coating, de-dusting and/or feeding. The conveyors can also include covers (e.g., dust-tight covers), side discharge gates, bottom discharge gates, spécial liners (e.g., anti-stick, stainless steel, rubber, custom steal, and or grooved), divided troughs, quench pools, screens, perforated plates, detectors (e.g., métal detectors), high température designs, food grade designs, heaters, dryers and or coolers. In addition, the trough can be of various shapes, for example, fiat bottomed, vee shaped bottom, flanged at the top, curved bottom, fiat with ridges in any direction, tubular, half pipe, covered or any combinations of these. In particular, the conveyors can be coupled with an irradiation Systems and/or equipment.

The conveyors (e.g., vibratory conveyor) can be made of corrosion résistant materials. The conveyors can utilize structural materials that include stainless steel (e.g., 304, 316 stainless steel, HASTELLOY® ALLOYS and INCONEL® Alloys). For example, HASTELLOY® Corrosion-Résistant alloys from Hynes (Kokomo, Indiana, USA) such as HASTELLOY® B-3® ALLOY, HASTELLOY® HYBRID-BC1® ALLOY, HASTELLOY® C-4 ALLOY, HASTELLOY® C-22® ALLOY, HASTELLOY® C-22HS® ALLOY, HASTELLOY® C-276 ALLOY, HASTELLOY® C-2000® ALLOY, HASTELLOY® G-30® ALLOY, HASTELLOY® G-35® ALLOY, HASTELLOY® N ALLOY and HASTELLOY® ULTIMET® alloy.

The vibratory conveyors can include non-stick release coatings, for example, TUFFLON™ (Dupont, Delawaie, USA). The vibratory conveyors can also include corrosion résistant coatings. For example, coatings that can be supplied from Métal Coatings Corp (Houston, Texas, USA) and others such as Fluoropolymer, XYLAN®, Molybdenum Disulfide, Epoxy Phenolic, Phosphate- ferrous métal coating, Polyuréthane- high gloss topcoat for epoxy, inorganic zinc, Poly Tetrafluoro ethylene, PPS/RYTON®, fluorinated ethylene propylene, PVDF/DYKOR®, ECTFE/HALAR® and Ceramic Epoxy Coating. The coatings can improve résistance to process gases (e.g., ozone), chemical corrosion, pitting corrosion, galling corrosion and oxidation.

Optionally, in addition to the conveying Systems described herein, one or more other conveying Systems can be enclosed. When using an enclosure, the enclosed conveyor can also be purged with an inert gas so as to maintain an atmosphère at a reduced oxygen level. Keeping oxygen levels low avoids the formation of ozone which in some instances is undesirable due to its reactive and toxic nature. For example, the oxygen can be less than about 20% (e.g., less than about 10%, less than about 1%, less than about 0.1 %, less than about 0.01 %, or even less than about 0.001 % oxygen). Purging can be done with an inert gas including, but not limited to, nitrogen, argon, hélium or carbon dioxide. This can be supplied, for example, from a boil off of a liquid source (e.g., liquid nitrogen or hélium), generated or separated from air in situ, or supplied from tanks. The inert gas can be recirculated and any residual oxygen can be removed using a catalyst, such as a copper catalyst bed. Altematively, combinations of purging, recirculating and oxygen removal can be done to keep the oxygen levels low.

The enclosed conveyor can also be purged with a reactive gas that can react with the biomass. This can be done before, during or after the irradiation process. The reactive gas can be, but is not limited to, nitrous oxide, ammonia, oxygen, ozone, hydrocarbons, aromatic compounds, amides, peroxides, azides, halides, oxyhalides, phosphides, phosphines, arsines, sulfides, thiols, boranes and/or hydrides. The reactive gas can be activated in the enclosure, e.g., by irradiation (e.g., électron beam, UV irradiation, microwave irradiation, heating, IR radiation), so that it reacts with the biomass. The biomass itself can be activated, for example by irradiation. Preferably the biomass is activated by the électron beam, to produce radicals which then react with the activated or unactivated reactive gas, e.g., by radical coupling or quenching.

Purging gases supplied to an enclosed conveyor can also be cooled, for example below about 25°C, below about 0°C, below about -40°C, below about -80°C, below about -120°C. For example, the gas can be boiled off from a compressed gas such as liquid nitrogen or sublimed from solid carbon dioxide. As an alternative example, the gas can be cooled by a chiller or part of or the entire conveyor can be cooled.

OTHER EMBODIMENTS

Any material, processes or processed materials dîscussed herein can be used to make products and/or intermediates such as composites, fillers, binders, plastic additives, adsorbents and controlled release agents. The methods can include densification, for example, by applying pressure and heat to the materials. For example composites can be made by combining fibrous materials with a resin or polymer. For example radiation cross-linkable resin, e.g., a thermoplastic resin can be combined with a fibrous material to provide a fibrous material/cross-linkable resin combination. Such materials can be, for example, useful as building materials, protective sheets, containers and other structural materials (e.g., molded and/or extruded products). Absorbents can be, for example, in the form of pellets, chips, fibers and/or sheets. Adsorbents can be used, for example, as pet bedding, packaging material or in pollution control Systems. Controlled release matrices can also be the form of, for example, pellets, chips, fibers and or sheets. The controlled release matrices can, for example, be used to release drugs, biocides, fragrances. For

example, composites, absorbents and control release agents and their uses are described in International Serial No. PCT/US2006/010648, filed March 23, 2006, and US Patent No. 8,074,910 filed November 22, 2011, the entire disclosures of which are herein incorporated by reference.

In some instances the biomass material is treated at a first level to reduce recalcitrance, e.g., utilizing accelerated électrons, to selectively release one or more sugars (e.g., xylose). The biomass can then be treated to a second level to release one or more other sugars (e.g., glucose). Optionally the biomass can be dried between treatments. The treatments can include applying chemical and biochemical treatments to release the sugars. For example, a biomass material can be treated to a level of less than about 20 Mrad (e.g., less than about 15 Mrad, less than about 10 Mrad, less than about 5 Mrad, less than about 2 Mrad) and then treated with a solution of sulfuric acid, containing less than 10% sulfuric acid (e.g., less than about 9%, less than about 8%, less than about 7%, less than about 6%, less than about 5%, less than about 4%, less than about 3%, less than about 2%, less than about 1%, less than about 0.75%, less than about 0.50 %, less than about 0.25%) to release xylose. Xylose, for example that is released into solution, can be separated from solids and optionally the solids washed with a solvent/solution (e.g., with water and/or acidified water). Optionally, the solids can be dried, for example in air and/or under vacuum optionally with heating (e.g., below about

1 50 deg C, below about 120 deg C) to a water content below about 25 wt% (below about wt.%, below about 15 wt.%, below about 10 wt.%, below about 5 wt.%). The solids can then be treated with a level of less than about 30 Mrad (e.g., less than about 25 Mrad, less than about 20 Mrad, less than about 15 Mrad, less than about 10 Mrad, less than about 5 Mrad, less than about 1 Mrad or even not at ail) and then treated with an enzyme (e.g., a cellulase) to release glucose. The glucose (e.g., glucose in solution) can be separated from the remaining solids. The solids can then be further processed, for example utilized to make energy or other products (e.g., lignin derived products).

FLAVORS, FRAGRANCES AND COLORANTS

Any of the products and/or intermediates described herein, for example, produced by the processes, Systems and/or equipment described herein, can be combined with flavors, fragrances, colorants and/or mixtures of these. For example, any one or more of (optionally along with flavors, fragrances and/or colorants) sugars, organic acids, fuels,

polyols, such as sugar alcohols, biomass, fibers and composites can be combined with (e.g., formulated, mixed or reacted) or used to make other products. For example, one or more such product can be used to make soaps, détergents, candies, drinks (e.g., cola, wine, beer, liquors such as gin or vodka, sports drinks, coffees, teas), syrups pharmaceuticals, adhesives, sheets (e.g., woven, none woven, filters, tissues) and/or composites (e.g., boards). For example, one or more such product can be combined with herbs, flowers, petals, spices, vitamins, potpourri, or candies. For example, the formulated, mixed or reacted combinations can hâve flavors/fragrances of grapefruit, orange, apple, raspberry, banana, lettuce, celery, cinnamon, chocolaté, vanilla, peppermint, mint, onion, garlic, pepper, saffron, ginger, milk, wine, beer, tea, lean beef, fish, clams, olive oil, coconut fat, pork fat, butter fat, beef bouillon, legume, potatoes, marmalade, ham, coffee and cheeses.

Flavors, fragrances and colorants can be added in any amount, such as between about 0.001 wt.% to about 30 wt.%, e.g., between about 0.01 to about 20, between about 0.05 to about 10, or between about 0.1 wt.% to about 5 wt.%. These can be formulated, mixed and or reacted (e.g., with any one of more product or intermediate described herein) by any means and in any order or sequence (e.g., agitated, mixed, emulsified, gelled, infused, heated, sonicated, and/or suspended). Fillers, binders, emulsifier, antioxidants can also be utilized, for example protein gels, starches and silica.

In one embodiment the flavors, fragrances and colorants can be added to the biomass immediately after the biomass is irradiated such that the reactive sites created by the irradiation may react with reactive compatible sites of the flavors, fragrances, and colorants.

The flavors, fragrances and colorants can be naturel and/or synthetic materials. These materials can be one or more of a compound, a composition or mixtures of these (e.g., a formulated or naturel composition of several compounds). Optionally the flavors, fragrances, antioxidants and colorants can be derived biologically, for example, from a fermentation process (e.g., fermentation of saccharified materials as described herein). Altematively, or additionally these flavors, fragrances and colorants can be harvested from a whole organisai (e.g., plant, fungus, animal, bacteria or yeast) or a part of an organism. The organism can be collected and or extracted to provide color, flavors, fragrances and/or antioxidant by any means including utilizing the methods, Systems and equipment described herein, hot water extraction, supercritical fluid extraction, chemical extraction (e.g., solvent or reactive extraction including acids and bases), mechanical extraction (e.g., pressing, comminuting, filtering), utilizing an enzyme, utilizing a bacteria such as to break down a starting material, and combinations of these methods. The compounds can be derived by a chemical reaction, for example, the combination of a sugar (e.g., as produced as described herein) with an amino acid (Maillard reaction). The flavor, fragrance, antioxidant and/or colorant can be an intermediate and or product produced by the methods, equipment or Systems described herein, for example and ester and a lignin derived product.

Some examples of flavor, fragrances or colorants are polyphenols. Polyphenols are pigments responsible for the red, purple and blue colorants of many fruits, vegetables, cereal grains, and flowers. Polyphenols also can hâve antioxidant properties and often hâve a bitter taste. The antioxidant properties make these important preservatives. On class of polyphenols are the flavonoids, such as Anthocyanidines, flavanonols, flavan-3-ols, s, flavanones and flavanonols. Other phenolic compounds that can be used include phenolic acids and their esters, such as chlorogenic acid and polymeric tannins.

Among the colorants inorganic compounds, minerais or organic compounds can be used, for example titanium dioxide, zinc oxide, aluminum oxide, cadmium yellow (E.g., CdS), cadmium orange (e.g., CdS with some Se), alizarin crimson (e.g., synthetic or non-synthetic rose madder), ultramarine (e.g., synthetic ultramarine, natural ultramarine, synthetic ultramarine violet ), cobalt blue, cobalt yellow, cobalt green, viridian (e.g., hydrated chromium(III)oxide), chalcophylite, conichalcite, comubite, comwallite and liroconite. Black pigments such as carbon black and self-dispersed blacks may be used.

Some flavors and fragrances that can be utilized include ACALEA TBHQ, ACET C-6, ALLYL AMYL GLYCOLATE, ALPHA TERPENEOL, AMBRETTOLIDE, AMBRINOL 95, ANDRANE, APHERMATE, APPLELIDE, BACDANOL®, BERGAMAL, BETA IONONE EPOXIDE, BETA NAPHTHYL ISO-BUTYL ETHER, BICYCLONONALACTONE, BORNAFIX®, CANTHOXAL, CASHMERAN®, CASHMERAN® VELVET, CASSIFFIX®, CEDRAFIX, CEDRAMBER®, CEDRYL ACETATE, CELESTOLIDE, CINNAMALVA, CITRAL DIMETHYL ACETATE, CITROLATE™, CITRONELLOL 700, CITRONELLOL 950, CITRONELLOL COEUR, CITRONELLYL ACETATE, CITRONELLYL ACETATE PURE, CITRONELLYL FORMATE, CLARYCET, CLONAL, CONIFERAN, CONEFERAN PURE, CORTEX ALDEHYDE 50% PEOMOSA, CYCLABUTE, CYCLACET®,

CYCLAPROP®, CYCLEMAX™, CYCLOHEXYL ETHYL ACETATE, DAMASCOL, DELTA DAMASCONE, DIHYDRO CYCLACET, DIHYDRO MYRCENOL, DIHYDRO TERPINEOL, DIHYDRO TERPINYL ACETATE, DIMETHYL CYCLORMOL, DIMETHYL OCTANOL PQ, DIMYRCETOL, DIOLA, DIPENTENE,

DULCINYL® RECRYSTALLIZED, ETHYL-3-PHENYL GLYCIDATE, FLEURAMONE, FLEURANIL, FLORAL SUPER, FLORALOZONE, FLORIFFOL, FRAISTONE, FRUCTONE, GALAXOLIDE® 50, GALAXOLIDE® 50 BB, GALAXOLIDE® 50 IPM, GALAXOLIDE® UNDILUTED, GALBASCONE, GERALDEHYDE, GERANIOL 5020, GERANIOL 600 TYPE, GERANIOL 950, o GERANIOL 980 (PURE), GERANIOL CFT COEUR, GERANIOL COEUR, GERANYL ACETATE COEUR, GERANYL ACETATE, PURE, GERANYL FORMATE, GRISALVA, GUAIYL ACETATE, HELIONAL™, HERBAC, HERBALIME™, HEXADECANOLIDE, HEXALON, HEXENYL SALICYLATE CIS 3-, HYACINTH BODY, HYACINTH BODY NO. 3, HYDRATROPIC

ALDEHYDE.DMA, HYDROXYOL, INDOLAROME, INTRELEVEN ALDEHYDE, ENTRELEVEN ALDEHYDE SPECIAL, IONONE ALPHA, IONONE BETA, ISO CYCLO CITRAL, ISO CYCLO GERANIOL, ISO E SUPER®, ISOBUTYL QUINOLINE, JASMAL, JESSEMAL®, KHARISMAL®, KHARISMAL® SUPER, KHUSINIL, KOAVONE®, KOHINOOL®, LIFF AROME™, LIMOXAL,

LINDENOL™, LYRAL®, LYRAME SUPER, MANDARIN ALD 10% TRI ETH, CITR, MARTEMA, MCK CHINESE, MEIJIFF™, MELAFLEUR, MELOZONE, METHYL ANTHRANILATE, METHYL IONONE ALPHA EXTRA, METHYL IONONE GAMMA A, METHYL IONONE GAMMA COEUR, METHYL IONONE GAMMA PURE, METHYL LAVENDER KETONE, MONTAVERDI®, MUGUESIA,

MUGUET ALDEHYDE 50, MUSK Z4, MYRAC ALDEHYDE, MYRCENYL ACETATE, NECTARATE™, NEROL 900, NERYL ACETATE, OCIMENE, OCTACETAL, ORANGE FLOWER ETHER, ORIVONE, ORRINIFF 25%, OXASPIRANE, OZOFLEUR, PAMPLEFLEUR®, PEOMOSA, PHENOXANOL®, PICONIA, PRECYCLEMONE B, PRENYL ACETATE, PRISMANTOL, RESEDA

BODY, ROSALVA, ROSAMUSK, SANJINOL, SANTALIFF™, SYVERTAL, TERPINEOL,TERPINOLENE 20, TERPINOLENE 90 PQ, TERPINOLENE RECT., TERPINYL ACETATE, TERPINYL ACETATE JAX, TETRAHYDRO, MUGUOL®, TETRAHYDRO MYRCENOL, TETRAMERAN, TIMBERSELK™, TOBACAROL, TRIMOFIX® O TT, TRIPLAL®, TRISAMBER®, VANORIS, VERDOX™,

VERDOX™ HC, VERTENEX®, VERTENEX® HC, VERTOFIX® COEUR, VERTOLIFF, VERTOLIFF ISO, VIOLIFF, VIVALDIE, ZENOLIDE, ABS INDIA 75 PCT MIGLYOL, ABS MOROCCO 50 PCT DPG, ABS MOROCCO 50 PCT TEC, ABSOLUTE FRENCH, ABSOLUTE INDIA, ABSOLUTE MD 50 PCT BB, ABSOLUTE MOROCCO, CONCENTRATE PG, TINCTURE 20 PCT, AMBERGRIS, AMBRETTE ABSOLUTE, AMBRETTE SEED OIL, ARMOISE OIL 70 PCT THUYONE, BASIL ABSOLUTE GRAND VERT, BASIL GRAND VERT ABS MD, BASIL OIL GRAND VERT, BASIL OIL VER VEINA, BASIL OIL VIETNAM, BAY OIL TERPENELESS, BEESWAX ABS N G, BEESWAX ABSOLUTE, BENZOIN RESINOID SIAM, BENZOIN RESINOID SIAM 50 PCT DPG, BENZOIN RESINOID SIAM 50 PCT PG, BENZOIN RESINOID SIAM 70.5 PCT TEC, BLACKCURRANT BUD ABS 65 PCT PG, BLACKCURRANT BUD ABS MD 37 PCT TEC, BLACKCURRANT BUD ABS MIGLYOL, BLACKCURRANT BUD ABSOLUTE BURGUNDY, BOIS DE ROSE OIL, BRAN ABSOLUTE, BRAN RESINOID, BROOM ABSOLUTE ITALY, CARDAMOM GUATEMALA CO2 EXTRACT, CARDAMOM OIL GUATEMALA, CARDAMOM OIL INDIA, CARROT HEART, CASSEE ABSOLUTE EGYPT, CASSIE ABSOLUTE MD 50 PCT IPM, CASTOREUM ABS 90 PCT TEC, CASTOREUM ABS C 50 PCT MIGLYOL, CASTOREUM ABSOLUTE, CASTOREUM RESINOID, CASTOREUM RESINOID 50 PCT DPG, CEDROL CEDRENE, CEDRUS ATLANTICA OIL REDIST, CHAMOMILE OIL ROMAN, CHAMOMILE OIL WILD, CHAMOMILE OIL WILD LOW LIMONENE, CINNAMON BARK OIL CEYLAN, CISTE ABSOLUTE, CISTE ABSOLUTE COLORLESS, CITRONELLA OIL ASIA IRON FREE, CIVET ABS 75 PCT PG, CIVET ABSOLUTE, CIVET TINCTURE 10 PCT, CLARY SAGE ABS FRENCH DECOL, CLARY SAGE ABSOLUTE FRENCH, CLARY SAGE C'LESS 50 PCT PG, CLARY SAGE OIL FRENCH, COPAIBA BALSAM, COPAIBA BALSAM OIL, CORIANDER SEED OIL, CYPRESS OIL, CYPRESS OIL ORGANIC, DAVANA OIL, GALBANOL, GALBANUM ABSOLUTE COLORLESS, GALBANUM OIL, GALBANUM RESINOID, GALBANUM RESINOID 50 PCT DPG, GALBANUM RESINOID HERCOLYN BHT, GALBANUM RESINOID TEC BHT, GENTIANE ABSOLUTE MD 20 PCT BB, GENTIANE CONCRETE, GERANIUM ABS EGYPT MD, GERANIUM ABSOLUTE EGYPT, GERANIUM OIL CHINA, GERANIUM OIL EGYPT, GINGER OIL 624, GINGER OIL RECTIFIED SOLUBLE, GUAIACWOOD HEART, HAY ABS MD 50 PCT BB, HAY ABSOLUTE, HAY ABSOLUTE MD 50

PCT TEC, HEALINGWOOD, HYSSOP OIL ORGANIC, IMMORTELLE ABS YUGO MD 50 PCT TEC, IMMORTELLE ABSOLUTE SPAIN, IMMORTELLE ABSOLUTE YUGO, JASMIN ABS INDIA MD, JASMIN ABSOLUTE EGYPT, JASMIN ABSOLUTE INDIA, ASMIN ABSOLUTE MOROCCO, JASMIN ABSOLUTE SAMBAC, JONQUILLE ABS MD 20 PCT BB, JONQUILLE ABSOLUTE France, JUNIPER BERRY OIL FLG, JUNIPER BERRY OIL RECTIFIED SOLUBLE, LABDANUM RESINOID 50 PCT TEC, LABDANUM RESINOID BB, LABDANUM RESINOID MD, LABDANUM RESINOID MD 50 PCT BB, LAVANDIN ABSOLUTE H, LAVANDIN ABSOLUTE MD, LAVANDIN OIL ABRIAL ORGANIC, LAVANDIN OIL GROSSO ORGANIC, LAVANDIN OIL SUPER, LAVENDER ABSOLUTE H, LAVENDER ABSOLUTE MD, LAVENDER OIL COUMARIN FREE, LAVENDER OIL COUMARIN FREE ORGANIC, LAVENDER OIL MAILLETTE ORGANIC, LAVENDER OIL MT, MACE ABSOLUTE BB, MAGNOLIA FLOWER OIL LOW METHYL EUGENOL, MAGNOLIA FLOWER OIL, MAGNOLIA FLOWER OIL MD, MAGNOLIA LEAF OIL, MANDARIN OIL MD, MANDARIN OIL MD BHT, MATE ABSOLUTE BB, MOSS TREE ABSOLUTE MD TEX IFRA 43, MOSS-OAK ABS MD TEC IFRA 43, MOSS-OAK ABSOLUTE IFRA 43, MOSS-TREE ABSOLUTE MD IPM IFRA 43, MYRRH RESINOID BB, MYRRH RESINOID MD, MYRRH RESINOID TEC, MYRTLE OIL IRON FREE, MYRTLE OIL TUNISIA RECTIFIED, NARCISSE ABS MD 20 PCT BB, NARCISSE ABSOLUTE FRENCH, NEROLI OIL TUNISIA, NUTMEG OEL TERPENELESS, OEILLET ABSOLUTE, OLIBANUM RESINOID, OLIBANUM RESINOID BB, OLIBANUM RESINOID DPG, OLIBANUM RESINOID EXTRA 50 PCT DPG, OLIBANUM RESINOID MD, OLIBANUM RESINOID MD 50 PCT DPG, OLIBANUM RESINOID TEC, OPOPONAX RESINOID TEC, ORANGE BIGARADE OIL MD BHT, ORANGE BIGARADE OIL MD SCFC, ORANGE FLOWER ABSOLUTE TUNISIA, ORANGE FLOWER WATER ABSOLUTE TUNISIA, ORANGE LEAF ABSOLUTE, ORANGE LEAF WATER ABSOLUTE TUNISIA, ORRIS ABSOLUTE ITALY, ORRIS CONCRETE 15 PCT IRONE, ORRIS CONCRETE 8 PCT IRONE, ORRIS NATURAL 15 PCT IRONE 4095C, ORRIS NATURAL 8 PCT IRONE 2942C, ORRIS RESINOID, OSMANTHUS ABSOLUTE, OSMANTHUS ABSOLUTE MD 50 PCT BB, PATCHOULI HEART N°3, PATCHOULI OIL INDONESIA, PATCHOULI OIL INDONESIA IRON FREE, PATCHOULI OIL INDONESIA MD, PATCHOULI OIL REDIST, PENNYROYAL

HEART, PEPPERMINT ABSOLUTE MD, PETITGRAIN BIGARADE OIL TUNISIA, PETITGRAIN CITRONNIER OIL, PETITGRAIN OIL PARAGUAY TERPENELESS, PETITGRAIN OIL TERPENELESS STAB, PIMENTO BERRY OIL, PIMENTO LEAF OIL, RHODINOL EX GERANIUM CHINA, ROSE ABS BULGARIAN LOW METHYL EUGENOL, ROSE ABS MOROCCO LOW METHYL EUGENOL, ROSE ABS TURKISH LOW METHYL EUGENOL, ROSE ABSOLUTE, ROSE ABSOLUTE BULGARIAN, ROSE ABSOLUTE DAMASCENA, ROSE ABSOLUTE MD, ROSE ABSOLUTE MOROCCO, ROSE ABSOLUTE TURKISH, ROSE OIL BULGARIAN, ROSE OIL DAMASCENA LOW METHYL EUGENOL, ROSE OIL TURKISH, ROSEMARY OIL CAMPHOR ORGANIC, ROSEMARY OIL TUNISIA, SANDALWOOD OIL INDIA, SANDALWOOD OIL INDIA RECTIFIED, SANTALOL, SCHINUS MOLLE OIL, ST JOHN BREAD ITNCTURE 10 PCT, STYRAX RESINOID, STYRAX RESINOID, TAGETE OIL, TEA TREE HEART, TONKA BEAN ABS 50 PCT SOLVENTS, TONKA BEAN ABSOLUTE, TUBEROSE ABSOLUTE INDIA, VETIVER HEART EXTRA, VETIVER OIL HAITI, VETIVER OIL HAITI MD, VETIVER OIL JAVA, VETIVER OIL JAVA MD, VIOLET LEAF ABSOLUTE EGYPT, VIOLET LEAF ABSOLUTE EGYPT DECOL, VIOLET LEAF ABSOLUTE FRENCH, VIOLET LEAF ABSOLUTE MD 50 PCT BB, WORMWOOD OIL TERPENELESS, YLANG EXTRA OIL, YLANG ΙΠ OIL and combinations of these.

