US20150361457A1 - Processing and transforming biomass - Google Patents

Processing and transforming biomass Download PDF

Info

Publication number
US20150361457A1
US20150361457A1 US14/433,217 US201414433217A US2015361457A1 US 20150361457 A1 US20150361457 A1 US 20150361457A1 US 201414433217 A US201414433217 A US 201414433217A US 2015361457 A1 US2015361457 A1 US 2015361457A1
Authority
US
United States
Prior art keywords
biomass
catalyst
acid
fermentation
less
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US14/433,217
Other languages
English (en)
Inventor
Marshall Medoff
Thomas Craig Masterman
Michael W. FINN
Andrew PAPOULIS
Natalya A. KORYABKINA
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Xyleco Inc
Original Assignee
Xyleco Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Xyleco Inc filed Critical Xyleco Inc
Priority to US14/433,217 priority Critical patent/US20150361457A1/en
Publication of US20150361457A1 publication Critical patent/US20150361457A1/en
Assigned to XYLECO, INC. reassignment XYLECO, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MEDOFF, MARSHALL, MASTERMAN, THOMAS CRAIG, FINN, MICHAEL W., KORYABKINA, Natalya A., PAPOULIS, ANDREW
Abandoned legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/081—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing particle radiation or gamma-radiation
    • B01J19/085—Electron beams only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/02—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor with moving adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/32—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by electrical effects other than those provided for in group B01D61/00
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/445—Ion-selective electrodialysis with bipolar membranes; Water splitting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
    • B65G27/00—Jigging conveyors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
    • B65G53/00—Conveying materials in bulk through troughs, pipes or tubes by floating the materials or by flow of gas, liquid or foam
    • B65G53/04—Conveying materials in bulk pneumatically through pipes or tubes; Air slides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
    • B65G53/00—Conveying materials in bulk through troughs, pipes or tubes by floating the materials or by flow of gas, liquid or foam
    • B65G53/34—Details
    • B65G53/40—Feeding or discharging devices
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
    • C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/12—Monohydroxylic acyclic alcohols containing four carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
    • C08B1/00—Preparatory treatment of cellulose for making derivatives thereof, e.g. pre-treatment, pre-soaking, activation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C10L1/023—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for spark ignition
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/10—Separation or concentration of fermentation products
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/02—Monosaccharides
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
    • C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/52—Propionic acid; Butyric acids
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/56—Lactic acid
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K13/00—Sugars not otherwise provided for in this class
    • C13K13/002—Xylose
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/001—Modification of pulp properties
    • D21C9/007—Modification of pulp properties by mechanical or physical means
    • E—FIXED CONSTRUCTIONS
    • E04—BUILDING
    • E04B—GENERAL BUILDING CONSTRUCTIONS; WALLS, e.g. PARTITIONS; ROOFS; FLOORS; CEILINGS; INSULATION OR OTHER PROTECTION OF BUILDINGS
    • E04B1/00—Constructions in general; Structures which are not restricted either to walls, e.g. partitions, or floors or ceilings or roofs
    • E04B1/62—Insulation or other protection; Elements or use of specified material therefor
    • E04B1/92—Protection against other undesired influences or dangers
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F7/00—Shielded cells or rooms
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21K—TECHNIQUES FOR HANDLING PARTICLES OR IONISING RADIATION NOT OTHERWISE PROVIDED FOR; IRRADIATION DEVICES; GAMMA RAY OR X-RAY MICROSCOPES
    • G21K5/00—Irradiation devices
    • G21K5/10—Irradiation devices with provision for relative movement of beam source and object to be irradiated
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01J—ELECTRIC DISCHARGE TUBES OR DISCHARGE LAMPS
    • H01J37/00—Discharge tubes with provision for introducing objects or material to be exposed to the discharge, e.g. for the purpose of examination or processing thereof
    • H01J37/30—Electron-beam or ion-beam tubes for localised treatment of objects