The colorants can be among those listed in the Color Index International by the Society of Dyers and Colourists. Colorants include dyes and pigments and include those commonly used for coloring textiles, paints, inks and inkjet inks. Some colorants that can be utilized include carotenoids, arylide yellows, diarylide yellows, β-naphthols, naphthols, benzimidazolones, disazo condensation pigments, pyrazolones, nickel azo yellow, phthalocyanines, quinacridones, perylenes and perinones, isoindolinone and isoindoline pigments, triarylcarbonium pigments, diketopyrrolo-pyrrole pigments, thioindigoids. Cartenoids include, for example, alpha-carotene, beta-carotene, gammacarotene, lycopene, lutein and astaxanthin Annatto extract, Dehydrated beets (beet powder), Canthaxanthin, Caramel, P-Apo-8'-carotenal, Cochineal extract, Carminé, Sodium copper chlorophyllin, Toasted partially defatted cooked cottonseed flour, Ferrous gluconate, Ferrous lactate, Grape color extract, Grape skin extract (enocianina), Carrot oil, Paprika, Paprika oleoresin, Mica-based pearlescent pigments, Riboflavin, Saffron, Titanium dioxide, Tomato lycopene extract; tomato lycopene concentrate,

Turmenc, Turmenc oleoresin, FD&C Blue No. 1, FD&C Blue No. 2, FD&C Green No. 3, Orange B, Citrus Red No. 2, FD&C Red No. 3, FD&C Red No. 40, FD&C Yellow No. 5, FD&C Yellow No. 6, Alumina (dried aluminum hydroxide), Calcium carbonate, Potassium sodium copper chlorophyllin (chlorophyllin-copper complex), Dihydroxyacetone, Bismuth oxychloride, Ferrie ammonium ferrocyanide, Ferrie ferrocyanide, Chromium hydroxide green, Chromium oxide greens, Guanine, Pyrophyllite, Talc, Aluminum powder, Bronze powder, Copper powder, Zinc oxide, D&C Blue No. 4, D&C Green No. 5, D&C Green No. 6, D&C Green No. 8, D&C Orange No. 4, D&C Orange No. 5, D&C Orange No. 10, D&C Orange No. 11, FD&C Red No. 4, D&C Red No. 6, D&C Red No. 7, D&C Red No. 17, D&C Red No. 21, D&C Red No. 22, D&C Red No. 27, D&C Red No. 28, D&C Red No. 30, D&C Red No. 31, D&C Red No. 33, D&C Red No. 34, D&C Red No. 36, D&C Red No. 39, D&C Violet No. 2, D&C Yellow No. 7, Ext. D&C Yellow No. 7, D&C Yellow No. 8, D&C Yellow No. 10, D&C Yellow No. 11, D&C Black No. 2, D&C Black No. 3 (3), D&C Brown No.

1, Ext. D&C, Chromium-cobalt-aluminum oxide, Ferrie ammonium citrate, Pyrogallol, Logwood extract, l,4-Bis[(2-hydroxy-ethyl)amino]-9,10-anthracenedione bis(2propenoic)ester copolymers, 1,4-Bis [(2-methylphenyl)amino] -9,10-anthracenedione,

I, 4-Bis[4- (2-methacryloxyethyl) phenylamino] anthraquinone copolymers, Carbazole violet, Chlorophyllin-copper complex, Chromium-cobalt-aluminum oxide,, C.I. Vat Orange 1, 2-[[2,5-Diethoxy- 4-[(4-methylphenyl)thiol] phenyljazo] -1,3,5-benzenetriol, 16,23-Dihydrodinaphtho [2,3-a:2*,3'-i] naphth [2',3':6,7] indolo [2,3-c] carbazole5,10,15,17,22,24-hexone, N,N’-(9,10-Dihydro- 9,10-dioxo- 1,5-anthracenediyl) bisbenzamide, 7,16-Dichloro- 6,15-dihydro- 5,9,14,18-anthrazinetetrone, 16,17Dimethoxydinaphtho (l,2,3-cd:3',2',l'-lm) perylene-5,10-dione, Poly(hydroxyethyl méthacrylate) -dye copolymers(3), Reactive Black 5, Reactive Blue 21, Reactive Orange 78, Reactive Yellow 15, Reactive Blue No. 19, Reactive Blue No. 4, C.I. Reactive Red

II, C.I. Reactive Yellow 86, C.I. Reactive Blue 163, C.I. Reactive Red 180, 4-[(2,4dimethylphenyl)azo]- 2,4-dihydro- 5-methyl-2-phenyl- 3H-pyrazol-3-one (solvent Yellow 18), 6-Ethoxy-2- (6-ethoxy-3-oxobenzo[b] thien-2(3H)- ylidene) benzo[b]thiophen- 3(2H)-one, Phthalocyanine green, Vinyl alcohol/methyl methacrylatedye reaction products, C.I. Reactive Red 180, C.I. Reactive Black 5, C.I. Reactive Orange 78, C.I. Reactive Yellow 15, C.I. Reactive Blue 21, Disodium l-amino-4-[[4-[(2bromo- l-oxoallyl)amino]-2-sulphonatophenyl]amino]-9,10-dihydro-9,1017466 dioxoanthracene-2-sulphonate (Reactive Blue 69), D&C Blue No. 9, [Phthalocyaninato(2-)] copper and mixtures of these.

Other than in the examples herein, or unless otherwise expressly specified, ail of the numerical ranges, amounts, values and percentages, such as those for amounts of materials, elemental contents, times and températures of reaction, ratios of amounts, and others, in the following portion of the spécification and attached claims may be read as if prefaced by the word “about” even though the term “about” may not expressly appear with the value, amount, or range. Accordingly, unless indicated to the contraiy, the numerical parameters set forth in the following spécification and attached claims are approximations that may vary depending upon the desired properties sought to be obtained by the présent invention. At the very least, and not as an attempt to limit the application of the doctrine of équivalents to the scope of the claims, each numerical parameter should at least be construed in light of the number of reported significant digits and by applying ordinary rounding techniques.

Notwithstanding that the numerical ranges and parameters setting forth the broad scope of the invention are approximations, the numerical values set forth in the spécifie examples are reported as precisely as possible. Any numerical value, however, inherently contains errer necessarily resulting from the standard déviation found in its underlying respective testing measurements. Furthermore, when numerical ranges are set forth herein, these ranges are inclusive of the recited range end points (e.g.,., end points may be used). When percentages by weight are used herein, the numerical values reported are relative to the total weight.

Also, it should be understood that any numerical range recited herein is intended to include ail sub-ranges subsumed therein. For example, a range of “1 to 10” is intended to include ail sub-ranges between (and including) the recited minimum value of 1 and the recited maximum value of 10, that is, having a minimum value equal to or greater than 1 and a maximum value of equal to or less than 10. The terms “one,” “a,” or “an” as used herein are intended to include “at least one” or “one or more,” unless otherwise indicated.

Any patent, publication, or other disclosure material, in whole or in part, that is said to be incorporated by reference herein is incorporated herein only to the extent that the incorporated material does not conflict with existing définitions, statements, or other disclosure material set forth in this disclosure. As such, and to the extent necessary, the disclosure as explicitly set forth herein supersedes any conflicting material incorporated

herein by reference. Any material, or portion thereof, that is said to be incorporated by reference herein, but which conflicts with existing définitions, statements, or other disclosure material set forth herein will only be incorporated to the extent that no conflict arises between that incorporated material and the existing disclosure material.

While this invention has been particularly shown and described with référencés to preferred embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the invention encompassed by the appended claims.

APPENDIX

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Biomass CHP Catalog

5. Biomass Conversion Technologies

In the context of this document, biomass conversion refers to the process of converting biomass into energy that will in turn be used to generate electricity and/or heat The principal categories of biomass conversion technologies for power and heat production are direct-fired and gasificaiion Systems. Within the direct-fîred category, spécifie technologies include stoker boilers, fluidized bed boilers, and cofiring. Within the gasification category, spécifie technologies include fixed bed gasifiers and fluidized bed gasifiera. Anaérobie digesters are also considered a biomass conversion technology; however, extensive information about digesters is readily available from EPA’s AgSTAR Program <www.epa.gov/agstar> and therefore, will not be discussed within this chapter.

Biomass power Systems are typîcally below 50 MW in size, compared to coal-fired plants, which are in the 100- to 1,000-MW range. Most of today’s biomass power plants are direct-fired Systems. The biomass fuel is bumed in a boiler to produce high-pressure steam that is used to power a steam turbinedriven power generator. In many applications, steam is extracted from the turbine at medium pressures and températures and is used for process heat, space heating, or space cooling. Cofiring involves substituting biomass for a portion of the coal in an existing power plant boiler. It is the most économie near-term option for introducing new biomass power génération. Because much of the existing power plant equipment can be used without major modifications, cofiring is far less expensive than building a new biomass power plant Compared to the coal it replaces, biomass reduces SOz, ΝΟχ, CO₂, and other air émissions.

Biomass gasificaiion Systems operate by heating biomass in an environment where the solid biomass breaks down to form a flammable gas. The gas produced—synthesis gas, or syngas—can be cleaned, filtered, and then bumed in a gas turbine in simple or combined-cycle mode, comparable to LFG or biogas produced from an anaérobie digester. In smaller Systems, the syngas can be fired in reciprocating engines, microturbines, Stirling engines, or fiiel cells. Gasification technologies using biomass byproducts are popular in the pulp and paper industry where they improve chemical recoveiy and generate process steam and electricity at higher efficicncies and with lower capital costs than conventional technologies. Pulp and paper industiy byproducts that can be gasifîed include hogged wood, bark, and spent black liquor.

Table 5-1 provides a summaty of biomass conversion technologies for producing heat and power.

Table 5-1. Summary of Biomass CHP Conversion Technologies

Biomass Conversion Technology	Common Fuel Types		Moisture Content	Capaclty Range
Stoker grate, underfire stoker txdilers	Sawdust, bark, chips, hog fuel, shavings, end cuts, sander dust	0.25-2 in.	10-50%	4 to 300 MW (many in the 20 to 50 MW range)
Fluidized bed boiler	Wood residue, peat, wide variety of fuels	< 2 in.	< 60%	Up to 300 MW (many in the 20 to 25 MW range)
Cofiring—pulverized coal boilers	Sawdust, bark, shavings, sander dust	< 0 25 in.	<25%	UptolOOO MW
Cofiring—stoker, fluidized bed boilers	Sawdust, bark, shavings, hoq fuel	<2 in.	10-50%	Upto300 MW
Fixed bed gasifier	Chipped wood or hog fuel, rioe hulls, shells, sewage sludge	0.25—4 in.	<20%	Upto50MW
Fluidized bed gasifier	Most wood and agriculture residues	0.25-2 in.	15-30%	Upto 25 MW

Source: Based on Wright, 2006.

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Modulât Systems employ some of the same technologies mentioned above, but on a smaller scale that is more applicable to faims, institutional buildings, and small industry. A number of modular Systems are now under development and could be most useful in remote areas where biomass is abundant and electricity is scarce.

5.1 Direct-Fired Systems

The most common utilization of solid fuel biomass is direct combustion with the resulting hot flue gases producing steam in a boiler—a technology that goes back to the 19“· ccntury. Boilers today bum a variety of fuels and continue to play a major rôle in industrial process heating, commercial and institutional heating, and electricity génération. Boilers are differentiated by their configuration, size, and the quality ofthe steam or hot water produced. Boiler size is most often measured by the fuel input in MMBtu per hour (MMBtu/hr), but it may also be measured by output in pounds of steam per hour. Because large boilers are often used to generate electricity, it can also be useful to relate boiler size to power output in electric generating applications. Using typical boiler and steam turbine generating efficicncies, 100 MMBtu/lir heat input provides about 10 MW electric output

The two most commonly used types of boilers for biomass fîring are stoker boilers and fluidized bed boilers. Either of these can be fiieled entirely by biomass fuel or cofired with a combination of biomass and coal. The efficiency, availability, operating issues, equipment and installed costs, O&M requirements and costs, and commercial status of each of these options are discussed below.

5.1.1 Boilers

Characterization

Stoker Boilers

Stoker boileis employ direct fire combustion of solid fuels with excess air, producing hot flue gascs, which then produce steam in the heat exchange section of the boiler. The steam is used directly for heating purposes or passed through a steam turbine generator to produce electric power. Stoker-fired boilers were first introduced in the 1920s for coal; in the late 1940s the Detroit Stoker Company installed the first Iraveling grate spreader stoker boiler for wood. Mechanical stokers are the traditional technology that has been used to automatically supply solid fuels to a boiler. Ail stokers are designed to feed fuel onto a grate where it bums with air passing up through it. lhe stoker is located within the fiimace section of the boiler and is designed to remove the ash residue after combustion. Stoker units use mechanical means to shift and add fuel to the fire that bums on and above the grate located near the base of the boiler. Heat is transferred from the fire and combustion gases to water tubes on the walls of the boiler.

Modem mechanical stokers consist of four éléments, 1) a fuel admission system, 2) a stationary or moving grate assembly that supports the buming fuel and provides a pathway for the primaiy combustion air, 3) an overfire air system that supplies additional air to complété combustion and minimize atmospheric émissions, and 4) an ash discharge system. Figure 5-1 illustrâtes the different sections of a stoker boiler.

A successful stoker installation requires selecting the correct size and type of stoker for the fuel being used and for the load conditions and capacity being served. Stoker boilers are typîcally described by their method of adding and distributing fuel. There are two general types of Systems—underfeed and overfeed. Underfeed stokers supply both the fuel and air from under the grate, while overfeed stokers supply fuel from above the grate and air fiom below. Overfeed stokers are further divided into two types—massfeed and spreader. In the mass feed stoker, fuel is continuously fed onto one end of the grate

5. Biomass Conversion Technologies

EPA Combined Heat and Power Partnership surface and travels horizontally across the grate as it bums. The iesidual ash is discharged from the opposite end. Combustion air is inlroduced from below the grate and moves up through the buming bed of fuel. In the spreader stoker, the most common type of stoker boiler, combustion airis again inlroduced primarily from below the grate but the fuel is thrown or spread unifonnly across the grate area. The finer particles of fuel combust in suspension as they fell against the upward moving air. The remaining heavier pièces fail and bum on the grate surface, with any residual ash removed from the discharge end ofthegrate. Chaingrate, traveling grate, and water-cooled vibrating grate stokers are other less common configurations that use various means to maintain an even, thin bed of buming fuel

Biomass CHP Catalog

Figure 5-1. Cut-Away View of a Traveling Grate Stoker Boiler

on the grate. Other specialized stoker Source: ORNL, 2002.

boilets include balanced draft, cyclonefired, fixed bed, shaker hearth, tangential-fired, and wall-fired. Practical considérations limit stoker size and, consequently, the maximum steam génération rates. For coal firing, this maximum is about 350,000 pounds per hour (lb/hr); for wood or other biomass firing it is about 700,000 lb/hr.

Underfeed Stokers

Underfeed stokers supply both fuel and primary combustion air from beneath the grate so that the top of the ftiel pile is not cooled by cold and moist fuel or cold air. The fhel is moved into a hopper and onto the grate by either a screw- or ram-driven mechanism. Underfeed stokers push the fuel into the bottom of the bed of fiiel while heat causes volatilization and complété combustion of the fuel by the time it rises to the top ofthe bed as ash and is discharged. As the fuel moves out over the grate where it is exposed to air and radiant heat, it begins to bum and transfer heat to the water tubes. As with any combustion process, ash accumulâtes as the fuel, is bumed. The two basic types of underfeed stokers are: 1) the horizontal-fèed, side-ash discharge type and 2) the gravity-feed, rear-ash discharge type. A cross-section of an underfeed, side-ash dischaige stoker is shown in Figure 5-2. The demand for underfeed stokers has diminished due to cost and environmental considérations. Underfeed stokers are best suited for relatively dry fuel (under 40 to 45 percent moisture.)

Figure 5-2. Cross Section of Underfeed, Slde-Ash Discharge Stoker

Source: ORNL, 2002.

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Biomass CHP Cataiog

Overfeed Stokers

Overfeed stokers are generally classified by the way the fuel is distributed and bumed within the boiler. The primary désignations are mass-feed or spreader stokers. Mass-feed stokers introduce fuel continuously at one end of a grate. As the fuel moves into the boiler, it falls onto the grate by gravity. To control the amount of fuel that entera the boiler, a gâte can be moved up or down, or the speed at which the fuel move9 beneath the gâte can be adjusted. Inside the boiler, the fuel bums as it travels along the grate. Primary combustion air flows upward from beneath the grate and through the buming bed of fuel, allowing for complété combustion. Any ash that remains on the grate is then dischaiged at the opposite end of the system. The two primary mass-feed stokers are 1) water-cooled vibrating grate and 2) moving (chain and traveling) grate stokers. A cross-section of an overfeed, water-cooled vibrating grate mass-fed stokeris presented in Figure 5-3.

Figure 5-3. Cross Section of Overfeed, Water-Coded, Vibrating-Grate, Mass-Feed Stoker

Source: ORNL, 2002.

Spreader Stokers

Spreader stokers are the most commonly used stokers because of their versatility. They are capable of distributing fuel evenly and to a uniform depth over the entire grate surface by using a device that propels the individual fuel particles inlo the air above the grate. Methods used to propel the fuel particles include air injection and nnderthrow and oveithrow rotors. As tlie fuel is thrown into the boiler, fine particles ignite and bum while suspended in the combustion air. Due to suspension buming, response times of spreader stokeis are better than for mass feed or underfeed stokera. The coarser particles that fait onto the grate end up buming in a thin bed of ftiel on the grate. Primary combustion air is supplied from beneath the grate. Because the fUel is evenly distributed across the active grate area, the combustion air is uniformly distributed under and through the grate. A portion of the total combustion air is admitted through ports above the grate as overfire air, completing the combustion process. Grates for spreader stokers are generally designed to move rather than remain stationary. Therefore, traveling grates, aircooled vibrating grates, and water-cooled vibrating grates are designs that hâve been used effectively. Modem boilers with spreader stokers incorporate:

• Equipment that distributes fuel uniformly over the grate.

• Specially designed air-metering grates.

• Dust collection and reinjectian equipment.

• Forceddraft fans for both undergrate and overfire air.

• Combustion controls to coordinate fuel and air supply with steam demand.⁵⁰ ^M ORNL, 2002.

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Biomass CHP Catalog

Along with the fuel feed System and fumace section geometry, air System design plays an important rôle in efficient and complété combustion of biomass fuels in stoker boileis. ExcesB air for bark, wood, and most biomass fuels is set at 25 percent or above for stoker firing. Because biomass fuels are typically highly volatile on a dry basis, are heterogeneous in size, and more often bum in suspension compared to coal, biomass combustion air Systems are designed to provide more overfire air than those used for coal. Modem designs use undeigrate and overfire quantifies of 40 and 60 percent, respectively.

Fluidized Bed Bollers

Fluidized bed boileis are the most recent type of boiler developed for solid fuel combustion. The primary driving force for development of fluidized bed combustion is reduced SO₂ and NO_X émissions from coal combustion. As the technology developed, it became apparent that the process could efficiently bum biomass and other low-grade fuels that are difficult or impractical to bum with conventional methods.

In this method of combustion, fiielisbumedinabedofhotineit, or incombustible, particles suspended by an upward flow of combustion air that is injected front the bottom of the combustor to keep the bed in a floating or “fluidizetÎ* state. The scrubbing action of the bed material on the fuel enhances the combustion process by stripping away the CO₂ and solids residue (char) that normally forms around the fuel particles. This process allows oxygen to œach the combustible material more readily and increases the rate and efficiency of the combustion process. One advantage of mixing in the fluidized bed is that it allows a more compact design than in conventional water tube boiler designs. Naturel gas or fuel oil can also be used as a stait-up fuel to preheat the fluidized bed or as an auxiliary fuel when additional heat is required. The effective mixing of the bed makes fluidized bed boilers well-suited to bum solid refuse, wood waste, waste coals, and other nonstandard fuels. Figure 5-4 shows the components of a fluidized bed

Figure 5-4. Cut-Away Viewof a Fluidized Bed Combustion Boiler

Tb brO flKterw Uetre* 4 erekhti-β tyilen

Source: Babcock & Wilcox, 2003.

combustion boiler.

The fluidized bed combustion process provides a means for efficiently mixing fuel with air for combustion. When fuel is introduced to the bed, it is quickly heated above its ignition température, ignites, and becomes part of the buming mass. The flow of air and fuel to the dense bed is controlled so that the desired amount of heat is released to the fumace section on a continuous basis. Typically, biomass is bumed with 20 percent or higher excess air. Only a small fraction of the bed is combustible material; the remainder is comprised of inert material, such as sand. This ineit material provides a large inventory of heat in the fumace section, dampening the effect of brief fluctuations in fuel supply or heating value on boiler steam output.

Fuels that contain a high concentration of ash, sulfur, and nitrogen can be bumed efficiently in fluidized bed boilers wliile meeting stringent émission limitations. Due to long résidence time and high intensity of mass transfer. fuel can be efficiently bumed in a fluidized bed combustor at températures

5. Biomass Conversion Technologies

EPA Combined Heat and Power Partnership______________________________Biomass CHP Catalog considerably lower than in conventional combustion processes (1,400 to 1,600° F compared to 2,200° F for a spreader stokcr boiler). The lower températures produce less NO_X, a significant benefit with high nitrogen-content wood and biomass fuels. SOi émissions from wood waste and biomass are generally insignificant, but where sulfiir contamination of the fuel is an issue, limestone can be added to the fluid bed to achieve a high degree of sulfiir capture. Fuels that are typically contaminated with sulfiir include construction débris and some paper mill sludges.

Fluidized bed boilers are categorized as either atmospheric or pressurized units. Atmospheric fluidized bed boilers are further divided into bubbling-bed and circulating-bed units; the fondamental différence between bubbling-bed and circulating-bed boilers is the fluidization velocity (higher for circulating). Circulating fluidized bed boilers separate and capture fuel solids entrained in the highvelocity exhaust gas and retum them to the bed for complété combustion. Atmospheric-pressure bubbling fluidized bed boilers are most commonly used with biomass fuels. The type of fluid bed selected is a function ofthe as-specified heating value of the biomass fuel. Bubbling bed technology is generally selected for fuels with lower heating values. The circulating bed is most suitable for fuels of higher heating values.

In a pressurized fluidized bed boiler, the entire fluidized bed combustor is encased inside a large pressure vessel. Buming solid fuels in a pressurized fluidized bed boiler produces a high-pressure stream of combustion gascs. After the combustion gases pass through a hot gas cleanup system, they are fed into a gas turbine to make electricity, and the heat in the hot exhaust gas stream can be recovered to boil water for a steam turbine. Therefore, a pressurized fluidized bed boiler is more efficient, but also more complicated and expensive. Capital costs of pressurized fluidized bed combustion technology are higher than atmospheric fluidized beds.

Efficiency

Boiler efficiency is defined as the percentage ofthe fuel energy that is converted to steam energy. Major efficiency factors in biomass combustion are moisture content of the fuel, excess air introduced into the boiler, and the percentage of uncombusted or partially combusted fuel. According to the Council of Industrial Boiler Owners (CIBO), the general efficiency range ofstoker and fluidized bed boilers is between 65 and 85 percent efficient.^{* 51} Fuel type and availability hâve a major effect on efficiency because fuels with high heating values and low moisture content can yield efficiencies up to 25 percent higher than fuels having low heating values and high-moisture contents.

Biomass boilers are typically run with a considérable amount of excess air so that they can achieve complété combustion, but this has a négative impact on efficiency. A CIBO rule of thumb indicates that boiler efficiency can be increased 1 percent for each 15 percent réduction in excess air.⁵²

Table 5-2 compares the efficiency of a biomass stoker and a fluidized bed boiler that are operated with 50 percent excess air with a final flue gas exit température of 350° F. The effîciencies are estimated based on the hcat-loss method, which is a way of determining boiler efficiency by measuring the individual heat losses (expressed as a percent of heat input) and subtracting them fiom 100 percent. As can be seen in the table, the largest energy loss in a boiler is the heat that leaves the stack. This loss could amount to as much as 30 to 35 percent of the fuel input in older, poorly maintained boilers. The table shows that decreasing fuel moisture content from 30 to 0 percent increases thermal efficiency by about 6 percentage points. This estimate assumes that the air-fuel ratio is maintained by adjusting air input based on the input moisture content. If the quantity of air is not reduced when wetter fuel enters the boiler then efficiency will drop even more as fuel moisture is increased.

³¹ Council of Industrial Boiler Owners, 1997.

⁵¹ORNL, 2002.

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The primary différence in efficiency between a stoker boiler and a fluidized bed boiler is the amount of fuel that remains unbumcd. As shown in Table 5-2, the efficiency of fluidized bed boilers compares favorably with stoker boilers due to lower combustion losses. Stoker boilers can hâve 30 to 40 percent carbon in the ash and additional volatiles and CO in the flue gases, while fluidized bed boiler Systems typically achieve nearly 100 percent fuel combustion. The turbulence in the combustor combined with the thermal inertia of the bed material provide for complété, controlled, and unifoim combustion. These factors are key to maximizing the thermal efficiency, minimizing char, and controlling émissions.

Table 5-2. Biomass Boiler Efficiency as a Function of Input Fuel and Combustion Characteristics

Characteristics	Biomass Stoker	Biomass Fluidized Bed
		Dry	As Received
Excess air (%)	50	50	50	50
Dry flue gas (Ib/lb fuel)	15.25	10.675	15.25	10.675
Final exhaust temp (°F)	350	350	350	350
High heating value (HHV) ofthe fuel (Btu/lb)	8,500	5,950	8,500	5,950
Moisture content of fuel (%)	0	30	0	30
Hydrogen percent in the fuel (%)	4.59	3.21	4.59	3.21
Efficiency L osses
Dry flue gas losses (%)	11.63	11.63	11.63	11.63
Moisture in fuel (%)	0.00	5.90	0.00	5.90
Latent heat (%)	5.69	5.69	5.69	5.69
Unbumedfuel (%) (1)	3.50	3.50	0.25	0.25
Radiation and miscellaneous (%) (2)	2.03	2.03	2.03	2.03
Total Combustion Losses (%)	22.85	28.74	19.60	25.49
Boiler Efficiency HHV Basis (%)	77.15	71.25	80.40	74.51

(1) Estimated (2) Includes radiation, moisture in air, and other misccilaneous issues.

When considcring factors that influence boilcr performance, it should be noted that efficiency is not constant throughout the entire operating range of a boiler. Peak efficiency generally occurs at a particular boiler output that is determined by design characteristics. Whenever boiler operations deviate from this output, the resulting performance is usually below peak efficiency. Operating continuously at peak efficiency is not practical due to seasonal demanda, load variations and fuel property variations; however, operating at a steady load and avoiding cyclic or on-off operation can improve efficiency.

Operating Availability³

Typically, both stokerand fluidizedboilers are designed for continuous operation, and design performance is in the 90+ percent availability range. Seasonal variability in fuel availability and/or quality can affect the plant availability, but this is a feedstock issue, not an issue of boiler performance. A well ³³ The availability of a power génération system is the percentage of time that the system can operate, or is “available” to operate. Both planned maintenance and unplanned outages hâve a négative effect upon system availability. Therefore an availability of 100% would represent a system that never broke down or needed maintenance (impossible to achieve in real operation).

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OperatingAdvantages andDisadvantages

Stoker and fluidized bed boilers hâve spécifie operating advantages and disadvantages with biomass fuels depending on the fuel characteristics and site requirements. Biomass fuels are extremely variable in terms of heating value, moisture content, and other factors that affect combustion. Wood and most other biomass fuels are composed primarily of cellulose and moisture. As discussed previously, the high proportion of moisture is signifîcant because it acts as a heat sink during the combustion process. The latent heat of évaporation depresses flame température, taking heat energy away from steam production, and contributing to the difficulty of efficiently buming biomass fuels. Cellulose, in addition to containing the chemical energy released in combustion, contains fiiel-bound oxygen. Ibis oxygen decreases the theoretical air requirements for combustion and, accordingly, the amount of nitrogen included in the products of combustion. A few general guidelines for direct firing of wood and biomass in boilers include:

• Maintain stable combustion, which can be achieved in most water-cooled boilers with fuel moisture contents as high as 65 percent by weight, as received.

• Use of preheated combustion air reduces the time required for fuel drying prior to ignition and is essential to spreader stoker combustion Systems. Design air températures will vary directly with moisture content.

• A high proportion of the combustible content of wood and other biomass fuel s bums in the form of volatile compounds. A large proportion of the combustion air requirement, therefore, is added above the fuel in stoker and other conventional combustion boilers as overfire air.

• Solid chars produced in the initial stages of combustion of biomass fuels are of veiy low density. Conservative sélection of fiimace section size is used to reduce gas vclocity and keep char entrainment into the flue gases and possibly out the stack at acceptable levels.

To ensure smooth fuel feeding, biomass fuels hâve to be carefully sized and processed. As discussed above, the moisture content of wood and other biomass waste can vary over a wide range, from 10 percent to more than 60 percent. To ensure steady heat input into the boiler using volumétrie feeders, efficient homogenization of fuel with different moisture contents at the fuel yard is a necessity.

Biomass-based fuels can increase the risk of slagging and fouling of heat transfer surfaces and, in some cases, the risk of fireside corrosion as well. Potassium ash content is relatively high in fresh wood, green particles, and fast-growing biomass, which causes the ash to melt atlow températures and leads to a tendency for fouling and slagging. Additionally, biomass fuels can contain chlorine, which, together with alkalis, can induce aggressive corrosion.

Table 5-3 provides a comparison of combustion characteristics and fuel issues for stoker and fluidized bed boilers. Stoker boilers hâve been around for a long time and are a relatively basic technology, whereas fluidized bed technology is newer and more complex, but offers more flexibility and operating control. Fluidized bed Systems offer signifîcant operating flexibility because they can operate under a wide range of load conditions. The thermal inerlia of the bed material allows it to withstand changes in moisture and heating content of the fuel without négative impacts. Additionally, the low fuel ³⁴ Energy Products ofldaho, a company that provides fluidized bed boilers, has reported operating availabilities of percent for their units, <www.energyproducts.com/fluidized_bed_combustors.htm>.

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Biomass CHP Catalog inventoiy présent in the unit makes it responsive to variable loads. Another advantage is that the fluidized bed can also maintain effîciency during system tum-down. Fluidized bed manufacturera hâve reported that the operating flexibility of their units has allowed their customers to take advantage of utility incentive programs for génération that follows electric demand.⁹⁹

Table 5-3. Comparison of Stoker and Fluidized Bed Boilers

	Boiler Type
Stoker	Fluidized Bed
Combustion Mechanism
Flow of solid fuel	Transported on stoker	Fluidized by combustion air and circulated through the combustion chamber and cyclone
Combustion zone	On the stoker	Entire area ofthe combustionfumace
Mass transfer	Slow	Active vertical movement-mass and heat transfer
Combustion Control
Responsiveness	Slow response	Quick response
Excess air control	Difficult	Possible
Fuel Issues
Appiicability to various fuels	Fair	High
Fuel pretreatment	Generally not necessary	Lumps mus! be crushed
Envlronmental Factors
Low sulfur oxide (SO,) combustion	ln-furnace desulfurization not possible	High rate of in-furnace desulfurization
Low NO, combustion	Difficult	Inherently low NO,
Appropriate facility size	Small	Medium to large

Equipment and Installed Costs

A biomass boiler system is a complex installation with many interrelated subsystems. An integrated steam system will include the fuel prep-yard and handling equipment, the boiler itself induced and forced air fans, controls, and water treatment Systems. Varying levels of émission control equipment will normally be needed as well. Most installations will include cyclone separators to capture large fly ash, a baghouse for fine partîculate matter (PM), and a dry scrubber system. NO, émissions control in stoker boilers is provided by a sélective non-catalytic réduction system using urea or ammonia that is installed in the top of the boiler. Other control equipment includes acid gas removal system, stack, ash handling, and continuous émissions monitoring equipment if required.

Table 5-4 provides total capital cost estimâtes (equipment and installation) for both stoker and circulating fluidized bed steam Systems for three biomass fuel feed rates: 100 tons/day, 600 tons/day and 900 tons/day. Thèse feed rates are comparable to steam Systems producing 20,000; 150,000 to 185,000; and 250,000 to 275,000 lb/hr of steam, respectively, depending on steam température and pressure. Installed costs can vaiy significantly depending on the scope of the equipment included, output steam conditions, geographical area, compétitive market conditions, site requirements, émission control requirements, and prevailing labor rates. Ihe estimâtes presented in the table are budgetaiy estimâtes based on published data and discussions with equipment suppliers and devclopers. The estimâtes arc ⁹⁵ Energy Product of Idaho, n.d.

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Biomass CHP Catalog based on steam conditions that might be typical for a process heating-only application in the small 100 tons/day biomass unit (250 pounds per square inch gauge [psig] saturated steam), and higher steam pressures (750 psig) for a steam turbine CHP configuration in the larger units. The range of expected cost variations can be as high as +/- 35 percent depending on the site and system variables listed above. Steam conditions also hâve a significant impact on boiler cost; higher températures and pressures require thicker tubes and more expensive materials (see Table 5-5).

Table 5-4. Estimated Installed Capital Costs for a Biomass-Fueled Steam Plant

	Biomass Fuel Feed (tons/day)
Characteristics	100	600	900
Biomass heat input (MMBtu/hr)	35.4	297.5	446.3
Steam pressure (psig)	275	750	750
StokerBoiler Integrated Steam Plant
Steam output (Ib/hr)	20,000	165,000	250,000
Stoker boiler equipment cost	$1,195,000	$7,980,000	$10,790,000
Other equipment and installation	$795,000	$10,020,000	$12,460,000
Total Installed Boiler System Cost	$1,990,000	$18,000,000	$23,250,000
Total Installed Biomass Prep-Yard*	$2,640,000	$5,430,000	$7,110,000
Total Installed Steam Plant Cost	$4,630,000	$23,430,000	$30,360,000
Unit Cost ($/lb steam)	$232	$142	$121
Fluidized Bed Integrated Steam Plant
Steam output (Ib/hr)	20,000	175,000	260,000
Fluidized bed boiler equipment cost	$6,175,000	$14,490,000	$19,790,000
Other equipment and installation	$795,000	$10,020,000	$12,460,000
Total Installed Boiler System Cost	$6,970,000	$24,510,000	$32,250,000
Total Installed Biomass Prep-Yard*	$2,640,000	$5,430,000	$7,110,000
Total Installed Steam Plant Cost	$9,610,000	$29,940,000	$39,360,000
Unit Cost ($/lb steam)	$480	$171	$151

*Prep-Yard costs are estimated based on the capital cost curve developed in section 4.1.5

Source: Based on data from Antares Group, Inc., 2003; discussion with equipment suppliers and deveiopers.

As shown in Table 5-4, the prep-yard and fuel handling system represents a significant portion of the total steam system costs, ranging from 15 to 25 percent of the total steam system costs for the larger sized units and 25 to 50 percent of the total cost of the 100 tons/day steam system. Fluidized bed boiler equipment costs are higher than the simpler stoker technology ; the fluidized bed boiler itself is more than three times as expensive as a stoker boiler in the smallest size shown; in the larger sizes, the fluidized bed boiler is 35 to 40 percent more expensive. The unit capital costs ($/lb steam) for a biomass-fuclcd steam plant, including the prep-yard costs, are 20 to 25 percent more expensive for the larger fluidized bed Systems. A portion of the higher capital cost is offset by the higher output due to higher efficiency.

The cost of the boiler is also a function of the steam output conditions as shown in Table 5-5. Generating higher pressure and température steam requîtes spécial and more expensive alloys and thicker water tubes. Boilers producing very high pressure steam can be more than twice as expensive as boilers generating low pressure steam.

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Table 5-5. Effect of Steam Output Conditions on Boiter Capital Costs

Steam Conditions	Boiler Cost Factor
150-250 psig	1.0
600-750 psig	1.15-1.25
1,250-1,500 psig	1.5-2.0

Source: Matches, 2003.

O&M Costs

Estimated non-fuel O&M costs for stoker and fluidized bed boiler Systems are provided in Table 5-6 for the three steam system sizes, based on published data and discussion with manufacturera, lhe O&M costs are evaluated within the context of an integrated plant. Total O&M costs include the labor for the prep-yard, and labor, materials, and parts for the boiler system itself. Boiler system O&M estimâtes were based on an animal non-labor component for spare parts and maintenance equipment assumed to be 2 percent of boiler capital costs. Variable costs for chemicals, water, and electricity needed to run blowers and auxiliary equipment were assumed to be approximately $0.20 to $0.25 per thousand pounds of steam output.

Table 5-6. Annual O&M Costs for a Biomass-Fueled Steam Plant

Biomass Fuel Feed (tons/day)

Characteristics	100		900
Stoker Boiler Intel	jrated Steam Plant
Steam output (Ib/hr)	20,000	165,000	250,000
Prep-yard labor	$400,000	$320,000	$320,000
Boiler section O&M	$160,000	$1,095,000	$1,110,000
Total Annual O&M	$560,000	$1,415,000	$1,430,000
Total Annual O&M ($/1,000 lb Steam)*	$3.55	$1.09	$0.73
Fluidized Bed Integrated Steam Plant
Steam output (Ib/hr)	20,000	175,000	260,000
Prep-yard labor	$400,000	$320,000	$320,000
Boiler section O&M	$260,000	$1,190,000	$1,205,000
Total Annual O&M	$660,000	$1,510,000	$1,525,000
Total Annual O&M, ($/1,000 lb Steam)*	$4.19	$1.09	$0.74

*Based on 90 to 95 percent steam system capacity factor.

Source: Based on data from Antarcs Group, Inc., 2003; discussions with developers.

As shown in Table 5-6, the two boiler types are assumed to hâve the identical prep-yard labor requirement for the same output. The 100 tons/day plant uses a less automated system, so the labor requirement is higher than for the larger plants using an automated prep-yard. On a unit cost basis, O&M costs are higher for the fluidized bed boiler in the 100 tons/day size, but equal to the stoker boiler O&M costs for the two larger sizes.

Commercialization Status

Stoker boilers hâve long been a standard technology for biomass as well as coal, and are offered

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Biomass CHP Catalog by a number of manufacturera. Fluidized bed boilers are a more recent technology, but are also commercially available through a number of manufacturers. Until recently, however, fluidized bed boiler use has been more widespread in Europe than the United States, and many of the suppliera are Europeanbased.

As shown in Table 5-6, when evaluated within the context of an integrated plant on a unit cost basis, O&M costs are higher for a smaller circulating fluidized bed processing 100 tons/day, but lower than the stoker boiler for the two iatger sizes evaluated in this study.

Overall Cost andPerformance Characteristics

A summary of the cost and performance of typical biomass steam Systems is shown in Table 5-7.

Table 5-7. Summary of Biomass Combustion Boiler System Cost and Performance

Biornass Fuel Feed (tons/day)

System	100	eoe	900
Biomass Fuel Charactenstics
Energy content (dry) (Btu/lb)	8,500	8,500	8,500
Moisture content (%)	50	30	30
Energy content (as reeewed) (Btuflb)	4,250	5,950	5,950
Stoker Boiler Integrated steam Plant
Steam output (Ib/hr)	20,000	165,000	250,000
Boiler efficiency (zéro moisture) (%)	77	77	77
Boiter efficiency (moisture adiusted) (%)	63	71	71
Heat input to boiler (MMBtu/hr)	35.4	297.5	446.3
Heat input to steam (MMBtu/hr)	22.5	212.0	318.0
Capacity factor (%)	95	95	95
Cost Factors
Total installed boiler costs	$1,990,000	$18,000,000	$23.250,000
Total installed steam system costs	$4,630,000	$23,430,000	$30,360,000
Unit capital cost ($/lb steam)	$232	$142	$121
Non-fuel O&M cost ($/1,000 Ib steam)	$3.55	$1.09	$0.73
Fluidized Bed Integrated Steam Plant
Steam output (Ib/hr)	20,000	175.000	260,000
Boiler efficiency (zéro moisture) (%)	80	80	80
Boiler efficiency (moisture adjusted) (%)	67	75	75
Heat input to boiler (MMBtu/hr)	35.4	297.5	446.3
Heat input to steam (MMBtu/hr)	23.6	221.7	332.5
Capacity factor (%)	95	95	95
Cost Factors
Total installed boiter costs	$6,970,000	$24,510,000	$32.250,000
Total installed steam system costs	59,610,000	$29,940,000	$39,360.000
Unit capital cost (S/lb steam)	$480	$171	$151
Non-fuel O&M cost ($/1,000 Ib steam)	$4.19	$1.09	$074

Source: NREL, 2003.

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5.1.2 Cofîring

One of themost cost effective and easily implementedbiomass energy technologiesis cofîring with coal in existing coal-fired boilers. Cofîring refersto the practice ofmixing biomass with afossil fiiel in high-efficiency boilers as a supplementary energy source. In biomass cofîring hiomass can substitute forup to 20percent ofthe coal used in the b oiler. Cofîring is typically used when either the supply of biomass is intermittent or when the moisture content of the biomass is high. At large plants, biomass i s cofîred with coal, and more coal is typically used than biomass. At small plants, biomass is cofîred with naturel gas, and more biomass is typically used than natural gas because the natural gas is used to stahilize combustion when biomass with high-moisture content is fed into the b oiler.

Characterization

Figure5-5 shows aprocess diagram for a standard coal-based cofîring plant. Biomass has been cofîred with coal economically in commercial plants, which is prindpally viewed as a fuel costréduction strategy. In certain situations, cofîring has provided opportunities for utilities to get fuel from wood manufacturing and other businesses at zéro or négative cost. Overall production cost sawings can also be achieved by replacing coal with inexpensive biomass fiiel sources such as wood waste and waste paper. Typically, biomass fuel supplies should cost at least 20 percent less, on a thermal basis, than coal supplies before a cofîring proj ect can be economically attractive.

Source: Antues Group, Inc., 2003.

Biomass cofîring is mainly a rétro St application. Abasicprinciple of cofîring is that signifîcant changes to the boiler are not required beyond some minor burnermodifications or additions necessary to introduce and bum the supplémentai fiiel. To meet this objective, cofîring biomass fuelsis usually done on a limited basis, with the amount ofbiomass ranging from 5 to 15 percent ofthe total heatinput to frie boiler.⁵⁰ Biomass fuel s that hâve been successfully cofîred include wood and pelletized waste paper. Interest isgrowing in cofîringbiomass among electricutilities and otherusersof coal boilers, chiefly due to the need to improve air émissions from coal-buming facilities, as well as to diversifÿ fuel supplies.

Table 5-8 gives a sense of the size of typical utility cofîring power plants, the percentage of biomass fuel used (generally about 10 percent butup to 50 percent), and the types ofbiomass feedstock used (wood, wood waste, wood residues, and sawdust).

⁵⁶ Fehrs mdDonoven, 1999.

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Table 5-8. Utility Cofiring Biomass With Coal (Continuous Operation)

Plant Name	Location	Biomass Feedstock	Total Plant (MW)	Biomass (MW)	Boiler Type
6th Street—Alliant Energy	Cedar Rapids, IA	Agricultural and wood waste	85	6.5	Fluidized bed
Bay Front—Northem States	Ashland, Wl	Wood residues	34	5.0	Stoker
Colbert—Tennessee Valley Authority	Tuscumbia, AL	Wood residues	190	3.0	Pulverized coal
Greenridge—AES Corporation	Dresden, NY	Wood residues	108	10.0	Pulverized coal
King—Northern States Power	Bayport, MN	Sawdust	560	10.0	Cyclone
Tacoma Steam Plant #2	Tacoma, WA	Wood	25	12.5	Fluidized bed
Willow Island—Allegheny Energy	Pleasants, WV	Sawdust, tirederived fuel	188	2.3	Cyclone
Yates—Southem Co./Georgia Power	Newnan, GA	Wood residues	150	2.0	Pulverized coal

Source: Antares Group, 2003

Efficiency

Usually, no major changes in boiler efficiency resuit from cofiring. However, some design and operational changes might be needed to maximize boiler efficiency while maintaining acceptable opacity, baghouse performance, and other operating requirements. Without these adjustments, boiler efficiency and performance can decrease. For example, at a biomass heat input level of 10 percent, boiler efficiency losses of 2 percent were measured during cofiring tests at a facility with a pulverized coal boiler when no adjustments were made.” Numerous cofiring projects hâve demonstrated that efficiency and performance losses can be minimized with proper awareness of operational issues.

Operating Availability

The availability of biomass and coal cofired boilers is similar to that of regularcoal boilers, if proper modifications are made to the system. If some of the potential operating issues mentioned in the next section manifest, then availability might be negatively affected.

Operating Advantages andDisadvantages

Typically, cofiring biomass in an existing coal boiler requires modifications or additions to fuel handling, processing, storage, and feed Systems. Slight modifications to existing operational procedures, such as increasing overfire air, might also be necessary, as well as increasing fuel feeder rates to compensate for the lower density and heating value of biomass.

As covered in Chapter 4, fuel characteristics and processing can greatly affect the ability to use biomass as a fuel in boilers. Wood chips are préférable to mulch-like material for cofiring with coal in stoker boilers because the chips are similar to stoker coal in terms of size and flow characteristics. This ¹⁷ Tillman, 2000.

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Another fuel considération when dealing with biomass is the potential for problems with slagging, fouling, and corrosion. Some biomass fuels hâve high alkali (principally potassium) or chlorine content that can lead to unmanageable ash déposition problems on heat exchange and ash-handling surfaces. Chlorine in combustion gases, particulariy at high températures, can cause accelerated corrosion of combustion system and flue gas cleanup components. These problems can be minimized or avoided by screening fuel supplies for materials high in chlorine and alkalis, limiting the biomass contribution to boiler heat input to 15 percent or less, using fuel additives, or increasing soot-blowing. The most troublesome biomass resource tends to be agricultural residues, încluding grasses and straws, which hâve high alkali and chlorine contents. In contrast, most woody materials and waste papers are relatively low in alkali and chlorine and should not présent this problem.

Currently, about 25 percent of the fly ash from coal-fired power plants is used as a feedstock for cernent and concrète production, while another 15 percent is used as a feedstock in other applications?' According to current industry standards?⁹ only fly ash from coal combustion qualifies for use in cement/concrete applications. Cofiring biomass in a coal power plant would keep the fly ash from meeting the ciurent standard. Similarly, coal fly ash will sometimes not meet the current standard when certain émissions control techniques are used, such as ammonia injection. Though these restrictions can impact the économies of biomass cofiring, the value of finding a productive use for fly ash and other coal combustion products is primarily the avoidance of a roughly $20/ton landfill fee. For coal with 10 percent ash content, this value would be worth about $2/ton of the input fuel cost. While the current restrictions are a banier to considering cofiring in some applications, other uses of fly ash are not affected, and researchers are cuirently studying the impact of using fly ash from biomass and biomass/coal cofiring on concrète characteristics. Early results show that biomass and cofîred fuels do not adversely affect the usefiilness of fly ash in cernent and concrète, and in fact might hâve some advantages?⁰ It is likely that this work will eventually lead to a réévaluation of the standard and inclusion of fly ash from cofiring as an acceptable cement/concrete feedstock as has already happened in Europe?¹

Equipment and Installed Costs

Cofiring typically does not involve added investment for the boiler equipment that is already in place for the coal-fired plant. There arc additional costs for new fuel handling and processing equipment, boiler modifications, contrais, engineering fees, and contingency. For blended fuel input Systems, in which the biomass is added upstream of the coal fuel préparation equipment, the costs for the added feed préparation are on the order of 15 to 30 percent of the costs shown in the previous section in Table 5.4 for a dedicated biomass system. For Systems using a separate fuel feed system, the costs are comparable to the costs (S/ton of biomass feed) for a dedicated biomass plant.

“ AmericanCoal Ash Association, n.d.

^WASTMC-618 “Wang, 2007.

“ In 2004, European Standard EN 450 dealing with fly ash spécifications for use in concrète was approved for modification to inc lude fly ash from a wide range of cofired biomass and waste feedstocks. These changes are in the process of being adopted by the European Union member countries.

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O&M Issues

As discussed under capital costs, additional O&M to the boiler section attributable to the addition of biomass for cofiring is minimal. Maintenance requirements for boilers cofiring biomass and coal are similar to those for coal-only boilers. However, slight changes to previous operational procedures, such as increasing overfire air and fuel feeder speeds, might be needed. Increases in O&M costs for biomass cofiring with coal are almost entirely for the biomass receiving and feed préparation. For a blended system, the adjustments to feed préparation O&M are also on the order of 15 to 30 percent of the cost of a dedicated biomass plant.

Commercialisation Status

Organizations such as electric utilities, DOE, and the Electric Power Research Institute (EPRI), hâve conducted research and field tests on biomass cofiring in small- and laige-scale utility boilers for a number of years. These tests hâve shown that cofiring with biomass has been successfully accomplished in a wide range of boiler types, including cyclone, stoker, pulverizcd coal, and bubbling and circulating fluidized bed boilers. According to the Fédéral Energy Management Program, at least 182 separate boilers and organizations in the United States hâve cofired biomass with fossil fuels although this number is not comprehensive. Of the 182 cofiring operations, 114 (or 63 percent) hâve been at industrial facilities, 32 at utility-owned power plants, 18 at municipal boilers, 10 at educational institutions, and eight at fédéral facilities”.

5.2 Gasification Technologies

Biomass gasification for power production involvcs heating solid biomass in an oxygen-starved environment to produce a low or medium calorific gas. Depending on the carbon and hydrogen content of the biomass and the gasifier’s properties, the heating value of the syngas, can range anywhere from 100 to 500 Btu/cubic foot (10 to 50 percent that of natural gas). The heating value of syngas generally cornes from CO and hydrogen produced by the gasification process. The remaining constituents are primarily CO₂ and other incombustible gases. Biomass gasification offers certain advantages over directly buming the biomass because the gas can be cleaned and filtered to remove problem chemical compounds before it is bumed. Gasification can also be accomplished using chemicals or biologie action (e.g., anaérobie digestion); however, thermal gasification is currently the only commercial or near commercial option.

The fuel output from the gasification process is generally called syngas, though in common usage it might be called woodgas, producer gas, or biogas. Syngas can be produced through direct heating in an oxygen-starved environment, partial oxidation, or indirect heating in the absence of oxygen. Most gasification processes include several steps. The primary conversion process, called pyrolysis, is the thermal décomposition of solid biomass (in an oxygen-statved environment) to produce gases, liquids (tar), and char. Pyrolysis releases the volatile components of the biomass feed at around 1,100° F through a sériés of complex reactions. Biomass fuels are an idéal choice for pyrolysis because they hâve so many volatile components (70 to 85 percent on dry basis, compared to 30 percent for coal). The next step involves a further gasification process that converts the leftover tare and char into CO using steam and/or partial combustion. In coal gasification, pure oxygen or oxygen-enriched air is preferred as the oxidant because the resulting syngas produced has a higher heating value, and the process is more efficient. In biomass gasification, oxygen is generally not used because biomass ash has a lower melting point than coal ash, and because the scale of the plants is generally smaller.

DOE, 2004.

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Very high température processes involving passing the biomass through a plasma arc hâve been devcloped and tested primarily for waste remediation, contaminated wastes, and MS W. Plasma processes are not discussed in this report.

Compared with direct-fired biomass Systems, gasifîcation is not yet an established commercial technology. There is great interest, however, in the development and démonstration of biomass gasifîcation for a number of reasons:

A gascous fuel is more versatile than a solid fuel. It can be used in boilers, process heaters, turbines, engines and fuel cells, distributed in pipelines, and blended with natural gas or other gaseous fuels.

Gasifîcation can remove fuel contaminants and reduce émissions compared to direct-fired Systems.

Gasifîcation can be designed to handle a wide range of biomass feedstocks, from woody residues to agricultural residues to dedicated crops, without major changes in the basic process.

Gasifîcation can be used to process waste fuels, providing safe removal of biohazards and entrainment of heavy metals in non-reactive slag.

A gaseous fuel can be used in a high-efficiency power génération system, such as a gas turbinecombined cycle or fuel cells, provided it is cleaned of contaminants. When equipment is added to recover the heat from the turbine exhaust, system efficiencies can increase to 80 percent.

Like the direct combustion processes described in the previous section, two principal types of gasifiers hâve emerged: fixed bed and fluidized bed. Fixed bed gasifîers are typically simpler, less expensive, and produce a lower heat content syngas. Fluidized bed gasifiers are more complicated, more expensive, and produce a syngas with a higher heating value.

5.2.1 Gasifiers

Characterization

Fixed Bed Gasifiers

Fixed bed gasifiers typically hâve a fixed grate inside a refractory-lined shaft. The fresh biomass fuel is typically placed on top of the pile of fuel, char, and ash inside the gasifier. A further distinction is based on the direction of air (or oxygen) flow: downdraft (air flows down through the bed and leaves as biogas under the grate), updraft (air flows up through the grate and biogas is collected above the bed), or crossflow (air flows across the bed, exiting as biogas). Schematics of the primary section of the fixed bed gasifier types are shown in Figure 5-6.

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Figure 5-6. Fixed Bed Gasiffcr Types

Êiorrws*

Tar.Ww :

C*3x“C0â

C+CQ^xJCO r+waû *GQ*HS ! Gm. T«r. ww«r

K k	·' l ' /;....-Ppay-fe kl	C*CO?k2CO
1	f\|		R««ÎQPtKM1
	RriWieo'O™ Air		ÇftœcuSion
h

Source: Bain. 2006.

Table 5-9 compares fixed bed gasifier types. Table 5-10 provides typical physical characteristics of a fixed bed gasifier. Fixed bed gasifiers are usually limited in eapadiy, typîcally used for génération Systems that are able to produce Jess ihan 5 MW. Tlie physics ofthe rcfractory-iined shaftreactor vessel limiis the diameter and thus lhe tiiroughput Dcvelopa-s hâve identified a good match between fixed bed gasifiers and small-scale distribnted power génération equipment. llowevcr, tlie variable économies of biomass collection and fêeding, coupled with the gaxifier's low eificiencw make die économie viahility of tlie tecluiology pavticularly site-specific.

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Table 5-9. Comparison of Fixed Bed Gasifîcation Technologies

	Type of Gasifier
Downdraft	lipdraft	Crossflow
Operation	Biomass is introduced from the top and moves downward. Oxidizer (air) is introduced at the top and flows downward. Syngas is extracted at the bottom at grate level.	Biomass is introduced from the top and moves downward. Oxidizer is introduced at the bottom and flows upward. Some drying occurs. Syngas is extracted atthe top.	Biomass is introduced from the top and moves downward. Oxidizer is introduced at the bottom and flows across the bed. Syngas is extracted opposite the air nozzle at the qrate.
Advantages	Tare and particulate in the syngas are lower, allowing direct use in some engines without cleanup. The grate is not exposed to high températures.	Can handle higher-moisture biomass. Higher températures can destroy some toxins and slag minerais and métal. Higher tar content adds to heating value.	Simplest of designs Stronger circulation in the hot zone. Lower températures allow the use of less expensive construction materials.
Dlsadvantages	Biomass must be vety dry (<20 percent moisture content). The syngas fs hot and must be cooled if compression or extensive cleanup is required. About 4 to 7 percent of the carbon is unconverted and remains In the ash.	Higher tar content can foui engines or compressore. The grate is exposed to high températures and must be cooled or otherwise protected.	More complicated to operate. Reported issues with slagging. High levels of carbon (33%) in the ash.

Table 5-10. Typical Characteristics of a Fixed Bed Gasifier

Parameter	Fixed Bed, Downdraft
Fuel size (inches)	0.4-4
Fuel ash content (% weight)	<6
Operating température (°F)	1450-2550
Control	Simple
Turn-down ratio	4:1
Construction material	Mild steel + refractory
Capacity (MW_lh.„.i) (tons biomass/day)	<5 («30)
Start-up time	Minutes
Operator attention	Low
Tar content (Ib/M MBtu product gas)	<1.2
Heating value (Btu/scf) HHV	130

Source: GasNet, n.d.

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Fluidized Bed Gasifiers

Fluidized bed gasifiers utilize the same gasification processes and offer higher performance than fîxed bed Systems, but with greater complexity and cost. Similar to fluidized bed boilers, the primary gasification process takes place in a bed of hot inert materials suspended by an upward motion of oxygendeprived gas (Figure 5-7). As the amount of gas is augmented to aehieve greater throughput, the bed will begin to levitate and become “fluidized.” Sand or alumina is often used to further improve the heat transfer. Notable benefits of fluidized bed devices are their high productivity (per area of bed) and flexibility. Fluidized bed gasifiers can also handle a wider range of biomass feedstocks with moisture contents up to 30 percent on average.

Figure 5-7. Fluidized Bed Gasifier

Source: Bain, 2006.

There are three stages of fluidization that can occur on the gasifier depending on the design: bubbling, recireulating, and entrained flow. At the lower end of fluidization, the bed expands and begins to act as a fluid. As the velocity is increased, the bed will begin to “bubble.” With a further increase in airflow, the bed material begins to lift off the bed. This material is typically separated in a cyclone and “recirculated” to the bed. With still higher velocities, the bed material is entrained (i.e., picked up and carried off in the airflow).

Fluidized bed gasifiers can be designed to use a portion of the pyrolysis gases to generate the heat to drive the process, or they can be extemally fired. Operating the gasifier at higher pressures increases the throughput; however, this also increases the gasifier's complexity and cost. In these units, the biomass is fully converted after going through the pyrolysis and char conversion processes.

By reducing the quantity of air and process température, it is possible to operate fluidized bed boilers as gasifiers. In this operating mode, the gasifiers produce a gas with a heating value of slightly more than 100 Btu/cubic foot (ft³). This gas is bumed above the bed as additional air supply is injected upstream of the boiler tube section.

Table 5-11 provides typical physical characteristics of a fluidized bed gasifier. A number of advanced-concept fluidized bed gasifiers aiming to produce a syngas with a heating value between 250 and 400 Btu/ft³ are under development. This type of syngas would be more appropriate for use in gas

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Biomass CHP Catalog turbines, fuel cells, and reciprocating internai combustion engines; however, these advanced concept gasifiers hâve not reached the point where they are proven in commercial operation.

Table 5-11. Typical Characteristics of a Fluidized Bed Gasifîer

Parameter	Fluidized Bed
Fuel size (inches)	0-0.8
Fuel ash content (% weight)	<25
Operating température (°F)	1,350-1,750
Control	Average
Turn-down ratio	3
Construction material	Heat-resistant steel
Capacity (W™.) (biomass tons/day)	5 and up (> 30)
Start-up time	Hours
Operator attention	Average
Tarcontent (Ib/MMBtu productgas)	<2
Heating value (Btu/scf) HHV	150

Source: GasNet, n.d.

Effîciency

Both fixed and fluidized bed biomass gasification uses similar types of equipment as direct combustion. The biomass fuel is fed into a combustion/reaction vessel with either a fixed, fluidized, or moving bed. The thermodynamics of heat Ioss arc similar, but gasification conditions are different from direct combustion. In direct combustion, 10 to 14 times the weight of the fuel is introduced as air. In gasification, the air entering the reactor, if any, is only one to two times the weight of the fuel. This différence reduccs heat losses from the reaction zone. On the other hand, the syngas exits the gasification reactor at very high températures (1,200 to 1,500° F); some of this heat Ioss can be recovered either directly through the use of heat exchangers in the gas cooling section, or indirectly through the use of heat recovery from the combustion of the syngas in the power génération section. To the extent that heat is used to preheat incoming air, introduce high-temperature steam, or diy the incoming biomass, the effîciency of biomass to syngas converaion will be increased. Heat that is recovered from the hot gas cooling section can also be added to the CHP heat recovery. In this case, the intermediate effîciency value of syngas conversion is not increased but the overall CHP effîciency is. These différences combine to produce biomass to syngas effîciencies (heating value of the syngas divided by the heating value of the biomass) of 60 to 80 percent. In integrated configurations, however, additional steam can be generated from cooling the hot syngas exiting the reactor prior to cleanup.

Operating Availability

Due to the faetthat commercialization of biomass gasification plants is in its early stages, no facility survey information was found on their availability or reliability. Plants are designed for continuous operation, and design performance is in the 90+ percent range. Actual expérience with emerging technology tends to resuit in lower availability than is experienced during broad commercial use, as materials handling problème, control issues, and component failures cause more frequent unplanned outages than arc seen after accumulating additional operating expérience. With a newly established support infrastructure, outages also tend to last longer before being fixed or solved. A well

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Biomass CHP Cataiog designed system, however, has a reasonable expectation of operating in the 85 to 95 percent availability range.

Operating Issues

As discussed above, moisture content, gas cleanup, and operating pressure can ail affect operation of a gasifier. There are a number of operating issues common to the different types of gasification Systems.

Moisture Content

Green biomass, defîned as freshly harvested plant material, can contaîn a significant amount of water by weight (up to 60 percent). This water does not contribute to the heat content of the syngas while consuming a significant amount of energy in gasification. Even though water cannot be bumed (oxidized) at elevated températures, it will dissociate into its elemental components—hydrogen and oxygen. The hydrogen will contribute to the calorific value of the syngas. This reaction is very temperature-sensitive, and the hydrogen and oxygen will usually recombine into water vapor as the syngas cools. Therefore, the moisture content of biomass must be strictly limited. If there is excess moisture, the gasification process cannot sustain itself without an extemal source of heat. As the moisture content of the biomass increases, the net energy available in the syngas decreases. Fixed bed gasifiers that use internai combustion of the syngas typically utilize biomass with less than 20 percent moisture content. Fluidized bed gasifiers typically require less than 30 percent moisture content.

Green biomass is the most readily available and inexpensive biomass product. The drying process requîtes a considérable additional capital investment and increases the O&M costs. Unfortunately, the cost of the drying equipment (equipment cost and O&M cost) seldom covers the cost savings of using green biomass.

Gas Cleanup

As syngas leaves the gasifier, it contains several types of contaminants that are harmful to downstream equipment, ash handling, and émissions. The degree of gas cleanup must be appropriately matched to its intended use. For use in reciprocating engines, gas turbines, and especially fuel cells, a very clean gas is required. As discussed in Table 5-12, the primary contaminants in syngas are tars, particles, alkali compounds, and ammonia. The types of contaminants that are observed dépend on the biomass feedstock and the gasification process used.

Table 5-12. Gas Cleanup Issues

Contaminant	Description	Treatment
Tar	Tars (créosote) are complex hydrocarbons that persist as condensable vapors.	Wet scrubbers, eleetrostatic precipitators, barrier filters. catalysts, or combustion.
Particles	Particles are very small, solid materials that typically include ash and unconverted biomass.	Cyclone separators, fabric filters, eleetrostatic precipitators, and wet scrubbers.
Alkali compounds	Potassium, alkali salts, and condensed alkali vapors are part of the chemical composition of biomass.	First, cool syngas below 1,200* F, causing the alkali vapors to condense. Second, use cyclone separators, fine fabric filters, eleetrostatic precipitators, and wet scrubbers.
Ammonia	Ammonia is formed from nitrogen (fuel-bound and In air) and hydrogen (in fuel and in moisture content). When syngas is burned, ammonia is converted to NO_X.	Catalysts, hydrocarbon reforming, or wet scrubbing.

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Because gasification occurs at an elevated température, syngas can hâve as much as a third of its total energy in sensible heat. Cleaning the gas while it is hot would be advantageous from an energy use perspective, but this task is currently diffrcult to accomplish. Rescarch is ongoing regarding hot gas filters, which can be applied in coal gasification, as well as other high-temperature processes. Wet scrubbers are currently one of the most reliable and least expensive options for gas cleanup, even though they sacrifice a large portion of the sensible heat of the syngas. Cooling the hot syngas can provide a source of steam for the cleaning process, power génération, or end-usc.

Operating Pressure

Gasifiers can be operated at either atmospheric or elevated pressures. Air-blown, atmospheric gasifiers produce a very low Btu gas 110 to 170 Btu/scf. To introduce this gas into a gas turbine in the power génération section of the plant requires considérable compression energy, up to a third of the turbine’s output. Therefore, it would be advantageous to produce the syngas at a high pressure so that it can be introduced directly into the combustion section of a gas turbine without additional compression. Pressurized reactors, however, do need to compress any combustion air or oxygen that is introduced into the reactor and maintain a pressure seal on the biomass input and ash removal Systems.

Advantages and Disadvantages

Fixed bed and fluidized bed gasifiers have spécifie operating advantages and disadvantages with biomass fuels depending on the biomass characteristics and site requirements. Table 5-13 provides a qualitative comparison of gasifier characteristics and operating issues for fixed bed and fluidized bed Systems.

Table 5-13. Relative AdvantagesZDisadvantagesof Gasifier Types

Gasifier		Disadvantages
Updraft fixed bed	Mature for heat Small-scale applications Can handle high moisture No carbon in ash	Feed size limits High tar yields Scale limitations Low Btu gas Slagging potential
Downdraft fixed bed	Small-scale applications Low particulates Low tar	Feed size limits Scale limitations Low Btu gas Moisture-sensitive
Bubbting fluid bed	Large-scale applications Feed characteristics Direct/indirect heating Can produce higher Btu gas	Medium tar yield Higher particle loading
Circulating fluid bed	Large-scale applications Feed characteristics Can produce higher Btu gas	Medium tar yield Higher particle loading
Entrained flow fluid bed	Can be sealed Potential for low tar Potential for low methane Can produce higher Btu gas	Large amount of carrier gas Higher particle loading Particle size limits

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Equipment andInstalled Costs

The main cost for the gasification train is the primaty gasification reactor itself. Supplementary processing can occur in a tar cracker. Indirect gasifiers hâve separate char combustors to supply heat. The next major part is the gas clcanup section, which includes ash removal, quench, bag filter, wet senibber, and heat exchangers to cool the syngas and provide heat to other parts of the process or to contribute to the CHP heat utilization. Capital costs for the gasification section and for a biomass-to-syngas plant are shown in Table 5-14. These costs are estimated based on published estimâtes (Antares Group, Inc., 2003) and discussions with equipment suppliera. The unit costs do not show a uniform dcclining trend as a lunction of size, but instead vary depending on the process considered.

Table 5-14. Biomass Gasification Capital Costs to Produce Syngas

	Gasifier Cases
Atmospheric^:Gasification	Atmospheric Gasification	Atmospheric < Gasification	High-Pressure Gasifier
Gasifier type	Fixed	Fluidized	Fluidized	Fluidized/ high-pressure
Tons/day (as received)	100	260	450	1,200
Gasifier equipment	$1,225,000	$10,050,000	$15,158,000	$34,682,000
Installation	$612,000	$5,024,000	$7,578,000	$17,338,000
Total Installed Gasification	$1.837,000	$15,074,000	$22,736,000	$52,020,000
Biomass Prep Yard*	$2,639,700	$3,947,400	$4,972,000	$9,685,766
Total Installed Capital Cost	$4,476,700	$19,021,400	$27,708,000	$61,705,766
Unit Cost ($/MMBtu/hr) (syngas)	$127,164	$209,425	$174,130	$161,270

*Prcp-Yard costs arc estimated based on the capital cost curve developed m section 4.1.5

Source: Based on data from Antares Group, Inc., 2003; discussion with equipment suppliers and developers.

O&M Costs

Non-fuel O&M costs for gasification include O&M labor, supervisory labor, water, ash removal, insurance, taxes, royalties, and other operating materials. These costs are estimated in Table 5-15 based on published estimâtes and discussions with equipment suppliées/³ ⁶³ Antares Group Inc., 2003

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Table 5-15. Gasification O&M Cost Estimâtes for Syngas Production

	Gasifier Cases
Atmospheric Gasification	Atmospheric: Gasification	Atmospheric Gasification	High-Pressure Gasifier
Gasifier type	Fixed	Fluidized	Fluidized	Fluidized/ high-pressiire
Tons/day (as received)	100	260	450	1,200
Net capacity, MMBtu/hr	35.2	90.8	159.1	382.6
Prep-yard labor costs	$400,000	$320,000	$320,000	$400,000
Gasifier section O&M	$502,000	$634,500	$789,500	$2,235,800
Total Annual O&M (to svnqas)	$902,000	$954,500	$1,109,500	$2,635,800
Gasification O&M ($/MMBtu)	$3.250	$1.333	$0.884	$0.874

A summary ofthe cost and performance for the range of biomass gasification Systems considered is provided in Table 5-16.

Table 5-16. Biomass Gasification Cost and Performance

	Gasification Technologies
Atmospheric Gasification	Atmospheric Gasification	Atmospheric Gasification	HighPressure Gasifier
Gasifier type	Fixed	Fluidized	Fluidized	Fluidized/ high-pressure
Tons/day (as received)	100	260	450	1,200
Feedstock Characteristics
Energy content dry (Btu/lb)	8,500	8,500	8,500	8,476
Moisture content (%)	30	30	30	38
Energy content as received (Btu/lb)	5,950	5,950	5,950	5,255
Biomass Conversion
Gasifier efficiency (moisture adjusted)(%)	65	71	71	72
Biomass fuel value to gasifier (MMBtu/hr)	49.6	127.9	224.1	531.9
Fuel produced (MMBtu/hr)	32.2	90.8	159.1	382.6
Heating value (Btu/scf HHV)	110.0	110.0	110.0	128.8
Fuel pressure (psig)	Atmospheric	Atmospheric	Atmospheric	Pressurized
Plant capacity factor (%)	90	90	90	90
Capital Costs
Gasifier equipment	$1,225,000	$10,050,000	$15,158,000	$34,682,000
Installation	$612,000	$5,024,000	$7,578,000	$17,338,000
Total Installed Gasification Section	$1,837,000	$15,074,000	$22,736,000	$62,020,000
Biomass Prep-Yard	$2,639,700	$3,947,400	$4,972,000	$9,685,766
Total Installed Capital Cost	$4,476,700	$19,021,400	$27,708,000	$61,705,766
Unit Cost ($/MMBtu/hr) (syngas)	$127,164	$209,425	$174,130	$161,270

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Commercial Status

The majority of commercial gasification projects use coal or petroleum coke as a feedstock. Biomass gasification technologies havc bccn a subject of commercial interest for several décades. By the 1990s, CHP had been identified as a potential near-term technology. Research and development concentrated on integrated gasification combined cycle and gasification cofiring démonstrations, which led to a number of commercial-scale Systems. In the United States, projects mostly processed hard-tomanage feedstocks like bagasse and alfalfa. Low-cncrgy gasifiers are now commercially available, and dozens of small-scalc facilitics are in operation.

A review of gasifîcr manufacturera in Europe, the United States, and Canada⁶⁴ identified 50 manufacturera offering commercial gasification plants in which 75 percent of the designs were fixed bed downdraft type; 20 percent of the designs were fluidized bed Systems. The actual number of biomass gasification Systems in operation worldwide is unknown, but is estimated to be below 50 based on literature review and discussions with industry sources. There are only a handful of commercially operating biomass gasification Systems in the United States at this time, and many of these are partially govemment-funded démonstration units. In comparison, there are currently more than 100 biomass-fueled fluidized bed boilers in operation around the world.

There is still a considérable amount of development activity underway to address existing technical and operational issues:

• Gasification—Some gasification technologies using biomass and black liquor hâve developed to the point oflarge-scale démonstration. However, gasifier Systems hâve not rcached widespread commercial availability for système suitable for intégration with hydrogen séparation technologies for fuel cells or fiiel synthesis. This is due in part to areas of fuel chemistry that are not established cnough to support the commercial démonstration programs and facilitate the development and scale-up of advanced gasifiers and gas cleanup système.

• Syngas cleanup and conditioning—The raw gases from biomass Systems do not currently meet strict quality standards for downstream fiiel, chemical synthesis catalysts, or those for some power technologies. These gases will require deaning and conditioning to remove contaminants such as tar, particulates, alkali, ammonia, chlorine, and sulfiir. Available cleanup technologies do not yet meet the needed cost, performance, or environmental criteria needed to achieve commercial implémentation.

• Sensors and centrais—Development of effective process contrôle is needed to maintain plant performance and émissions at target levels with varying load, fuel properties, and atmospheric conditions. New sensors and analytical instruments are under development to optimize control Systems for thermochemical Systems.

• Process intégration—As with ail new process technologies, demonstrating sustained integrated performance that meets technical, environmental, and safety requirements at sufficiently large scale is essential to supporting commcrcialization. Applications such as black liquor intégration in paper mills has the added complexity of being attached to an existing commercial process where the unit operations associated with steam production, power, pulping, and chemical recovery must ail be integrated.

⁶⁴ Européen Biomass Industry Association, n.d.

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Biomass CHP Catalog • Containment (materials οΓ construction)—Expérience with existing gasifiers indicates that gasification reactions are difficult to contain and that materials development for reactor shells and internais, rcfractory materials to line containment vessels, vessel design, and increased knowledge of bed behavior and agglomération will improve performance over the long term.

5.3 Modular Systems

Modular biomass-fueled CHP Systems are defined as small Systems, less than 5 MW, though typically smaller, with the main operating components coming in one or more pre-engineered and packaged modules for simple installation at the user’s site. The Systems typically include a fuel processor (combustion or gasification), neccssary intermediate fuel cleanup, an electric generator, and heat recovery from both the power génération and energy conversion sections. An automatic fuel storage and delivery system must be added for a complété operating System.

Small modular biomass Systems can supply electricity to rural areas, farms, businesses, and remote villages. These Systems use locally available biomass fuels such as wood, crop waste, animal mamirc, and LFG. Development of biomass-fueled modular power Systems is ofgrcat interest intemationally as a means to bring power to isolated communities in areas lacking power and fuel infrastructure. In the United States, there is interest in small Systems to utilize opportunity fuels from a local area, such as crop wastes or fire control forest thinnings.

A partial listing of spécifie developer/manufacturer modular Systems is provided in Appendix D.

Charade rization

Modular Systems are essentially scaled down versions of larger Systems. There are Systems that use direct-fired technology with steam power, and Systems that use gasification technology and gaseous fuel buming power technologies (discussed in Chapter 6) such as internai combustion engines, microturbines, and Stirling engines. There are also direct fired Systems that use Stirling engines for power production, as well as Systems that employ gasification, wherein the hot raw gas is combusted to raise steam.

Modular Gasification Systems

Figure 5-8 shows a schematic of a 75-kW modular biomass gasification system that is représentative of Systems under development. The figure shows that there are eight submodules included in the basic system and that the storage and feed submodules are not included.

Basic Package Modules

1. Automatic biomass feed system.

2. Dryer to reduce the feedstock moisture content.

3. Chip sorter for sizing.

4. Heat exchanger that extracts heat from the gasifier for use in the dryer and for onsite thermal applications.

5. Gasifier feeder.

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6. A downdraft gasifier producing low Btu gas (heating value of about 110 Btu/sof—HHV).

7. Filtering stages th at remove particulates.

8. The power module—this can be an internai combustion engine designed to run on low Btu fuel, a microturbine, a Stirling engine, or even a fiiel cell. The power module also has heat recovery equipment to provide additional useable thermal energy for onsite use. Because the gas is of such a low Btu content, propane or naturel gas is required on system start-up. After start-up, the system can nui on the syngas alone.

Systems such as these will require feedstock storage with an in-place delivery system. An inground storage bunker with amoving bed would allow direct delivery offuel loads into the automated system. This can consist of a permanently installed live bottom van into which dump trucks can deliver a sized fuel supply.

Figure 5-8. Example Modular Biomass Gasiflcation System

Source: Community Power Corporation, n.d.

Modular Combustion Systems^

Direct combustion in fixed bed combustors is a commercial technology in larger sizes. In these larger Systems, as characterized prevîously, power is generated by steam tuibines. In modular Systems, other power Systems are being developed that are more suitable for small-sized applications. The typical power and heat cycles being employed or explored for use are as follows:

• Steam cycle • Organic Rankine cycle (ORC) ⁶⁵ Example shown, BioMax, is developed by Community Power Corporation.

5. Bomass Conversion Technologies

EPA Combined Heat and Power Partnership

Biomass CHP Catabg • Brayton cycle, hot ait turbine • Entropie cycle, as defined by its developer, similar to Organic Rankine cycle but with a higher température differential producing higher effidencies • Stirling Engine, extemal combustion

Modular power and heat cycles that can be drivai by biomass combustion are shown in Figure 5-9.

Figure 5-9. Heat Engine Power Cycles for Modular Biomass Combustion Systems⁰⁰

Source: Smith, 2006.

In addition to the four power cycles shown, very small (500 watts to 10 kW) modular Systems are being developed using Stirling engine technology. The generators will convert various biomass fuels (wood, wood pellets, sawdust, chips, or biomass waste) to electricity and useful heat” These Systems typically convert 10 to 20 percent of the fuel eneigy to electricity; 60 to 70 percent of fuel energy is then available for heating water and spaces. The bumer for the prototype system includes a ceramic fire box and a fuel hopper with a fuel capacity of 24 hours. It accomplishes complété two-stage combustion with comparatively low émissions. The Stirling engjne-altemator requires miniinal maintenance because its gas bearings eliminate contact, friction, and wear. Its projected life is 40,000 hours.

Modular Hybrid Gasification/Combustion Systems

The modular hybrid gasification/combustion system opérâtes functionally like a direct combustion system. Power is derivedby aback-pressure steam turbine that alsoprovides steam for onsite thermal energy requirements. The différence is that the combustion chamber is actually a gasifîcation “ Smith. 2006.

° A system under development by Sunpower Stirling engine technology licensee is Extemal Power LLC of Indianapolis.

5. Biomass Conversion Technologies

EPA Combined Heat and Poher Partnership

Biomass CHP Catalog system that uses a two-chamber gasifier approach. lhe systemis similar to atwo-stage combustion boiler design. This approach allows the production of gas in a relatively cool chamber at températures from 1,OOO°F to l,400°F, and then combustion in a relatively hot chamber—the boiler—at températures up to 2,300“F. These températures allow the complété removal of catbon from the fuel in the gasifier, and more complété oxidation of complex organics in the oxi dation zone. The combination of thés e features results in a clean-buming, fuel-efficient system. CHP units include small back-pressure steam turbines from 100 kW up to several mégawatts.

This approach combines the simplicity and low cost of a combustion system with the gasification advantages of more complété carbon conversion and cleaner combustion characteristics. An example of a modular gasification/combustion system is shown in Figure 5-10. This system has the capability to use fuels withmoisture contents ranging from6 to 55 percent (wet basis). The system also has a 20:1 turndownratio to allow it to idle during periods oflowheat demand.

Figure 5-10. Example of Modular GasUIcatton/Combustlon Process

Source: Chiptec* Wood Energy Systems, nd.⁶³

Efficiency

Modular system electric génération efficiencies are typically fairiy low as shown in Table 5-17.

In applications requiring considérable thermal energy, the overall CHP efficiencies are comparable to gas fired Systems. However, the electric to thermal ratio for these Systems is much lower, so more of the total usetul energy is deliveredintbe form ofheat rather than in the formofhighervalue electricity.

⁶⁸ Examp le shown is a p atented process by Chiptec® Wood Energy Systems, Burlington, Vermont

S. Biomass Conversion Technologies

EPA Combined Heat and Power Partnership

Biomass CHP Catalog

Table 5-17. Efficiencies of Modular Biomass Systems, Based on Conversion of Switchgrass at 20 Percent Moisture

System Type	Electric Efficiency	Thermal Energy Delivered	Overall CHP Efficiency
Small steam	6%	59%	65%
Air Brayton	8%	41%	49%
Organic Rankine	11%	56%	67%
Entropie	13%	63%	76%
Stirling	13%	64%	77%
Modular gasifier	16-22%	29-53%	55-75%
Hybrid gasifier/combustor	<15%	45-55%	60-70%

Operating Advantages andDisadvantages

The main operating advantages today are in the use of opportunity biomass fuels of low value such as wood chips or forest thinnings. In addition, many of the Systems are targeted at remote applications where it would be too costly to connect to grid electricity.

The main disadvantage affecting ail types of modular Systems is the comparatively high capital costs associated with ail of the required equipment. This equipment also takes up considérable space compared to conventional gas-fired CHP Systems. The engine generator Systems occupy only about 5 percent of the total space required for the modular biomass System. Another disadvantage is the need for maintenance and repairs associated with the many subsystems, particularly the solids handling components and filters.

Equipment and Installed Cost

Equipment costs are spéculative. Information in this section is as provided by the vendors and secondary sources. Figure 5-11 shows a range of costs (S/kW) for different types of direct-fired Systems. It is not clear that these costs include the costs of feedstock storage and delivery, which would add another $600 to 1,000/kW to the overall costs.

5. Biomass Conversion Technologies

EPA Combined Heat and Power Partnership

Biomass CHP Cataiog

Figure 5-11. Size and Cost Ranges for Direct-Fired Modular Systems⁴⁹

COST

Size Range (kWe)

Small-scale Steam

W«a w WM a* ««Mfiaa μμιμμμμιιν

Organic Rankine Cycle ma»

Entropie Cycle

Air Turbine

Cost Range ($/kWe

Source: Srnith, 2006.

Modular gasifîcation costs are estimated to be between $2,500 to $4,000/kW for the basic equipment with another $600 to $l,000/kW for a biomass storage bunker and $1,000 to $2,000/kW for installation.

The hybrid gasification/combustion system by itself costs about $300/kW. This component must be matched with feedstock storage and delivery ($600 to $l,000/kW), small-scaleboiler, small-scale steam turbine generator ($900 to Sl,200/kW), and other equipmetit, including contrôle, cyclone fly ash recovery system, and exhaust stack. Overall installed capital costs would be $12,000 to $18,000/kW.

O&M Costs

Most modular Systems are characterized by continuons operation, automatic ash and char extraction, automatic feed, and automatic process control. Maintenance of 0.5 to 3 hours per week is required for monitoring feedstock deliveries, ash removal, filter cleaning or replacement, and inspecting and fixing problems with the automatic feed system. In addition, prime movers such as internai combustion engines or microturbines require similar maintenance attention as for gas-fîred Systems.

The overall costs and reliability of these Systems has not yet been established.

Commercial Status

There are a number of small development companies working on modular biomass heat and power Systems (listed in Appendix D). Most of the Systems that hâve been installed in the United States are part of research, development, and démonstration projects fùnded by a variety of fédéral and state sources. DOE has an active research and development program on modular biomass as does USDA and the U.S. Forest Service. The United Nations also has an ongoing program in this area to develop village power Systems using biomass.

⁴⁹ Smith, 2006.

5. Biomass Conversion Technologies

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Biomass Technology Review

October 21, 2010

Prepared for

Biomass Power Association

Prepared by

McHale & Associâtes, Inc.

Center Street

Portland, ME 04101

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Executive Summary

This study was performed for the Biomass Power Association to review current technology that is available for high efficiency biomass power génération. The available technology is listed with a brief description of the technology.

The Massachusetts Department of Environmental Resources (DOER) has proposed new requirements for biomass Renewable Energy Crédits (RECs). The minimum standard is a net plant efficiency of 40% to receive '/2crédit and a net efficiency of 60% to received a full crédit'. This study concludes that such efficiency standards are not achievable by a power génération unit currently in operation or by any new unit to be buih any time in the foreseeabte future.

Eleven existng plants were in the United States and Canada were reviewed. The average efficiency for a biomass power génération project is 23% The heat rate for power génération ai biomass leaders in the industry is between 11,700 Btu/kWh (29.2%) and 20,000 Btu/kWh (17.1%).

Regarding new facilities, the Report concludes that no new existing, financeable, commercially proven technology is available to meet the proposed efficiency standards.

The proposed efficiency standards can only be met by using cogénération, or Combined Heat and Power (so-caled CHP’), which changes the économies of biomass energy from electricityonly to providing electricity as a by-product of thermal production. An existing facility thaï currently qualifies under the Massachusetts RPS program is not likely to draw a large industrial host to the facility and are uniikely to find financing even if such a hosl were found. . Even assuming that new biomass thermal applications could be economically justifiod given the price of competing fossi fuel sources, lhe distance from the fuel supply and the number of fuel deliveries to the plant eacli day makes such applications highly unlikely.

District energy applications are unlikely to be built under the proposed requirement.. The reason is that the heating load of a District Energy facility Is not constant over the year. The heating load in the summer is zéro; the average annual heat load is about 44% of the winter peak. Plants are likely to run only part of lhe year. For the periods that they do run and meet the efficiency requirements, thepower generated is reduced to provide the thermal load, which results in reduced REC revenue that is insufficient to run the facility profitably.

The European biomass expérience is not directly applicable to the New England market. Feedin tariffs, a mature carbon market, long term stable market incentives, and a much higher power cost make CHP and district energy projects attractive. None of those factors exist in New England today.

Flnally, It Is important to noie that lhe literature descrlbing high efficiency power plants is misleading. It is important that common terms and définitions are used. The standard in the United States is to use Higher Heating Value (HHV) for solid fuel projects. In Europe, Lower Heating Value (LHV) is used for calculation of lhe fuel heating value and plant efficiency. Depending on the fuel, there is a 4%-7% différence in the resuit. So the reported 35% efficiency

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Biomass Technology Review is 33% on a HHV basis. Additionally, the efficiency can be reported on a Gross output basis or a Nel output basis. The Net output is the Gross less the plant auxiliary load. For a typical plant, 1he auxiliary load is 10% -12% of the total génération. Assuming the reported 35% efficiency was based on gross output, LHV basis, the HHV, net efficiency would be less than 30%.

In summary, using a high efliciency standard for biomass power production is not reasonable, lacks économie viability, and assumes European-style markets and subsidles that are not found anywhere in the United States. The resuit of the proposed efficiency requirement will be to eliminate biomass as a ready, dispatchable, renewable energy power resource from the existing Massachusetts portfolio of renewable energy. and create a barrier for new biomass electricity anywhere in the Commonwealth or the Région.

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Biomass Technology Review

Table of Contents

Executive Summary1

Introduction6

Définitions6

Background6

US Biomass Power Market6

The European Biomass Power Market9

Power Génération versus Combined Heal and Power Plants9

Conversion of existing Biomass Power Plants to CHP facilities10

Plant Efficiences10

Efficiencies12

Heat Rate12

Efficiency12

Carnot Efficiency12

Rational Efficiency13

Overall Efficiency13

Energy Utilization Factor13

Overall Efficiency13

General Efficiency Notes13

Higher Heating Value versus Lower Heating Value13

Location for Measurement of Plant Input and Output values14

Merchantable Bio-products14

Cycle Efficiencies for Thermal Power and Chemical Cycles15

Technology Discussion19

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Biomass Technology Review

Steam Rankine Cycle

Steam Generators or Boilers19

Suspension Type Burners20

Hearlh Type Boilers21

Grate Boilers21

Fluidized Bed Boiler22

Steam Turbines22

Condensing Steam T urbine22

Extraction Steam Turbine23

Heat Rejection23

Gasification24

Gasification Boilers25

Synthesis Gas or Liquid Gasifiers26

Pyrolysis Systems27

Gasifiers for the production of Merchantable Bio-products28

Gasification for Gaseous or Liquid Fuel Cycles28

Simple Cycle IC based CHP plant29

Simple Cycle Combustion Gas Turbines30

Simple Cycle Micro turbines30

Heat Recovery from CTG units30

Combined Cycle Plants30

Other Power Génération Cycles31

Sterling Cycle Power Plants31

Organic Rankine Cycles 32

Entropie Cycles32

FuelCell332

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Biomass Technology Review

Typical Fuel Utilization Efficiencies for Biomass Fueled Power Cycles

..............................33

Fuel Quality and Cosf33

Cogénération Discussion34

Thermal Demande for Waste Heat34

Industrial Processing34

District Heating and Cooling35

Biomass Project Economies39

New England Biomass Plants39

Biomass Project Costs39

Comparison between Fossil Fired Plants and Biomass40

Biomass Pricing and Delivery41

Biomass Plant Efficiency42

Project Economies44

Biomass Power Generating Case45

Biomass Cogénération Facility45

Small Biomass Combined Heat and Power46

Thermal Only Plant46

Small Thermal Plant (Heating Plant)46

Regulatory Risk46

Conclusions50

Référencés

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Biomass Technology Review

I. Introduction

This report examines the technologies and project économies for biomass power génération and cogénération In the context of a proposed efficiency standard for the Commonwealth of Massachusetts. Abackground of the biomass market in the United Siales and specifically in New England is discussed. A review of current and emerging biomass technologies is discussed. Project économies are presented for existing technology to compare power génération and cogénération schémas.

A. Définitions

The following définitions are used in this document:

AR - As Received

BD - Bone Dry (0% Moisture)

Blu - British Thermal Unit

CHP - Combined Heat and Power. Used inlerchangeably with cogénération

CTG - Combustion Turbine Generator

DE - District Energy

REC - renewable Energy Crédit

STG - Steam turbine Generator

Syngas - Synthesis gas

LHV - Lower Heating Value, generally used for fuel heating value outside the US HHV - Higher Heating Value, generally used as the standard in the US MWh- Mégawatt hours Q = Heat Transfer

W = Work

Subscripts

B - Boiter

A = Ambient, used for thermal sink

S = Stack

U = Useful Heat

B. Background (i) US Biomass Power Market

The growth of the renewable biomass power génération industry in the United States was a direct resuit of the passage and implémentation of the Public Utility Regulaiory Policies Act²which opened up power génération to indépendant power producers. A combination of an interest in reducing US energy imports, increased imported fuel prices, and a ban on new natural gas génération along with the availability of long term power contracte led to the construction of many “merchant” (non utility owned) biomass power plants during the 1980's.

As the fuel for biomass plants was plentiful and obtained at a low oost in rural areas, small capacity electric génération plants were installed in many rural areas where a logging and wood

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Biomass Technology Review processing economy existed. Although the fuel supply was plentiful, the Btu content was low and the fuel had a low density leading to the need to keep the plants relatively small to reduce trucking costs which generally limited a plant size lo a 10 to 20 MW output that could be supported by harvesting operations in an approximate 60 to 75 mile radius. The économies of biomass power génération has never been such that trees are eut solely to supply these plants, as the cost lo harvest the wood far exceeds the value of the fuel to the generator once transportation is included. The sale of wood biomass fuel Is generally used as a means of partially subsidizing the économies of a logging operation that is producing higher grade wood for sawmill and wood pulp production. Large amounts of low grade wood fuel are also generated during forest management procedures.

In addition to the standalone biomass electric power génération plants, the régional pulp, paper and wood processing industry long présent In the area installed blomass flred steam plants as fuel oil prices rose with some electric power génération capacity to primarily supply process steam and power for internai use for their processes. Also présent at some pulp producing facilities are recovery “boilers' thaï burn apulping byproduct, referred to as black liquor, as a means of chemical recovery and steam génération. Although black liquor Is occaslonally referred to as biomass fuel, the production of it is kept within one site and is part of the pulping cycle and therefore is not a viable biomass fuel with respect to régional electric power demand beyond load réduction at the facilities that generate it. These plants typîcally are not a major contributor of biomass generated power to lhe grid and will not be included in the discussion of lhe merchant fleet of biomass power plants in the région.

Subséquent to the installation of merchanl biomass power plants in New England, continued deregulation and the discovery of additional nalural gas deposits in North America led to a building boom of combined cycle natural gas power plants, which in turn led to an overail drop in energy prices below those that could be supported by the biomass industry. With a rise in the Interest In the potentlaf cïmate change impact ot continued fossil fuel génération, the Gommonwealth of Massachusetts established incentives to encourage génération of an ever Increasing percentage of their electric power from renewable power sources leading to the Massachusetts Renewable Portfolio Standard (RPS). Given the lack of significant renewable power génération currently available in Massachusetts, a market has developed lo supply the Commonwealth with renewably generated biomass power. Other New England states hâve also imposed RPS standards, each with differing interprétations and required percentages of renewable power. Despite the demand for renewable biomass power, there hâve been few merchant biomass power facilities constructed in the région since the 1980's due to lack of availability of long term contracte and low prices for natural gas. Recently, with lhe potentiel for long term incentives for renewable génération, merchant blomass power plants are again being proposed, although lhe Nation’s inability to place a price on carbon that would differentiate biomass from fossil fuels is limiting the aclual construction of plants. Figure 1 shows the current biomass power facilities located in the ISO New England market. Facilities that are REC qualified for the Commonwealth of Massachusetts are labeled.

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Biomass Technology Review

Figure 1

Merchant Biomass Power Plants in New England

The renewable power market is currentfy composed of two mature technologies and a host of small emergent technologies. The two mature technologies are hydroelectric and biomass power génération. Hydroelectric power génération in the New England market has plateaued and is shrinkîng as dams are removed for économie, fishery and recreational purposes. The emergent technologies, predominately consisting of wind and solar of various configurations, are slowly maturing although to date the technologies generally produce power on a non predictable basis that does not necessarily line up with the load demand of the région. As the majority of the electric power in the région is generated when needed with minimal storage capability. there is a damand for both primary types of electric power, base load and dispatchabie. Baseload power is typically generated on a predictable 24 hour per day or planned basis reflecting average régional demand; dispatchabie power is electric génération that can reliably be capable of being rapidly put into operation to supply transients in power demand. Hydroelectric can be baseloaded or dispatchabie depending on the availability of upstream storage. Landfill gas is base load power. Biomass can vary its load profile somewhat

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Biomass Technology Review to reflect System demand, The addition of émargent power génération adds a third component to lhe system which is intermittent. Although capable of generating power when appropriais resources, such as sun and wind are available, suitable dispatchable génération capacity or lhe capability to reduce the régional load must be available in case the resources are not available. Typically this dispatchable génération Is higher cost fossil fueled génération with lower efficiency. The ratio of the rated output of power plant and the amount of power that can be expected to be generated on a long term basls Is generally referred to as the availabilily of a plant. The mature renewable technologies typically hâve reliabilities in excess of 90% while the emergent technologies generally are regarded as less than 10%.

To date, both emergent technologies are dépendent upon large subsidies of various types to be economically viable. Although off shore generated wind has the potential to hâve a higher availability, its current deployment and predicted cost makes it a possible future complément lo the mature renewable technologies, but will not replace them unless there is a radical change in the New England Power Market and Its abllity to control load based on génération availability rather than customer demand.

Gnrrently the région exhibits a long term electric load demand with two seasonal peaks, one seasonal peak roughly corresponding to lhe peak winter heating load and a second major yearly peak corresponding lo the maximum stimmer cooling load.

(ii) The European Biomass Power Market

The current European biomass power market demand is a mix of demand for combined heat and thermal projects along with a growing demand for imported wood pellets to substituts a portion of fuel used in coal baseload power plants. Carbon réduction targets, high fossil fuel tariffs and an existing large coal based génération fleet hâve driven up the demand for renewably generated biomass power. Large existing district heating Systems in many régions along with very generous subsidies for renewably generated power of any type, has led to the installation of biomass fired combined heat and power facilities optimized to tie into the dislrict heating grids. Although district heating grids enable very high fuel utilization efficiency during fîmes of adéquate heating demand, the renewable electric power génération is a byproduct of the demand for heat. The relative scarcity of local wood fuel and high value for renewable fuel has led to a far reaching market of sourcing wood products from around the world. Given the économie and regulatory climate of shipping a low grade fuel long distances, the majority of the imported wood products are converted at the shippers site to wood pellets that allow the siting of biomass power plants in urban areas due to the far lower site footprint and local impact albeit at a far higher cost to the ultimate consumer.

(iii) Power Génération versus Combined Heat and Power Plants

The New England power grid is supplied by power generation-only biomass plants that are optimized to maximize electric power production. An alternative to power generation-only plants are Combined Heat and Power (CHP) plants, where lhe production ol electrical energy is balanced with lhe production of useful thermal energy. When there is a steady demand for both

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Biomass Technology Review thermal and electrical energy, a CHP plant can hâve higher overall fuel utilization than a comparable power- only plant. The vast majority of CHP plants are installed in industrial facilities that can generate electricity for less than the cost of purchasing utility power. The downside to a CHP plant is that the overall efficiency only remains high if there is use for the thermal power generated by lhe plant. Alhough there are several variations of CHP plants, the majority are set up to supply a thermal load to industrial facilities with electric power produced as a byproduct thus linklng the power production to the thermal demand of lhe facility instead of to the régional power demand. Generally, the économies of the industrial sites is lo remain a net user of power with sales of power to the gird only during unusual operational modes.

CHP plants are also occasionally inslalled where a small génération capability is installed on the outlet of the boiler to generate small volumes of power while dropping the stream pressure from a higher pressure lo a lower pressure. This is common where there is a small demand for higher pressure steam and a much higher demand for lower pressure steam. In the past, there was also some value for onsite génération to allow the heating plant to remain operational when grid power was not available. but few small generators are equipped with the required equipment to perform this task.

Newer CHP système are being installed where power is generated from a renewable feedstock and the résultant power is credited with Feed-in Tariffs that reward renewable power génération that offsels power previously supplied from lhe grid. Feed-in Tariffs are generally set at a high rate to encourage renewable génération. This method has been used quite successfully in Europe, although the overall costs hâve been quite high and most programs hâve reduced the tariffs recently to far lower levels in an attempt to reduce the subsidy cost. CHP units are primarily thermal units that hâve added equipment to generate power while supplying thermal demand rather than power plants intended to supply régional power demand. Therefore small CHP plants are not expected to contribute substantially to support the régional power demands that tend to occur independent of thermal load, leading to limited or no availability during spring summer or fall.

(iv) Conversion of existing Biomass Power Plants to CHP facilities

The conversion of a Biomass power plant to CHP purposes would be not be possible for the majority of the existing biomass power facilities in New England as there is no large year round thermal demand in close proximity to the plants. The plants, as currently configured, would require substantial alterations including replacement of the condensing steam turbine in order to export significanl volumes of thermal energy to an adjacent host facility ï one could be found.

III. Plant Efficiencies

There are numerous définitions tor efficiency used for the description of conversion of energy. As each définition is targeted for a different audience, it is easy to confuse one définition ot

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Biomass Technology Review efficiency with another leading to compensons of “apples to oranges. The illustration below in Figure 2 illustrâtes a generic thermal cycle.

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Biomass Technology Review

Qa.Qia

Thermal Process

Qs = Stack

W= Work (Electicj

Qa= Rejscted Heat

Qu= Usefu! Ttiemnal f« va»Fjcw*cai4rtt<vi»iue

Figure 2

Generic Thermal Cycle

A Efficiencies

The comparison of process and plant “efficiencies” Is difflculf as there are multiple définitions of efficiencies. In the US, the American Society of Mechanical Engineers publishes a sériés of Performance test codes that when properly executed can be usedto define the efficiency of a given thermal process and establish the llkely uncertalnty In the results. Barring access to standardized testing and an agreed upon test methodology, efficiency compensons are at best a broad approximation and at worse can be abused to make one type of power conversion process look betterthan another. Llsted below are some of the more utllized efficiency définitions.

Heat Rate - This term Is typically used In the electric power Industry to describe the amount of energy input required to produce a given amount of electric power. The typical Englîsh units are Btu/kW. Note of ail the efficiency définitions llsted below, this définition has the useful work output as a denomlnator. Ail others use It as a numerator. Therefore as the heat rate reduces, the plant efficiency increases.

HR-Qb/W _Effidency -Useful Work out divided by Fuel in ητΗ-W/Qb

Carnot Effidency - The Carnot efficiency Is the most efficient cycleto convert thermal energy unto work. This Is atheoretlcal cycle that cannot be obtained In practice but is useful in determining an upper maximum power génération. It is important to note

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Biomass Technology Review that the températures used in the équation are absolute températures, degrees Rankine in English units.

To ^Tb-TaI/Tb^Qb-CW/Qb

Rational Efficiency.- Is a ratio of actual work produced by a system to the syslem Exergy, which is the maximum useful work possible during a process that brings a system into equilibrium with a heat réservoir. The actual work is always going to be less than the exergy. This efficiency is useful for designing and optimizing processes.

r)q=W/the change in thermodynamic potential ot the system.

Overall Efficiency - Is the work output of the system divided by the fuel input where the fuel input is calculated by the mass flow rate of the fuel mulliplied by the calorific value of the fuel.

T]O = W/Qftri

Where: Q_FlMl = Fuel mass flow rate X calorific value

Energy Utilization Factor.- This efficiency is the closest approximation to the efficiency defined in the proposed régulation. It is the useful work plus useful thermal energy divided by the fuel input

E_uf = (W+Qu)/Qb

Overall Efficiency.- Tliis term is defined in the proposed DOER régulation 225 CMR 14.05(8)(b)(2). It is similar to the Energy Utilization Factor above with the inclusion of a energy value (Blu) lor any Merchantable Bio-products. As stated in the régulation, merchantable bio-products ‘shall be presaibed an energy content based on its enthalpy of réaction. Although a simple définition, the assignment of a value to a chain of complex chemical reactions that are occurring simultaneously with the production of useful thermal and electric may be complex to calculate consistently.

η = (W+Qu+ Q merchantable bio-products)/QB

General Efficiency Notes To further cloud the calculation of efficiency, there are several differing conventions thaï are used, which make comparisons between various processes difficult. Listed below are some common inconsistencies

Higher Heating Value versus Lower Heating Value

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Biomass Technology Review

There are two common methods of stating the heat content (Btu of kJ) of fuels. The Higher Heating Value (HHV) takes into account the condensation of byproducls, while the Lower Heating Value (LHV) does not. This reduces the numerical value of Btus for a fuel expressed on a LHV basis. The différence between the two are dépendent upon the constituants of each fuel, range from approxlmately 5% for coal, 10% for natural gas and a typical range of 6 to 7% for biomass fuels.’ The US power industry typically uses HHV for fuel input in efficiency calculations while the Européen Industry and combustion turbine equipment manufacturera use LHV for fuel heating value basis.

It is important that stated plant efficiencies and equipment efficiencies require units. Typical Européen plant efficiency quotes will hâve to be adjusted by the heating value ratio of LHV to HHV to be able to compare values with US plant efficiencies.

225 CMR 14 does not state if the fuel input will be stated as HHV or LHV which can Introduce a 6 to 7% différence In efficiencies.

Location for Measurement of Fiant Input and Output values

The location and définition of the inputs and outputs of a power cycle must be defined precisely and accurately in order to détermine a consistent efficiency calculation. The inlet fuel content can vary from the as received moisture content to the moisture content immediately priorto combustion. Fuel content can also be listed as the bone dry content ofthe fuel ignoring the loss in heating value due lo the moisture in the fuel.

Third party testing of power plants usually measure the plant revenue meter output for the power output. This reading includes any losses associated with step up transformera required to ralse the plant voilage to the grid voltage. Other efficiency measurements may elect to read the power output al the generator leads thus giving a higher than normal plant efficiency. In extreme cases, the plant may not account fully for energy used for internai station loads artificially raising plant loads.

Plant output readings ai tlie generator terminais represent the plant’s Gross Output. Subtracting the plant auxiliary loads gives the Net Output. The output and efficiency basis (gross or net) should be idenlified.

Merchantable Bio-products

The term merchantable bio-products has been introduced into the required plant efficiency for REC qualification. The proposed régulations définition is “For Merchantable Bio-Products the product shall be prescribed an energy content based on its enthalpy of reaction, to be approved by the Department, and those units of energy appropriately convertedto MWhs,

As the standard combustion process is efficient at converting the chemical energy in the incoming fuel to predominately a mixture of oxygen, CO2 and water vapor, any

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Biomass Technology Review merchantable bio-product removed from the power génération process will lead to a reduced power and thermal output.

The use of a direct conversion of chemical energy into electrical energy with no factor to account for the conversion efficiency will drive the power producer to bypass power génération in place of merchantable bio-product production as a way of meeting the DOE efficiency standards.

As the standard is wrltten, the contribution for merchantable blo-pcoducts Is 100% versus the contribution for thermal and power are reduced by the cycle eflidency. The resuit of this will be to increase the biomass input to a facility to generate an équivalent electric output. Given that the biomass resource is fuel constrained due to the économie distances to transport fuel, the net electrical output for each biomass facility will be less.

Cycle Efficiendes for Thermal Power and Chemical Cycles.- Figure 3 through Figure 5 illustrate the basic power génération cycles.

Biomass Technology Review

Euf»(W+Qu)/F

W= Net Work Cb=Net Useful Heat Output

Cogen (CHP) Extraction Qu

Basic Cycle Illustrations and Efficiencies -1 of 3

Figure 3

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Biomass Technology Review

Basic Cycle Illustrations and Efficiencies - 2 of 3

Figure 4

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Biomass Technology Review

Q>

Gasifier with IC engine

Turbine

Qo

Gasifier with Fuel Cell

Basic Cycle Illustrations and Efficiencies - 3 of 3

Figure 5

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Biomass Technology Review

IV. Technology Discussion

A. S team Rankine Cycle

The steam Rankine cycle is generally reported to generate 80% of the electric power in the world. The efficiency of the Rankine cycle is a factor of the boiler efficiency and the steam cycle efficiency. The design of the cycle accounts for the tradeoff between efficiency, capital cost, fuel cost, and plant lifetime. Decisions about pressure, température, reheat or regenerative heating are based on optimizing the project. Ail projeds hâve an optimum design that is not necessarlly the highest efficiency. The cycle has been optimized to generate the maximum amount of electric power from a thermal supply within cost constraints.

The three major components are a boiler, steam turbine and the heat rejection system. The boiler converts the fuel into thermal energy resulting in superheated steam vapor being sent to a steam turbine. Power plants based on this cycle and typical components are designed for baseload or daily cycling load operation with the maximum efficiency point occurring al or around 85% load. The equipment used is relatively large with a high mass and is prone to differential expansion Issues when cycled leading to the desire to maintain the plant warm even during periods of low demand. The basic components and flows of major constituents are shown in Figure 6.

Steam Generators or Boilers

There are numerous variations of boilers used to couvert the energy in the fuel to steam. Boiler design dépends on the fuel considered. A boiler designed for gaseous or liquid fuels are unsuitable for solid fuels without extensive conversion. Given the smatler size of biomass boilers due to the économies of fuel supply, the biomass industry has used relatively straighttorward designs thaï are flexible in the ability to deal with fuel that varies in particle size and moisture content. Although the typical biomass fuel moislure content is 45% by weight, the boilers are generally designed to accept wide variations in moisture content. The practical limit for combustion is approximately 60% moisture content where the energy required to dry and combust the fuel is roughly equal to lhe Btu content of the entering fuel.

Biomass power génération is usually based on a low value waste products from another higher value wood processing operation. Bark, sawdust, lumber ends, agricultural waste are typical fuel supplies and there can be a high level of non-combuslible constituents entrained in the fuel stream thaï must be accounted for in fuel handling and combustion.

Biomass boilers must also be able to handle a high level of non burnable constituents that are inhérent with a low grade fuel resource. This is typically referred to as bottom ash” which is predominately non carbon containing minerais that can be recycled for bénéficiai use along with inert gravel and rocks.

The maximum operating température and pressure of a boiler is a tradeoff between unit cost and the metallurglcal properties of the boiler and the downsiream steam turbine High pressure

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Biomass Technology Review and température advanced steam generator designs increase effîciency of the steam cycle but are more expensive to build and maintain.

Evaporate

Propane

Combustion Air ’t Thèse items add to cycle effîciency but are not required

Typical Rankine Cycle Biomass Power Plant

Figure 6

Rankine Power Plant

Suspension Type Bumers

Allhough rarely used for large biomass génération boilers but popular in coal boilers, a suspension bumer requires a finely ground dry fuel supply which is introduced along with a large volume of air to suspend” the fuel in the combustion chamber of the boiler. Radiant heat

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Biomass Technology Review from the walls and other burning fuel ignite the particles where the combustible constituent’s bum and any non combustible materials drop to the base of the boiler.

Given that a typical biomass fuel as delivered is quile high moisture content, this is not a good design for biomass use which usually requires the fuel to be introduced to the combustion zone fromadrying zone.

Sawmill facilities use this design on occasion to combusl sawdust thaï is finely ground and is relatively dry..

Hearth Type Boilers

This design is rarely if ever used for modem boilers. Fuel is deposiled on a burning bed of coals at the base of the boiler via injection ports or air swept feeders. A portion of the combustion air is injected under the bed to support drying, partial combustion and gasification. Fine particles are carried upwards for subséquent further combustion, while heavy particles remain in the bed until lhey hâve broken down into smaller particles. Hearth units are occasionally equipped with sloped vbrating grates to attempt to distribute fuel and coals somewhal uniformly and allow removal of non btimable solids with a manual or automated system. Other Systems of this configuration are manually cleaned out on a routine basis. The non uniformity of combustion leads to émissions controls issues and the labor required for ash removal hâve led to a réduction in their use.

Grate Boilers

Grate boilers are defined as either fixed grate or movlng grate boilers. A Fixed grate Is similar to the hearth type boiler. Fuel is added and bumed on the grate. The ash is removed by hand raking or by the action of new fuel pushing the ash off of the grate.

A moving grate added at the base of the boiler automates ash removal. The grate continuously moves in one direction to assist in spreading ofthe burning fuel pile and remove non burnable ash and inert solids from the bed. These unils are typically equipped with air swept feeders that attempt to spread the incoming fuel uniformly across the face of the bed. The operation of the unit must be adjusted carefully, as un-combusted carbon (char) can be carried past the combustion zone of the boiler into the downstream émission equipment. Unburned char reduces the boiler efficiency because it is energy added to the boiler that Is not combusted.

There are also some potential issues with the formation of CO unless careful addition of secondary air is applied. This design is a relatively economical to install and operate and many of the New England biomass units use this design.

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Fluidized Bed Boiler

Bubbling Fluidized Bed Boiler

Bubbling Huid Bed (BFB) boilers utilize a heated sand bed in place of grates at the base of the boiler. Combustion air is Injected under the sand bed at a velocity adéquate to partially suspend lhe sand bed in the air so thaï it responds in a matter similar to a fluid.

Solid fuel is distribuled onto the sand bed, where it partially combusts after drying and gasification. The sand in lhe bed beccmes turbulent and heated which acts to break down the fuel into small particles on a rapld basis. Non combustble ash and Inert solid objecte fall to the boltom oi the bed and are drained periodically using an aulomated system. The system potentlally leads to near complété combustion and minimal char carryover to downstream equipment. BFB boilers hâve a higher etticiency llian grale type stoker boilers that is somewhal offset by higher auxiliary loads for fan power.

Clrculatlng Fluidized Bed Boilers

Circulating Fluid Bed (CFB) boilers use a similar concept to the BFB wherein sand is fluidized by the addition of high velocity air. Unlike a bubbling bed system where the sand is retained in a spécifie lower zone of lhe boiler, a CFB unit circulâtes the hol sand Ihrough the entire range of the boiler combustion zone. The fuel is in contact with the sand and effective mixing and combustion allows good effîciency and low émissions.

The entrance to the tube section of the boiler is configured with a cyclone or l-Beams to remove the sand and char from the gas stream to be recycled back into the furnace. This leads to near complété combustion of ail burnable carbon in the fuel slream and is of particular value to lor hard to burn materials.

The CFB process also is of great value for fuels with contaminants such as sulfur, as lime can be injected into the bed for SO2 control. Although this technology is very good for coal and solid wastes, it is excessive for small facililies burning clean wood fuel and is very capital and □peralionally expensive due lo the high levels of erosive wear and high horsepower requirements.

Steam Turbines

The steam turbine consists of variously configured internai sections that converl lhe energy in steam to mechanical shaft power. Each indîvidual turbine is assembled out of various internai sections and optimized to operale under a given range of inlet and outlet conditions. There are two major types of turbines and one major variation

Condensing Steam Turbine

A condensing turbine is designed to obtain the maximum amount of shaft work out of a given steam input. A standalone sleam electric generating plant will typically use a condensing turbine to maximize the electric power génération The condensing turbine is typically the second most

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Biomass Technology Review costly component of a power plant and is designed to operate within spécifie operational parameters.

A sealed condenser is connected to the discharge of lhe turbine and operated at a vacuum. The turbine exhaust is a mixture of steam and some water droplets discharged from the turbine below atmospheric pressure. The discharge pressure is directly related lo température thaï the condenser cooling water température.

As the theoretical (and practical) efflclency Is controlled by the energy différence between the inlet steam to the turbine and the turbine exhaust, the efficiency of the cycle is increased as the condenser température is lowered. Generally this low température is supplied by either a cooling tower that is dépendent on the ambient wet bulb température, or a cooling water source such as cooling ponds, rivers or océan. As there are regulatory limits on thermal discharges into waler bodies, the use of river and océan cooling is increasingly rare for small power plants.

Due lo the ambient température, there is a seasonal change in the plant output and efficiency and the cooling waler température changes,

Extraction Steam Turbine

A variation on a straight condensing turbine is an extraction turbine. The extraction turbine is designed to allow a designed range of volumes of steam to be extracted from the turbine at intermediate pressures prior to the outlet of the turbine to the condenser.

The sleam extraction can be used to supply industrial or commercial processes. The regeneraiive steam cycle uses steam extraction to heat boiler feedwater to improve the efficiency of lhe overall cycle. Many of the current biomass power plants in operation in New England hâve small extraction stages used for feedwater heating to improve the plant efficiency. The number of feedwater heating stages is a function of plant size and the tradeoff between cycle efficiency and cost.

Backpressure Steam Turbine

Backpressure turbines discharge sleam al a higher then ambient pressure and température, generally for use in an industrial or commercial processes. The units are designed to operate on 100% superheated. Tlie efficiency of the unit is still constrained by the Carnot Cycle and due lo the higher pressure discharge a backpressure steam turbine will produce lower amounts of mechanical sliaft power at a lower efficiency than an équivalent condensing turbine operated at the same Inlet température. Backpressure turbines are generally physically much smaller than a similarly rated condensing turbine.

Heat Rejection

The condenser used at the exhaust of the steam turbine is a heat exchanger that opérâtes below atmospheric pressure. The condenser can be cooled with either a cooling water flow or a by air cooling. The majority of the small biomass plants use water for cooling although there are some air cooled units in operation in the région. Most water based Systems use cooling towers

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Biomass Technology Review that take advantage of direct cooling and évaporation to lower the cooling water temp to approach the wet bulb température of the ambient air.

The cooling tower dépends on évaporation as part of the cooling process and requires water makeup to the plant from outside sources.

An air cooled condenser uses far less makeup water at a cost of the loss of evaporatlve cooling leading to a higher operating température than obtainable with a direct cooling tower.

There are hybrid cooling Systems that mix attributes of both methods. A hybrid tower is used to reduce lhe water drift and plume from a wet cooling tower.

A remaining means of cooling traditionally used on larger power plants with access to water bodies is the use of once through cooling water. The use of once through cooling is rare in small biomass plants due to thermal régulations in effect for most water bodies.

B. Gasification

Gasification is the conversion of solid fuel to gaseous constituants. There are multiple variations on the process dépendant upon the source of heat and the relative amount of air used in the process.

Figure 7 illustrâtes the major variations in gasification technology and their state of commercialization. Commercialization is defined that the equipment is available for sale with émission and performance guaranlees and currenlly in commercial operation with an availability équivalant to commercial génération equipment by a party, other than the manufacturer or developer of the technology.

Small scale under 250 kW units were excluded from discussion due to their low potential impact to régional power.

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INPUTS

GASIFIER TYPE

INTERIÆDIATE PRODUCT

Electricrty Cbemicals

FINAL PRODUCT

POWER' ISpaiicADIasel·

Gasification Processes and Their Products

Commericalzed Near Commericialized Pilot or lab concept

South African processes were eicluded hom commericiaBæd status as theyare predominatelyoosi feedstock»

The Blomass Energy Foundation Press, Ncx/ 2002,3rd edftion T. Reed Fig 10-4

The base drawing for this figure was obtained from ⁴

Figure 7

Gasification Processes

Gasification Boilers

Although fuel drying, gasification, combustion, and heat transfer occurs in any solid fuel boiler, the term gasification boiler (or gasifier) typically refers to a low output commercial or institutional two stage device where one stage heats the solid fuel in the presence of low oxygen levels to drive out gases from solid fuel. The résultant gas stream is routed to a refractory lined vessel where additional air is injected into the stream to promote complété combustion.

The high température exhaust is routed through a conventional heat transfer device that either generates steam or hot water for either power production or heating purposes. Their major use is in small biomass fired heating plants as the added complexity over a conventional wood boiler is not économie for commercial power génération. An additional use that has proven popular is to instali a gasifier section upstream of a conventional gas fired boiler in place of the existing

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Biomass Technology Review gas burners lo allow buming solid fuels without and extensive boiler relrofif. A gasifier conversion allows rétention of a majorily of the boiler structure when switching to wood fuel.

Synthesis Gas or Liquid Gasifiers

Although wood fired gasifiers hâve been In use prier to the 1940's the technology was substantially abandoned thereafter. The gaseous fuel stream produced by the earlier design direct gasifiers, generally referred to as synthesis gas, had a very low Btu content, high moisture levels and contained condensable lars. The condensable tars caused downstream deposits and the liquids resulting from the moisture and condensed tars were generally corrosive and would now be considered hazardous waste. This technology was developed and used predominately in areas where conventional liquid fuels were in short supply and fell out of favor rapidly once conventional fuel supplies became available. There are still some third world use of this technology, generally in areas with excess biomass and little or no émission régulations.

An advanced level of this technology has remained in limited use in South Africa on coal fueled plants as a means of génération of various products including chemical feedstocks and fossil fuel replacements. By the use of the Fischer Tropsch process, numerous chemical feedstocks can be selectively produced, although typically the cost is such thaï conventional feedstocks are less coslly. Currenlly in the research or near commercial caiegory are improved versions for the conversion of solid fuel to gaseous or liquid constltuents by thermal breakdown. The driver far the resurgence is related to the use of renewable resources in place of fossil fuels for a feedstock which makes the résultant products qualified for slgnificant incentives.

Most of the effort on current gasification technology is to improve the gas treatment Systems to produce a higher energy density fuel, low in moisture without condensable tars and contaminants. Small scale units tend to incorporate equipment to sub-cool the synthesis gas stream and attempt to filter out the résultant condensables, thus forming liquid hazardous waste streams. Larger scale units use high température catalysts to couvert the tars to gaseous forms that will not condense or form deposits.

This technology is currently pre-commercial, nearing full scale trials for small scale biomass fired combined heat and power plants based on Internai combustion (IC) engines that are below the economical sizing of conventional biomass plants These units generally requre a higher grade of wood and sizing criteria compared to conventional biomass faciIitles. Nexterra Systems Corp ’has sold several full scale trial IC based units and Is nearing commercial production⁶. Nexterra reports efficiency near 60% but the available published data does not identify whether the efficiency is gross or net and whether it is based on LHV or HHV.

There are pre-commercial attempts at the use of synthesis gas to fire conventional gas turbines. To date there are no existing long term commercial applications with publically available performance resuis.

Although there are multiple uses and configurations for synthesis gas or liquids, the literature, indicates a range ot conversion efficiencies from solid wood to usable synthesis gas at a 60 to

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Biomass Technology Review percent efficiency⁷ when fed 20% moisture content biomass Some processes are capable of operation at higher moisture content, albeit ai a lower cycle efficiency. When used as a feedstock for power génération this puts synthesis gas at an upfront disadvantage as lhe 20 to 25 percent of the inlet energy which has been used to produce lhe synthesis gas will lead to lower cycle efficiency 1han obtalnable with natural gas or liquid fuels.

It is important to note that most advanced cycles that use gasifiers require low moisture wood and thaï drying wood to supply the unit is not included in lhe efficiency quoled.

Pyrolysis Systems

A subset of gasification Systems are pyrolyzers that use either direct or indirect heat generally at a lower température range to drive off volatile gases or liquide from the biomass feedstock. There are physical différences between a gasification and pyrolysis. In general though, processes thaï operate between 300°C and 600Ό are considered pyrolysis. Processes over 600%} are considered gasification. The température and lime determined the percentage of char, liquid, and gas that is produced.

The volatile gases or llqulds from the fuel can be processed to form merchantable bio-products. Dépendent upon process conditions, a combustible char product can be produced that can either be used ta heat the process or can be marketed as a constituent of a product called “bio char or bio-coal. When Bio-char is mixed with an appropriate blend of organic wastes it is means of low cost carbon séquestration and is used as a soil amendment. There is no currently viable market for this product beyond the demand for research.

Another product of pyrolysis can be a product referred to as bio-oil. Bio-oil can be burned directly in some industrial or commercial boilers or used sis a chemical feedstock for higher value products. It is potentially a competitor to rural biomass power plants in that a high value product can be processed local to a waste wood source and transported in a denserform to other markets. The NH Office of Planning commissioned a study “New Hampshire BioOpportunity Analysis³ to discuss the commerclallzatlon of the technology. Although It Is promising from a standpoint of biomass utilization, the process is a net energy user and it is not likely to be a contributor to the régional renewable power génération market.

Dynamolive Energy Systems’ has a full scale pilot fast pyrolysis system that generated commercial quantités of char and a liquid fuel referred lo as Bio-Oil. The plant was shut down, but is reporledly scheduled to restait in the 4¹¹¹ quarter of 2010. Conceivably this plant could intégrale apower génération cycle, although the company appears lo be marketing the products of pyrolysis as high value products.

An altemate merchantable bio-product process that has garnered some régional publicity is Maine Bio Products ¹⁰ Biofine process which uses a pyrolysis reaction along with other technology to produce chemical feedstocks from the lignin component of the biomass. In addition to the high value chemical feedstocks, char is produced as a byproduct. Although

Biomass Technology Review another promising biomass use, the process is a net energy user untikely to contribute to the régional renewable power génération market.

Both of the prior processes and a host of others do not hâve commercial facilities in place nor are they operational. They are untikely to be net producers of régional electricity in New England.

Gasifiers for the production of Merchantable Bio-products

As discussed in the introduction section, given that the combustion process is quite efficient at converting the chemical content of the fuel to gaseous byproducts, the removal of merchantable bio-products from a power or CHP cycle will reduce the plant output since the energy in the fuel Is removed from the process and Is not used for power génération. Although the Gommonwealth’s proposed régulation is writlen to address the génération ol renewable power. it has the indirect effect of incentivizing the génération of merchantable bio-products ai the expense of power génération.

C. Gastfication for Gaseous or Liquid Fuel Cycles

The use of synthesis gas is not yet commercialized for most direct combustion purposes; there is much discussion of this potential in the literature. Using internai combustion engines with biomass gasifiers for CHP is close to commercial production. It the technical and économie hurdles are overcome to convert wood synthesis gas into a clean usable gaseous fuel with adéquate properties for use in direct combustion devices, gas and liquid synthesis streams could become the fuel supply for several power génération cycles. Fuel supply limitations and capital cosl considérations limil the construction potential until there is a substantiel, stable, long term incentive for the production of renewable power. Thaï said, the technology is nol currently commercialized.

Figure 8 shows expected efficiencies and commerdalization status of the major gasification cycles when operated on biomass synthesis gas.

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Biomass Technology Rsview

Cycla Effîciency for Combined Heat and Power System» operatlnn on biomass fuel

Combustion Unt Type Commençai Biomass hstallalions?

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Electric Effîciency nal. gaa (HHV basls)

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Heal Génération effîciency onnat.gas____________

Electriceff. onsyrthesi” gasat__________

Heat Génération effîciency on syngaa_____________

Total Conversion gfficîency on syngas rotai Conversion efficlercy on syn gas

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Figure 8

Cycle Efficiencies for Biomass CHP Systems

Simple Cycle IC based CHP plant

The use of synthesis gas for CHP in IC engines is near or at the commercial slage with some customer units in place. The units reportedly are not economically compétitive with conventional heating and power génération Systems due to the high initial capital cost and competing fossil fuel prices, but are in some demand for démonstration projects where a premium for renewably

Biomass Technology Review powered electric and thermal is applied; and Incentives are available to offset the initial capital cost. There are inhérent limitations in the internai design ol this type of gasifier that limits the efficient output lo an internai dimensional limitation and therefore génération of large amounts of electrical power must be accomplished in multiple units thereby limiting the economy of scale. The best fit for this technology Is currently for onsite “behind the fence” génération In one to two MW gross electrical output blocks

Simple Cycle Combustion Gas Turbines

There currently are no CTG's that could be located in commercial long-term use operaling on synlhesis gas. Although the application is similar in concept to an IC application, CTG Systems are a better fit for large scale power génération as CTG's are offered in a wide range of sizes and hâve a very small equipment footprint for the equipment electrical output. These Systems will require the use of a dilferent configuration gasifier in order lo operate at the higher CTG fuel flow requirements. They are much simpler to operate than a steam Rankine cycle and do not require licensed personnel to operate. The limitations to the CTG are the tight internai tolérances and fuel quality spécifications. CTG’s are more susceplible to fuel deposits than IC engines.

Simple Cycle Micro turbines

A subset of conventional CTG's that compete with IC engines are micro turbines (generaly less than 1 MW) offered by several manufacturers. These units are typically intended for behind the fence applications where there is constant thermal demand. Although there are units rated for low Btu syngas, there are no commercial Systems offered at this point that Integrate a gasifer with lue! condilioning and the turbine in one package. Although the units are rated for syngas, their fuel quality requirements are considerably more stringent that IC engines.

Micro turbines are highly susceptible to fuel contamination making operation on synthesis gas difficult without extensive upstream conditioning and filtering. Given the low Btu content syngas from wood waste and the significant number of processing steps to generate syngas of sufficient quality to operate a micro-turbine, it is doubtful if lhe capital and operational costs for this technology will be attractive in the near future.

Heat Recovery from CTG units

The résultant exhaust heat from the units can be directed through a heat recovery device that generales either steam or hot water. The exhaust température (rom either device is in the range of 800°F to 1000°F dépendent upon actual configuration.

Combined Cycle Plants

Nalural gas fired Combustion Turbine Combined Cycle (CTCC) plants are a cost effective, high efficiency technology for use with naturel gas or liquid fuels. The main driver is the development of high efficiency CTG’s . Given the increase in CTG and CTCC efficiency, the availability and pricing of naturel gas, and the ability to quickly permit and construct faciities. a large number of

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Biomass Technology Review cycSng and baseloaded units hâve been installed across the country over the last decade. Like a simple cycle gas or liquid plant, lhe fuel is combusted in a CTG and the hot CTG exhaust gas energy is recovered in a Heat Recovery Steam Generator (HRSG) to generate high pressure steam where il is converted to power with a condensing steam turbine.

CTG inlet combustion températures are combined with the far lower (near ambient) discharge températures of the steam Rankine cycle leading to a high overall plant electric génération capacity. These plants are intended as electric power génération plants, as any thermal energy extracted above the steam turbine condenser température will lead to a reduced cycle efficiency. Typical efficiencies range from 40% to over 60% (LHV).

The tradeoff for this design is thaï the plant complexity increases from a simple cycle plant as there are two power génération cycles required. The plant size is most economical between 250 MW and 1500 MW. Although, there are extensive CTG based cogénération plants located In the United States.

Large 250 MW biomass based CTCC plants would be too large to be fueled economically from renewable waste wood supplies, as lhe radius of required fuel supply area would exceed the range where the fuel and resources required to haul the fuel would exceed the fuel value of the wood. Smaller plants could be built, but the capital cost per MW increases as the plant becomes smaller. Commercial application of lhe CTCC to biomass will require advances in hot gas cleanup to ensure the plant can operate reliably.

D. Other Power Génération Cycles

There are numerous alternative power cycles mentioned in the literature. Generally, however, they are a variation on current cycles. Many are in the early development scale, so published actual long term operational and efficiency data is not readily available.

Sterling Cycle Power Plants

A technology that is mentioned often In the literature is the Stirling cycle, generally referred to as an external combustion engine or oocasionally a heat engine”. The cycle uses an internai working fluid that is heated and cooled extemally to generate power. It is a heat engine and conslrained by the Carnot cycle with similar internai frictions! characteristics as IC engines. The major advantage to the cycle is the ability to uses a variety of heating and cooling sources to generate power. As combustion is extemal to the engine, the fuel quality should potentially allow a lower grade of fuel to be bumed to heat the unit. Although long mentioned as a possible future power génération cycle due lo its theoretical efficiency and fuel flexibility, to date it has been notoriously difficuh to commercialize. Currently the major use of Stirling generators are for solar to electric power generators with one large scale deployment in operation in the US west with another recently approved for California. There hâve been niche applications being developed for microscale CHP use with one commercial unit made by Whispergen” in production.

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Biomass Technology Review

Organic Rankine Cycles

Organic Rankine Cycle (ORC) Systems utilize low boiling point fluids as an alternative to steam in a conventional Rankine cycle. By using organic fluids with low boiling points, the ORC system can capture waste heat from other sources and generate electric power.

The ORC unit is a Rankine cycle, and its efficiency is constrained by the Carnot cycle. The primary value of an ORC unit is for dealing with relatively low température waste heat sources that are O low to economically generate power with conventional steam Systems. ORC equipment, manufactured by Turboden,¹² is currently used in Européen pellet manufacturing processes where large volumes of relatively low température heat are required. When matched with an appropriate thermal demand, this equipment reportedly has high overall fuel utilization efficiency, well above competing technologies. Although capital intensive, the combination of high feed-in tariffs and high cycle efficiencies appears to be economically attractive in the Européen market for wood pellet production. In the US, ORC is being used for geothermal power plants and is being advocated for use as low température heat recovery units. Currently the low efficiency and high capital costs of small scale equipment hâve restricted the use to subsidized pilot applications.

Entropie Cycles

There is little publically available information on this power cycle.¹³ The Entropie Cycle appears to be targeted for similar small electrical output applications as Organic Rankine Cycles. The claimed thermal conversion efficiency is 71%, with a 194 deg F thermal outlet température. It appears to be a thermodynamic concept with no reported pilot of commercial installation.

Fuel Cells

Although a fuel cell is not a thermal cycle, it is capable of generating energy from a chemical fuel stream leading to the technical possibility of the operation of a fuel cell from a biomass gasifier stream.

Current fuel cell technology is oriented towards the use of hydrogen as a fuel source, with upstream reformer technology used to separate the hydrogen from the carbon molécules to allow use of hydrocarbon fuels. Current Systems in use are highly susceptible to catalyst “poisoning requiring careful high levels of contaminant removal upstream of the cell. Dépendent upon the reformer technology used, either CO2 or CO is formed as resuit of reforming. These two compounds generally act as “poisons’' in the catalysts used in the fuel cell and therefore high fuel purity is required. The proton exchange and solid oxide fuel cells both operate at relatively low températures and therefore the thermal output is too low for most applications

There are research scale fuel cell technologies including Direct Methanol Fuel Cells that can burn methanol which can be produced via biomass gasification and reforming. There are two variations of fuel cells, Molten Carbonate Fuel Cells and Solid Oxide Fuel cells that hâve the capability of processing CO directly. Both technologies are in the pre-commercial phase for

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Biomass Technology Review large Systems. There are some small scale units (less than 20 kW) currently marketed tor high value specialized applications.

Typical Fuel Utilization Efficiencies for Biomass Fueled PoweT Cycles - Figure 9 shows the typical cycle efficiencies of various power cycles from multiple sources. As noted, the Organic Rankine Cycle system efficiency for the commercial system is capable of high cycle efficiency only when there is a demand for low température, 180°F thermal output.

iName	State or Prov	Heat MW ;Rate	PSI	Temp	Boiler Type	Cond enser	Wet Bulb Temp *2	Carnot Eff	Reported Eff. KW/Heat Rate *3	Actual effyCarnot eff.

1;Williams Lake	RC	60 11700.1575	95O:Stoker	Cl	57 5	63%	29%	46%
2;Shasta	CA	49.9; 17200	901'	9O5:Stoker	Cl	62 3	62%	20%	32%
3:Colmac	CA	49:12400:1255	925;Fluid BedCT	/6.4	61%	28%	45%
4 Straîton	ME	45 13500; 1485	955:Stoker	CT	66.7	63%	25%	40%
5 Kettle Falls	WA	46 14100 1500	950:Stoker	CT	64.3	63%	24%	39%
6 Grayling	Ml	36;13600;1280	950:S1oker	CT	71.7	62%	25%	40%
7 Mc Neil	VT	53 14000 1275	95O:Stoker	CT	70.7	62%	24%	39%
8 Multitrade	VA	79.5h 4000;1500	95O;Stoker	CT	75.6	62%	24%	39%

Average for 8 plants with expected heat rates				62%	25%	40%
9 Mariera	CA	25 20000	850	850;Bubbling ;CT	'69.3	60%		29%
10 Chowchilla II	CA	10;20000	650	750	Bubbling	CT	69 3	56%	17%	30%
11 El Nido	CA	10:20000	650	750	Bubbling	Cl	69.3	56%	17%	30%
Average Values	for i i	biomass pi:	mis re	poried				61%	...............23%	.........37%

Figure 9

Typical Cycle Efficiency

V. Fuel Quality and Cost

The biomass fuel used by conventîonal merchant power plants has little use to other buyers. The plants are typically equipped with extensive processing to preprocess the biomass for combustion. The fuel stream includes some sawmill residual, bark from debarking operations, whole tree chips including branches leaves and twigs and on rare occasion bole log chips composed of the main trunk of the trees. Ail of these fuels hâve particular handling

Biomass Technology Review characteristics that generally require btendmg of the fuel and extensive processing equpment to remove non burnable contaminants and resize fuel to within a range of sizing that can be metered successfully into the boiler.

As the fuel input requirements of the boiler decreases to smaller boiler Systems, the fuel characteristics must be more uniform. The recommendations for small scale school thermal only boiler Systems installed in many Vermont school districts¹⁴ has led to the recommendation that only bole tree chip or residuals from spécifie manufacturing operations be used for fuel. If this expérience Is applied to potentiel future installations of small biomass CHP units in Massachusetts, this will tend to drive the market for CHP quality chips to a higher grade more uniform and costly wood product than the biomass product currently used by the merchant plants. As this higher grade wood is in demand for wood pellet manufacturing applications, the cost will inevitably increase, and lower grade biomass will be underutilized.

VI. Cogénération Discussion

Thermal Demande for Waste Heat

In order to generate electricity in a thermal process, low température thermal energy must be removed from the power génération process. If there is demand for the thermal energy, the température and quantity of the thermal demand will establish the lower operating température of the power génération cycle. There are two options for thermal demand-- industrial processing and district Heating and cooling. Thermal demand is directly linked to the power génération of the System. If the thermal demand decreases and there is no other way to remove heat from the System, power génération will decrease.

Industrial Processing

The demand for thermal energy at industrial facilities' is as variable as the industries themselves. A broad generalization is that the majority of thermally intensive processes use steam to directly heat processes and reactions, with the maximum process température required generally setting the température from the boiler (or turbine extraction).

Intermediate, heat transfer fluids may be used internai to the process, but generally the heat transfer fluids are heated directly by steam from a central boiler. In some processes, gas fired infrared radiant heaters or electric résistance heat is used in specialized areas, generally in facilities with no central heating plant.

In addition to direct thermal processing, a large load demand is drying of products generally by the use of steam to air heaters which typîcally condense the steam to a saturated water mixture. The steam coil air heaters typîcally heat large volumes of air which is used to reduce the moisture content of materials, speed up solvent release or speed up cross-linking in polymer Systems. Most long term facilities hâve implemented energy conservation methods, if economically viable, wherein heated exhaust streams are used to preheat incoming air or materials. In addition to process spécifie thermal demands, inevitably there is a space heating

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Biomass Technology Review and cooling dernand that is dépendant upon the outside température. Space heating and cooling will be discussed in detail in the district heating seclion.

At times, regulatory policies and energy costs hâve made the installation oi cogénération Systems at industrial sites attractive and there are many large facilities that hâve contractée! with third parties to install these Systems as the expected rates of return for power génération does not typically match up with the expected rates of returns for Industrial processes.

Building a cogénération system adjacent to the manufacturing facility présents a power developer a long term issue in that lhe design and operation of the power génération faciïty is dépendent upon an externat party, the owner of lhe industrial process. If the industrial process shuts down, the power plant project économies may be substantially affected¹⁵. In general, lhe linkage of a power facility to a spécifie manufacturer introduces significant long term investment risk into the decision to build a cogénération plant.

District Heating and Cooling

Outside of internai use by the power plant for lhe processing and production of merchantable bio-products, the potential use of this thermal energy Is generally directed at the space heating needs of adjacent structures. The distribution of heating for space thermal demanda is generally referred to as District Heating (DH) Systems. There Is also potential to provide cooling In a district energy system, generally referred to as District Cooling, although low operating efficiencies, high capital cost and the thermal constraints imposed on CHP plants makes this a less attractive option in most areas except for high density cooling loads.

District heating Systems are capital intensive and require dense, urban scale applications to be cost effective. In less dense applications, heavy infrastructure subsidies are required for DE to be cost effective. The capital requirements and location is directly contrary to the fuel needs and the operation of a typical biomass power plant which requîtes signilicant acreage for fuel storage and processing along with extensive truck deliveries. Like many industrial operations, operating on a 24 hour per day, 350 day basis, a biomass plant is typically not compatible with the residential and light commercial activities in a many cities.

Implémentation of a new district heating system is difficult as there is little incentive for potenlial customers to make use of the service when there is a substantiel upfront cost to convert existing heating Systems to operate with district heating. Infrastructure issues are substantiel as the syslems need to be installed in either public right of ways or on negotiated right of ways over private property. There are reliability concerne that must be overcome until multiple combustion units are in place and connected to the system to allow some redundancy to cover unexpected power outages of thermal sources.

There are twoforms of DE Systems in common use, High Température and Low Température.

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High Température Disirict Heating

District energy Systems were developed and still in use In some urban cilles in the United States. The Systems in operation are high température Systems that use steam. The steam is routed to primarily commercial and governmental facilities in city carriers, using insulated steam and return condensate pipes. Each facility served by the system is connected to the disirict system via two underground pipes, one carrying steam into the building and one carrying condensai© back lo the district energy plant. The underground infrastructure for these Systems is capital extensive and can be a major issue in the installation or extension of Systems in any bul dense urban areas with access to low cost capital.

Steam used by the customer is condensed and returned via a smaller diameter ppe back to the district heaiing plant for reuse.

Building cooling can be provided with additional piping from a central plant or with remole the installation of absorption type cooling units, although their économie use is generally restricted to high value commercial applications due to absorption chillers low efficiency and capital cost. The advantage of absorption chillers is lhe balanced steam load year round.

The market for district heating in college campuses is driven bythe initial capital cost of the system balanced against the reduced need for maintenance of individual building heating Systems.

High température Systems are generally fed by multiple boilers to provide seasonal load adjustment and maintain system reliability.

Low Température District Heating

Low température district heating Systems use hol water for heat transfer to the district’s customers. Unlike a high température system, the water temp is generally inadéquate for use as driver for absorption cooling which substantially reduces any opportunities for summer thermal load demand. The use of hot water in place of steam requires larger diameter supply and return piping for an équivalent heat load. The system température is constrained by the use of preinsulated engineered thermoplastic pping Systems that hâve lower installation costs and Installation requirements than steam piping used in high température Systems. The possible lower installation costs are offset by increased pumping costs and the need for either smaller heating plants placed close together or the use of hybrid Systems, using separate dedicated steam lines to reheat the low température water Systems.

The development of low température district heating is dépendent upon a significant amount of regulatory Incentives, fossil fuel tariffs. carbon réduction Incentives and building design standards to be cost effective. Combinations of these hâve been put in place at differing levels in the European countries that are actively maintaining and installing these Systems. Each country uses a different combination of publicly owned or user owned Systems. A combination of incentives and penalties on the government’s part provide support for these Systems. Although the incentives/penalties vary by country the following issues hâve to be addressed

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Low température district heating system températures do not support the use of fin tube radiation (typically used in many existing New England homes and commercial properties), unless an eleclrlc hea1 pump system is used to raise the water température. A combination of regulatory requirements, high energy costs and building standards, hâve been used in Europe to encourageirequlre Installation of radiant type heating Systems that are capable of operation at much lower source températures, thus reducing the need for heat pumps. Retrofitling an existing structure with radiant type heating Is expensive and Is a cost born by the building owner. Wlosl US commercial Systems also require higher température source water and will require either a heat pump to raise lhe water temp or the replacement of the heating coils in the HVAC units.

The overall heating demand per customer needs to be as low as possible to reduce the size of the installed district heating infrastructure. High tariffs on fossil heating fuels and building codes that require minimal energy usage generally hâve been used in Europe lo drive the heating demand down per unit volume. The current regulatory approach In lhe US has been limited to voluntary incentives to encourage upgraded efficiency. Although building efficiency standards are now In place in most New England areas, the majority of new construction tends to be In low density rural settings with the core of the housing stock in urban areas consisting of older less energy efficient Systems.

Govemmental support/ownership of district heating Systems is generally required to subsidize the high capital costs and low investment returns. Regulatory incentives including Tnusl connect” requirements and heating fuel utilization efficiency requirements create an incentive for high customer participation.

Impact of District Heating Thermal Loads on Electric Power Génération

As shown in Figure 10, a typical central Massachusetts heating and cooling degree days and the ISO electric load are plotted for a typical year.

The thermal heating demand for the Worcester Massachusetts based on the Worcester airport data varies widely from a winter peak to a summer period with no heating demand. Worcester Mass, was selected as it is near the center of the state and therefore should be représentative of the typical thermal demand curve for the state. The thermal loads and the ISO NE power demand are shown as the percentage of the monthly peak demand for purposes of comparison.

If the demand for summerlime cooling is added lo the thermal demand there is some summer load, although supplying this summer cooling demand would require the use ot a high température district heating system to supply adéquate température Ievels to supply absorption type cooling units. The high température syslem increases increase the outlet température of the accompanying power génération cycle in a CHP plant, and reduces the plant efficiency . Given this wide variation in thermal demand, the demand for useful thermal energy from a district heating syslem is very limited during the psriods of the highest summer time load demand.

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Biomass Technology Review

In a district heating application The lack of a continuous thermal load demand over the yearly makes it financially unattractive to connect a CHP to a district heating network as it will only be able to receive REC incentives during times of high thermal demand in the winter, early spring and late fail. It will be unable to receive REC incentives during summer periods when the demand for power is the highest.

As the power demand will remain during summer periods, fossil fueled power génération plants will hâve to generate additional power to compensate for the lackof renewable CHP produced power.

*1 Data for power consumption from ISO New England *2 Degree Data from 2009 ASHRAE Cllmatic Conditions for Worcester Mass Régional airport

Figure 10

New England Heating/Coolirrg Degree Days

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Biomass Project Economies

The project économies for a biomass facility are directly related to size and scale of the biomass power plant. The key aspects of biomass power génération are the project size and the fuel cost. Fuel cost is largely transport distance dépendent. The plant size détermines the capital that can be directed toward efficiency.

New England Biomass Plants

Large biomass power génération facilities hâve botter économies of scale. However, larger units are designed to a different standard compared with small units. An optimum size for a biomass power génération facility is about 50 MW. Mosl of the existing biomass power plants in New England are 15 MW to 30 MW. A list of biomass power génération facilities is shown in Table 1. Note that Boralex Stacyville was not listed In the database.

Table 1

Current Operating Biomass Power Facilities in New England”

Slate	Plant Name	Nameplate Capacity (Mégawatts)	Energy Source 1	Energy Source 2	Initial Yaar of Operation	Unit Statua
Operating units
ME	8oralex Ashland	396	WDS	DFO	1993	OP
ME	Boralex Fort Falrfield	375	WDS		1937	OP
ME	Boralex Stratton Energy	457	WDS	DFO	1939	OP
ME	Boralex Livermore Faite	396	WDS	DFO	1992	OP
ME	Greenville Steam	15,6	WDS		1983	OP
ME	Indeck West EnfIeld Energy Center	275	WDS		1987	OP
NH	Bridgewater Power LP	20	WDS	DFO	1937	OP
NH	DGWhitelield LLC	16	WDS		1988	OP
NH	Pinetree Power	175	WDS		1986	OP
NH	Plnetree Power Tamworth	25	WDS		1937	OP
NH	Schiller	50	WDS	BIT	1955	OP
NH	Springfield Power LLC	16	WDS		1987	OP
VT	J C McNeil	59 5	WDS	NG	1984	OP
VT	Ryegate Power Station	21.5	WDS		1992	OP

Biomass Project Costs

The project costs for new power génération units hâve risen dramalically over the last four years. Today, a typical 25 MW biomass power project is assumed to cosl about $112.5 million or $4,500/kW compared with an expected cost of about $2,500/kW in 2006.

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The most recent biomass project Is Snowflake in Arizona. The project was completed In 2007. The project costs are reported to be $2,200/kW with used, reconditloned equipment.

New,50 MW projects hâve reported an EPC cost of over $4,00Û/kW¹⁷

A comparison of plant costs In 2003 versus 2008 is shown in Hgure 11

Nuclear

Cunvuntionaf Coal

Cumbined Cycle

Combustion Turbine

Wirtd

Geuthermaf

Cuncuntrated Soiar

$0 1<0δβ XGÔÔ 4_xffi3û 5,000 β,οοη ?,ÔÔÔ

Figure 11

Power Plant Construction Costs

Comparison between Fossil Fired Plants and Biomass

Often bomass plants are lumped in with other solid fuel plants when discusslng design and économies. The general différences between a biomass facility and a fossil power plant are:

Fossil plants are characterized by a large infrastructure associated wi1h coal mining and -transport. Fossil plante are located near rail and high voltage power Unes. Biomass has highly decentraiized harvestng and transport Infrastructure. The source of biomass fuel Is local and Is transported by 1ruck. A typical radius for fuel sourclng is 60 miles to 75 miles.

141

Biomass Technology Revlew • Biomass is expensive to handle and transport. Coal is an energy dense fuel with a heating value of about 12,500 Btu/lb (AR). Wood has a low heating value of about 4,400 Btu/lb (AR) assuming a 50% moisture conlent. On a per volume basis wood is about 1 /3 the energy density of coal. Moving biomass by truck adds transport cost that makes project économies difficult for long haul distances.

Large utility sized fossil plants can take advantage of scale. The larger fossil facilities hâve better économies due to better fuel cost, higher efficiency, and reduced staff.

Coal plant efficiency is demonstrafing Incrémental efficiency gains with high température, high pressure, and double reheat supercritical Rankine cycle designs and advanced Integrated Gasification Combined Cycle (IGCC) designs. The highest reported efficiency for a coal fired ultrasupercritical steam generator is 42.5%.

Improvement of biomass cycle efficiency is in a nascent stage and is not available on a commercial or économie scale. Even if a biomass plant could reach 42% efficiency, advanced cycle design is not economically attractive for small biomass facilities competing with natural gas, combined cycle based power prices in the market.

Biomass boiler efficiency is limited due to the moisture content of the fuel.

Biomass Pricingand Delivery

Biomass power génération is limited to the availability of biomass. A typical facility is based on the available wood that can be reasonably harvested within transport range of the plant. A typical biomass project is 15 MW to 30 MW in size based on the wood avaiable within a région. A typical économie radius for a biomass plant Is 75 miles. Beyond 75 miles, the transport costs raise the cost o( fuel and the résultant cost for electric power produced by the plant. As an example, the raw wood cost is typically $4.00 lo $10.00 per ton. Harvesilng is $12Λοη to $18/ton. Assuming a transport cost ot $0.10 per mile (round trip) a 75 mile radius adds $15 per ton lo the fuel cost. For comparison, the average delivered biomass price is assumed to be $30/Ton as Received (AR). Assuming 40% moisture the delivered fuelprice is $50/Ton (BDT)

Large biomass facilities are feasible where substantiel biomass resources are available, or where transportation such as rail makes additional fuel available, albeit at a higher overall handling cost. The optimum plant size is generally considered to be 50 MW. Larger 100 MW plants hâve been proposed where fuel is available. Within the 15 MW to 25 MW size, there is a balance between technology cost, tuel cost, and plant cost

An additional issue for biomass power plant location is delivery of fuel. Normally, fuel is delivered using truck transport. The number of trucks per hour can be an issue in urban areas. A 50 MW biomass plant requires about 70 truckloads per day or 140 trips.

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Rail delivery éliminâtes the truck transport issue but requires multiple fuel handling steps that increase the delivered fuel cosl.

Biomass Plant Effîciency

A survey of biomass plants in the United Stales indicates that the heat rate for power génération at biomass leaders in the industry was between 11,700 Rtu/kWh (29.2%) and 20,000 Blu/kWh (17.1%)¹⁸. Eleven plants were reviewed in the United States and Canada. The Average effîciency was 14,840 Blu/kWh (23%).

The actual operating effîciency of a plant is not the same as the design efficiency. Variables such as the fuel moisture content and ambient température hâve an effect on the plant efficiency. The adual plant efficiency may be +/- 3% from the average.

The best reported efficiency for a biomass steam plant is 35%. The planl costs are not readily available. Kônigs Wusterhausen was placed into operation in year 2003. The facility is a 20 MW reheat cycle wilh a reported gross efficiency of 36.4%. This efficiency should be examined to ensure that the reported efficiency is on the same basis as used in the United States. Comparing US reported efficiency with European facilities requires adjustmenl for:

The US uses Higher Heating Value (HHV) compared with the European Lower Heating Value (LHV). This is typically 6 to 7% différence which leads to a 6 to 7% overstatement of efficiency as compared to US.

Gross efficiency does not accounl for the plant eleclrical load (parasitic load). Net outpul is the gross output less the plant auxiliary load. This value varies by plant design but a general range is 10% to 15% of gross output is consumed for plant loads.

The fuel moisture was not reported. Often European designs are based on low moislure content biomass fuel of 20%, compared with New England typical biomass moisture content of 40% to 50%.

The net efficiency for the Kônigs Wusterhausen facility is expected to be 29% % (HHV) or (11769 Btu/kWh).

Cost data for Kônigs Wusterhausen is not available. However, the plant was partially subsidized, received carbon crédits, and is in a power market that has a résidentiel rate of €21.1 ($0.30/kWh). The plant received a €7.71 feed in tariff exclusive of other crédits for low carbon génération.

The Biomass IGCC at Varnamo, Sweden” (CHRISGAS) is a small 6 MW electric, 9 MW thermal pressurized, CFB plant operated and was mothballed in 2000. The unit is nol commercially operating. It's hislory is limited to 3,600 hours of operation. The reported electric efficiency was 32% (LCV) and would be équivalent to 30% (HHV).

The major Issue with lhe facility was the hot gas cleanup System. Similar issues were experienced with the FERCO gasifier in Burlington, VT.

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Project costs were not reported however, it was noted that the facility was shut down due to poor économies. The facility is currently used for Research and Development (R&D) for gas synthesis projects

Applying cogénération or CHP will reduce the plant’s electric efficiency but will increase the net overall efficiency since the thermal load is fully counted in the équation. A 25 MW power génération plant efficiency is shown in Figure 12. The base plant has an efficiency of 27% with a condensing steam turbine. As extraction is increased, the electric efficiency drops because the same fuel heat input generales less power. The net efficiency increases to a maximum of 75% which is équivalent to abackpressure steam turbine. The réduction in output is shown in Figure 13.

Figure 12

Effect of Cogénération on Plant Efficiency

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Energytù Process

Figure 13

Effect of Extraction on Plant Output

Project Economies

An examination of plant économies and the effect of cogénération (CHP) was undertaken to identify typical efficiencies and project économies that could be expected for biomass power and thermal energy production. The cases are simplifîed first year proforma calculations typically used for screening studies to détermine viability of projects. The cases examined include:

1. New Biomass Génération - new 25 MW biomass plant with génération only.

2. New Biomass Cogénération - 25 MW (condensing basis) with 150 psig extraction to an industrial process to meet a 60% net efficiency standard.

3. Smail Biomass CHP-backpressure steam turbine generator

4. Thermal Only Plant-Heat Only

5. Small Biomass Thermal Plant - Heat only.

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Each plant is discussed below. The évaluation for each plant is based on the following assumptions:

Market power rate is assumed to be $100/MWh.

Massachusetts REC pricing is assumed to be $20/MWh

Steam sales price assumed to be $8.5/1000 Ib.

Fuel price is assumed to be $30Λοη (AR) • Boiler efficiency for the large plant is assumed to be 80%

Boiler efficiency for the small plant is assumed to be 70%

Plant auxiliary load is assumed fo be 10%.

Thermal heat for CHP is based on average Worcester, Massachusetts Heating Degree Days. The average annual thermal load is assumed to be 44.5% of the peak thermal load.

Although absorption chilllng can be used, no cooling using thermal plant output is assumed • Plant availability is assumed to be 90%.

Calculations are based on single year estimâtes with comparison before taxes, dépréciation, amortlzation (EBITDA).

The projects are assumed to be developed with 50% equity and 50% debl. The equity return is 15% over Ί 5 years and the debt is assumed to be 8% over 15 years.

A summary is shown in Table 3.

Biomass Power Generating Case

The power génération case is based on a new 25 MW condensing Steam Turbine Generator plant similar to the base case. The project cost is $4.000/kW or $107 million. Project development is assumed to be 5% of the EPC cost for the project.

The EBITDA return for a new biomass power génération faciity is -14.4%. This is driven by an annual cost of capital of $16 million.

Biomass Cogénération Facility

The same size facility as the base case is assumed to be developed adjacent to a large industrial steam customer. The steam turbine is an auto extraction steam turbine with an extraction port at 150 psig. An annual average steam load of 140,000 Ib/h at 150 psig is exported from the facility. The plant electric efficiency drops to 14.8% but lhe net efficiency increases lo 61.1%. The electric output from the plant is reduced to 13.9 MW from 26 MW. MASS RECs are available for the 15 MW.

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The EBITDA return is -20%

Small Biomass Combined Heat and Power

A small CHP planl is examined relative to the base case. The boiler size is reduced to 50,000 Ib/h, 450 psig/600°F with a backpressure STG exhausting to process al 50 psig. The net output is 1.6 MW. The electric efficiency is 8.2% and the net efficiency is 39%.

The EBITDA return is -107.5%

Thermal Only Plant

The last case examined is a small thermal only planl. The boiler is the same size as the previous case. The plant efficiency Is equal lo 75%, equal to the boiler efficiency (not including lhe auxiliary electric load needed to run the plant). The EBITDA relurn for this project is -150%.

Small Thermal Plant (Heating Plant)

A small 5,000 Ib/h, 10 psig heating plant is assumed for the last case. The steam price remains at $8.50 per 1000 Ib. Assuming that lhe boiler efficiency remains al 75%, The EBITDA is 250%.

Regulatory Risk

Project financing can be at risk in an uncertain regulatory environment, Government funding and programs can be uncertain or changed. Current fédéral and State incenlives programs such as:

Production Tax Crédits

BCAP • Renewable Portfolio Standards (RPS) • Accelerated dépréciation

- Grants dramatically affect the market and project development. In today's capital markets, there is scarce private capital beyond the developers own seed capital, making it a difficult environment in which to start and fund a new project™.

Comparisons are often made with European markets and biomass utilization. In addition to lhe différences described above, the absence of caibon credit/tax market is significant. To develop a European model one should expect:

1. Development of district heating/cooling market through required connection to an urban district energy system. Forcing heating users to connect to the district energy system and mandating equipment design forheqting (and cooling).

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2. Equivalent power pricing. A table of power pricing in Europe is shown in Table 5 2’.

3. Carbon subsides

4. Feed in Tariffs

The mix of renewables in Europe has dramatically shifted to biomass as shown in Table 2.

Table 2

European Union Renewable Energy Production

Ranking: Rtsource:	2007:	2006:	2005:	BarGraph:
1	Biomas»	65,60%	65,60%	64,60%
2	Hydre energy	21,70%	22,90%	24,00%
3	Wmd energy	6,60%	5,50%	530%
4	Geothermal energy	640%	520%	520%	8888
5	Solar energy	1,00%	020%	0,70%	8

Biomass Technology Review

Table 3 - Plant Economies Summary

	• NewCondendng New Exiradcn 3TG-New Backprassura :
:OMoription	Unit»	STG	» Proc·»· : STG to Thermal	Thermal only	Small Thermal
•Technicsi ·
’Ptanl Output :	kW		13.271.92(	1^15.62 :
'Average Annuel Steam Demand	:	. ... ...........·.....	...
				.60 :	z^iSJr.KJ		SSîi?
>SiMm Pressure ;	pei9	1K.GC	I9tit»:	CÛ.&3:	SCC»		10.0
iSlssm Temperelure	<F	«4.78	581.79 ·	2(6.13:	329.00		236.4
iStoarn Enthalpy	Btuflb	1,308.72	1,308 72;	1,179.54:	1,232.54		1,160 3
>Condensata Flow	IbAi		ίϊά,Φϊόϊ):	àWS’.ÈÏÎ:	îÿistftâ		.........^?·
^Condensai» Température	*	«aoc	180.00 :	160.(0:	18C.C0		tîO.O
tCûndsnesls Enlhalpy	Btullb :	14815	148.15 :	148 16 :	148.16		89 1
:=Net Energy to Process	MMBlufh '		182.20 :	22 97:	2415		2 3
•Net Energy to Process :	-ÎcW'····:.....		147,3^/1)7:	6,7® 80 :	........W		^Λ·......ëèO
(tAvallablIiiy	*		9»%c	KK>	SOftç	««
.•Fiant Heat Hâte : ^::piant EÜclency *	%	271%	15 1%:	8.2%:
•Net Plant EKclency	%	271H	88 6%:	42.6%:	750%		750
;Hmi Conaumptlon	MMBtu/h :	31514	315.14;	67.06:	36 59		3.4
>Heei Consumption	W......	të;à&’ô4_;	βέ,Μβ.όϊ:	i.9.èëOi:.	-'tWëè’		ifôôe
•Biomass Heating Value	Btuflb	&.K-C	8,3·»:	MW:	2,30)		3,4(0
•Motsiura Content :	%	MTfc	4(W{	43«;	40¾	40K
iFud Heating Value	Buj/ib	5.280 00	5.280 00:	5,280.00 :	5,280 00		5.260 0
;Hoai Consumption	Ton/h	29.84	29.64 ί	6.35:	3.47		0.33
tEfionomica

tProjecl Unit Coal	ÎSDÜcW . $	4,000
’DewIopnani (% of Capital)	%	5 0%	50%:	6.ÿ%f	50%:	5 0%
-:taalopTMnt Cost	USD	5,611.499	8,611/«:	1/2^3» :	875.XO		ικςΜ»
iÔC	%	1.5%	1.5%:	1.5%:	15%:	15
i'ÊC	USD	1.578.622	1,578,822:	354,375:	212,625		31500
•total Pro\|eci	USD	108,820,087	108,620,067 :		14,307,825		à,ïil,50ô ’
•AmuaÎ Dcbt	.....8	6,365,688 8	6,365,688: 9	1.428,969 : $	857,394		127,02
•Armai Equlty	t	8.881,834 8	8,881,834: $	2, 188,947 : 8	1,301,36(	8	162.78
•Annual Capital Cosi	$	16,027,603 8	16,027,603 : 8	3,597,937 ; 8	2,168,782	î	iiè.èt
:Stafl		23	23:	9:
Average Sattry	$	50,000 : S	50,000 : $	50,000: 5	50,00(	8	50,00
Burdens & BeneKts		130	130:	1.30 ;	ί 3C		13
•Siafl..........................	..........,.i„	1/06,000 8	1,495,000 : 8	έέί,όοο i	390,000	8	65,000
•Ctemicets & ConsumaUes	s	200,480 ' 8	200,460 : $	45,000 ί S	27,00(		4,00
Major Maintenance Fund	»	2,606,749; 8	2,506,749: $	562,500 : $	337,500	8	50.000
:Opsraiona	USD S	5^203,509 $	5,203,509:?	1,417,500; ?	989, KX		136.00

•Boiler Amid Fuel GonsumptiC MMBlu/h	2,464,554 :	2,484,554:	628,871 :	286,500		27,160
;Bdler Armai Fuel Consumptic	TotVy	235,280.	235,280:	50,084 :	27,321		2.572
Boiler Fuel Coet (AA)	USD	25.06	28.00:	25.»;	2G.K		2S.C0
:Arvtual Fuel Cott	USD	5,881,993;	5,881,993:		à&tëô	84,2»
: Annuel Coal	IBD	27,113,104	27,113,104·	6,207,025;	3,731,292	üà,tt
•A«rege Power Price	......... S	<·».·» «	1«·.ί« : $	101·»: _t	100.«	i	1«S.&
•AEC	»	ro.oo 8	20.CC : 2	Stit»: 8	χ,'.αΰ	£	20. »
•Power Price	USD/MW $	120.00 8	120.00: $	120 00: S	120 0(		120 0
•Staarn Price	U5D/1000	' S	S.S0; £	ÎSÔ ; j>	6.K		’β.»
•Armai Power Generated	MWh	187,55320	110,154 65:	12,739 11 ·
•Armai Steam Export	k lt/y .		1,103,780 00:	175,567 79:	175,567 73		17,666 77
•Armai Power Saies	»	23,706,391 68 8	13,218.557 65 : 8	1,528,693 59 ; ?		$
Armai Thermal Sales	»	! 8	9,381,960.00: $	1,492,240.70 · 8	1,492,240.70	8	149,224.0
•Annuel Sale»	è	33,706,391.88 8	22,8θά^ΐΪ6δ: *	3,020^34.29 _:T	Méià4ô.W	6	149,234.0?
Annuel Cott	: «	27,113,104.21 8	27,113,104.21 : *	6^67,034.95 ί \|	3,731,262.0:	8	523,115.5

-EBITDA	S	(3^06,71Z669 8	(4,512,585.66); S	(3^46,090.57): S	SSW	S	(373,881..
Gros· Margin		•14.4%	•20.0%:	-107.5%:	-150.0%	-250 6

149

Biomass Technology Review

Table4

Ausna €0.071 to.oâe €0061 €0044 •âjigarta €0003 •bu gala €0.077 iBigeria €0026 €0034 •Cyprus jtyprus €0 144 <0.142

NO DATA «rt *

NOQÂTÂ ; ÎCyprus ··$ ï :QBChftp joacn ftp, <0 116 €0041 €0036

tâorta'**'	eooàT	& jj: q \|i	'€'0?O78^S;	:DermerK ÏESoria	<0117 ''‘eôoæ'	î iDÏBnmàk ...... ; •’βίοϊβ'''	€0105 ; Tôoz?!
jRnland	€0120	;Rnland	€0.107	Rnlaid	NO DATA	; :Rnland	NODATA
•France	€0 136	:Rarx»	€0.117 :	:Rance	€0.068	t Ban»	€0.051
«Germany	'eozîï	: iûBcmtty	'<'α204'Ί	ÎGarmany		J ÎGMmaiy	'“«ooœ
jQ 60®	€0060	: i&eecs	€0.069 ;	•CTmco	NODATA	; :Qeaco	NODATA
:Hrçry	€0 148	:Hrxpry	€0.146 :	:Hrg»v	€0042	: H.ng»y	«0040
;lreitnd	<0.164	: jireiand	<0.153 ;	ilreiand	€0.107	; Jrelarû	€0.107
:lraly	€0260	: Jisiy	€ 0.224 *	•iisy	€0074	* JtàÎy	€0069

îlilhuarta	€0001	:Lithuanla	€0.079 :	tlilhunia	€0032	; ïLlthuarta	€0026
:U£xentxug	€0.189	: _:lLDenûourg	€0.162 ;	Luxembourg	€0.061	t tUwenibarg	€0.040
SMÏta’	'èoïos	Ί			.........noqàta'*	1 :M6ia	nomta	1

:RMand	€0140	: jMfinfl	€0.127 ·		€0048	; iftiand	€0042
:ftxiugal	€0172	: îtatugai	<0.143	•RylugÉ	<0068	; 'Rrlugai	«0062
•Rjmaria	<0130	Fcmarta	€0.114	iftmanla	€0036	i -Ftmania	«0035
:SortNa	'<0'179	: iSovsKa		£lowKa	'è'o'oie'	; iScvéMa	''èo.w
iSCTÆTia	€0132	: Sovenia	<0.113	•Savons	€0055	; :ScKenia	€0051
•Sdn	€0143	-φάΐη	€ 0.117 :	:$ein	€0063	; ^:Sân	€0053

Biomass Technology Review

Conclusions

Biomass power génération is a dispatchable power supply thaï uses waste wood to generate power. Development of any efficiency standard for Renewable Power Crédits should be carefully evaluated in light of existing technology and available power markets.

The proposed 40% minimum efficiency limit, which allows for 50% of the REC, is well above the efficiency of any of the merchant biomass based power plants currently In operation In the régional market. The only possible method of achieving lheproposed efficiency standards is by Insialllng large Industrial steam hosts, which Is highly unUkely. Flndlng a steam host, building an industrial facility, and altering the biomass power plant to deliver steam is not a reasonable proposition. It is nol expected that any of the current facilities could be upgraded in this manner, thus leading to the removal from the market of the current biomass renewable fleet currently part of theMassachusetts renewable portfolio.

For new facilities, lhe proposed requirement is equally unrealistic. The proposed 60% minimum efficiency limit for 100% RPS qualified génération does not appear lo be based on current commercialized technologies. A 60% efficiency criterion is outside of the published limils of Systems that are in pilol or research scale . Advanced biomass power génération technology will not meet even the minimum 40% criteria to receive RECs.. The net effect is that the proposed efficiency requirements will eliminate biomass as a renewable energy source for Massachusetts.

. A 60% efficiency requiremenl can only be achieved by developing new cogénération. As the thermal load is increased to meet the net efficiency requirement, the electrical output Is reduced, lowering the electric power available to obtain REC’s. The reduced incentive will adversely impact projecl économies. Moreover, such opportunities are unlikely to be pursued, given the challenges associated with siting large biomass facilities adjacent to industrial locations and issues with fuel transport in local communities, and the limited abilily ta find crédit worthy steam hosts.

That leaves smaller CHP opportunities, which hâve financial returns that are not attractive, and thermal-only applications that are both unattraclive and do not generale electricity under lhe RPS.

In summary, using a high efficiency standard for biomass power production is not reasonable, lacks économie viability, and assumes European-style markets and subsidies that are not found anywhere in the United States. The resuit of the proposed efficiency requirement will be to eliminate biomass as a ready, dispatchable, renewable energy power resource.

151

Biomass Technology Review

Référencés

225 CMR 14.00 RENEWABLE ENERGY PORTFOLIO STANDARD - CLASS t ² http://www law cornell.edu/uscode/html/uscode16/usc_sup_Ot_16_t0_46.html ³ http://bioenergy.ornl.gov/papers/misc/energy conv.html ¹¹ The Biomass Energy Foundation Press, Nov 2002, édition, T. Reed, Fig 111-4 ⁶ http://www nexterra.ca/ ¹¹ Private conversation with vendor représentative as to the state of commercializalion with respect to biomass gasification/internal combustion based génération equipment.

^I ht1p7/www.epa.gov/chp/documents/biomass_chp_catalog.pd1 ⁸ http://www.nh.gov/oep/programs/energy/documentsÆihbio-oilopportunityanalysis.pdf http://www.dynamotive.com/ ¹⁰ http://www.mainebioproducts.com ^II http ://www.whispergen. com/ ^,2 http://www.turboden.eu/en/home/index.php ¹³ http:.'/entrapicenergy.com/ ¹⁴ http://www.biomasscenter.org/pdfs/Wood-Chip-Heating-Guide.pdf ^K http://www.terc.gov/industries/electric/gen-info/qual-fac/benefits.asp ¹⁴ Form EIA-860, Annual Electric Generator Report, - Generator (Existing) File, 2008 (http://www.eia.doe.gov/cnea1/electricity/page/eia860.html) ¹⁷ Private correspondence ^ls G Willsee, Lassons Learned from existinq Biomass Power Plants, Appel Consultans. Inc. NREL Contract no. DE-AC36-99-GO10337 ” Stahl et al, biomass IGCC at Varnamo, Sweden - Past and Future. GCEP Energy Workshop, April 2004. http://gcep.stanford.edu/pdfs/energy_workshops_04_04/biomas3_stahl.pdf ²⁰ Sue Wyka, Biomass Project Financim Solutions in Today's Ditticult Capital Markets, Biomass Magazine, June 2009 ²¹ Europes Energy Portai, http://www.energy.eu/#Domes1ic

Claims

CLAIMS:

1. A method of generating energy comprising:

combusting a saccharified biomass material to produce energy.
2. The method of claim 1, wherein the saccharified biomass material includes cells.
3. The method of claims 2, wherein the cells are selected from the group

10 consisting of yeast cells, bacterial cells, fungal cells and mixtures thereof.
4. The method of any of the above claims, wherein the saccharified biomass material includes protein material.

15
5. The method of claim 4, wherein the protein material is an enzyme material.
6. The method of any one of the above claims, wherein the saccharified material includes denatured enzyme material.

20
7. The method of any one of the above claims, wherein the saccharified biomass material comprises lignocellulosic residue from lignocellulosic material that has been treated to reduce its recalcitrance prior to saccharification.
8. The method of claim 7, wherein the lignocellulosic material has been treated

25 with accelerated électrons to reduce its recalcitrance.
9. The method of claim 8, wherein the électrons hâve an average energy between about 0.3 MeV and about 5 MeV.

30
10. The method of claim 8, wherein the électrons hâve an average energy between about 0.5 MeV and about 3.5 MeV.
11. The method of claim 8, wherein the électrons hâve an average energy between 0.8 MeV and about 2 MeV.

153
12. The method of any one of claims 8 through 11, wherein the lignocellulosic biomass has been treated to a total dose between about 10 Mrad and about 100 Mrad.
13. The method of any one of claims 8 through 11, wherein the lignocellulosic biomass has been treated to a total dose between abouti 5 Mrad and about 50 Mrad.
14. The method of any one of claims 8 through 11, wherein the lignocellulosic biomass has been treated to a total dose between about 20 Mrad and about 45 Mrad.
15. The method of any one of claims 8 through 11, wherein the lignocellulosic biomass has been treated to a total dose between about 25 Mrad and about 40 Mrad.
16. The method of any one of the above claims, wherein the saccharified biomass material includes inorganic solids.
17. The method of claim 16, wherein the inorganic solids is selected from the group consisting of diatomaceous earth, celite, silica, pumice, perlite, alumina, zeolites, sand and mixtures thereof.
18. The method of any one of the above claims, wherein the saccharified biomass material includes less than 60 percent moisture.
19. The method of any one of claims 1 through 17, wherein the saccharified biomass material includes less than 50 percent moisture.
20. The method of any one of claims 1 through 17, wherein the saccharified biomass material includes less than 45 percent moisture.
21. The method of any one of claims 1 through 17, wherein the saccharified biomass material includes less than 40 percent moisture.
22. The method of any one of claims 1 through 17, wherein the saccharified biomass material includes less than 30 percent moisture.

154
23. The method of any one of the above claims, wherein saccharified biomass material includes less than 5 percent ash after combustion.
24. The method of any one of the above claims, wherein the saccharified biomass material includes less than 0.5 percent sulfur.
25. The method of any one of the above claims, wherein combustion produces greater than about 3500 BTU of energy per pound of the saccharified biomass material.
26. The method of any one of claims 1 through 24, wherein combustion produces greater than about 4000 BTU of energy per pound of the saccharified biomass material.
27. The method of any one of claims 1 through 24, wherein combustion produces greater than about 4500 BTU of energy per pound of the saccharified biomass material.
28. The method of any one of claims 1 through 24, wherein combustion produces greater than about 5000 BTU of energy per pound of the saccharified biomass material.
29. The method any one of claims 1 through 24, wherein combustion produces greater than about 6000 BTU of energy per pound of the saccharified biomass material.
30. The method of any one of claims 1 through 24, wherein combustion produces greater than about 7000 BTU of energy per pound of the saccharified biomass material.
31. The method of any one of the above claims, wherein the saccharified biomass material includes less than 35 percent by weight carbohydrates on a dry basis.
32. The method of any one of claims 1 through 30, wherein the saccharified biomass material includes less than 30 percent by weight carbohydrates on a dry basis.
33. The method of any one of claims 1 through 30, wherein the saccharified biomass material includes less than 25 percent by weight carbohydrates on a dry basis.

155
34. The method of any one of claims 1 through 30, wherein the saccharified biomass material includes less than 20 percent by weight carbohydrates on a dry basis.
35. The method of any one of claims 1 through 30, wherein the saccharified biomass material includes less than 10 percent by weight carbohydrates on a dry basis.
36. The method of any one of the above claims, wherein the energy is in the form of heat.
37. The method of any one of the above claims, wherein the energy is in the form of electrical energy.
38. The method of any one of the above claims, wherein during combustion a boiler is utilized.
39. The method of claim 38, wherein the boiler is selected from the group consisting of a stoker grate boiler, a fluidized bed boiler and a co-fired boiler.
40. The method of any of one of the above claims, wherein during combustion, a gasifier is utilized.
41. The method of claim 40, wherein the gasifier is a fixed bed or a fluidized bed gasifier.
42. The method of any one of the above claims, wherein the saccharified biomass is collected utilizing a rotary drum filter prior to combustion.
43. The method of any one of the above claims, wherein the saccharified biomass is collected utilizing a centrifuge prior to combustion.
44. A method of processing a biomass material, the method comprising;

processing a first portion of lignocellulosic material into a product and a solid residue, combusting the solid residue in a boiler to produce steam,

156 coupling the steam to a turbine to produce electricity, and using the steam and/or electric energy to process a second portion of lignocellulosic material into a product.
45. The method of claim 44, wherein processing comprises irradiating.
46. The method of claim 44 or 45, wherein processing comprises saccharifying.
47. The method of claim 46, wherein saccharifying produces glucose.
48. The method of claim 46 or 47, wherein saccharifying produces xylose.
49. The method of any one of claims 44 through 48, wherein processing comprises fermentation.
50. The method of any one of claims 44 through 49, further comprising drying the solid residue prior to combusting the sohd residue.
51. The method of claim 50, wherein drying reduces the moisture content of the solid residue to less than about 25 wt.% water.
52. The method of claim 50, wherein drying reduces the moisture content of the solid residue to less than about 20 wt.% water.
53. The method of claim 50, wherein drying reduces the moisture content of the solid residue to less than about 15 wt.% water.
54. The method of any one of claims 50 through 53, wherein the residue is dried using a screw dryer.
55. The method of any one of claims 44 through 54, further comprising combining the residue with a drying agent.
56. The method of claim 55, wherein the drying agent is a fine biomass material.

157
57. The method of claim 56, wherein the fine biomass material has a medium particle size of less than about 1mm.
58. The method of claim 56, wherein the fine biomass material has a medium particle size of less than about 500 micro meters.
59. The method of claim 56, wherein the fine biomass material has a medium particle size of less than aboutlOO micro meters.
60. The method of any one of claims 44 through 59, further comprising forming the residue into a form selected from cakes, pellets, densified shapes, powder or combinations thereof prior to combusting.
61. The method of any one of claims 44 through 60, wherein the residue, when in a dry form with less than 5 wt.% water, has an energy content of at least 4000 BTU per pound of the residue.
62. The method of any one of claims 44 through 61, wherein the residue includes at least 0.1% nitrogen in a nitrogen(III) compound.
63. The method of claim 62, wherein the nitrogen (ΙΠ) compound is selected from the group consisting of proteins, denatured proteins, protein residues, amino acids, amino acid residues, urea, ammonia and combinations thereof.
64. The method of any one of claims 44 through 63, wherein the lignocellulosic material is selected from the group consisting of wood, particle board, sawdust, agricultural waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, com cobs, com stover, switchgrass, alfalfa, hay, coconut hair, seaweed, algae, and combinations thereof.

2-1¼ ί [Ίονί