    • H01J37/317—Electron-beam or ion-beam tubes for localised treatment of objects for changing properties of the objects or for applying thin layers thereon, e.g. for ion implantation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0869—Feeding or evacuating the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0873—Materials to be treated
    • B01J2219/0879—Solid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0873—Materials to be treated
    • B01J2219/0881—Two or more materials
    • B01J2219/0886—Gas-solid
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0461—Fractions defined by their origin
    • C10L2200/0469—Renewables or materials of biological origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0461—Fractions defined by their origin
    • C10L2200/0469—Renewables or materials of biological origin
    • C10L2200/0476—Biodiesel, i.e. defined lower alkyl esters of fatty acids first generation biodiesel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/36—Applying radiation such as microwave, IR, UV
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P2201/00—Pretreatment of cellulosic or lignocellulosic material for subsequent enzymatic treatment or hydrolysis
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P2203/00—Fermentation products obtained from optionally pretreated or hydrolyzed cellulosic or lignocellulosic material as the carbon source
    • E—FIXED CONSTRUCTIONS
    • E04—BUILDING
    • E04B—GENERAL BUILDING CONSTRUCTIONS; WALLS, e.g. PARTITIONS; ROOFS; FLOORS; CEILINGS; INSULATION OR OTHER PROTECTION OF BUILDINGS
    • E04B1/00—Constructions in general; Structures which are not restricted either to walls, e.g. partitions, or floors or ceilings or roofs
    • E04B1/62—Insulation or other protection; Elements or use of specified material therefor
    • E04B1/92—Protection against other undesired influences or dangers
    • E04B2001/925—Protection against harmful electro-magnetic or radio-active radiations, e.g. X-rays
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01J—ELECTRIC DISCHARGE TUBES OR DISCHARGE LAMPS
    • H01J2237/00—Discharge tubes exposing object to beam, e.g. for analysis treatment, etching, imaging
    • H01J2237/20—Positioning, supporting, modifying or maintaining the physical state of objects being observed or treated
    • H01J2237/202—Movement
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01J—ELECTRIC DISCHARGE TUBES OR DISCHARGE LAMPS
    • H01J2237/00—Discharge tubes exposing object to beam, e.g. for analysis treatment, etching, imaging
    • H01J2237/30—Electron or ion beam tubes for processing objects
    • H01J2237/31—Processing objects on a macro-scale
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01J—ELECTRIC DISCHARGE TUBES OR DISCHARGE LAMPS
    • H01J2237/00—Discharge tubes exposing object to beam, e.g. for analysis treatment, etching, imaging
    • H01J2237/30—Electron or ion beam tubes for processing objects
    • H01J2237/31—Processing objects on a macro-scale
    • H01J2237/3165—Changing chemical properties
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/16—Mechanical energy storage, e.g. flywheels or pressurised fluids
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/33—Wastewater or sewage treatment systems using renewable energies using wind energy
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • lignocellulosic feedstocks are available today, including agricultural residues, woody biomass, municipal waste, oilseeds/cakes and sea weeds, to name a few. At present these materials are either used as animal feed, biocompost materials, burned in a co-generation facility or are landfilled.
  • Lignocellulosic biomass comprises 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 i.e., biomass material from which the lignin has been removed
  • Cellulosic biomass materials is more accessible to enzymes and other conversion processes, but even so, naturally-occurring cellulosic materials often have low yields (relative to theoretical yields) when contacted with hydrolyzing enzymes.
  • Lignocellulosic biomass is even more recalcitrant to enzyme attack.
  • each type of lignocellulosic biomass has its own specific composition of cellulose, hemicellulose and lignin.
  • this invention relates to systems, methods and processes for converting a biomass feedstock, e.g., cellulosic, starchy or lignocellulosic materials, to useful primary products, for example, alcohols, acids, esters, and sugars.
  • useful primary products for example, alcohols, acids, esters, and sugars.
  • the invention also relates to equipment, methods and systems to convert these primary products to useful secondary products, for example, converting esters by hydrogenolysis to alcohols (e.g., n-butanol, sec-butanol, iso-butanol, t-butanol, ethanol, and mixtures of any of these).
  • the invention relates to methods of making products.
  • the method includes producing one or more acids (e.g., acetic acid, n-butyric acid, iso-butyric acid) from biomass, e. g., saccharified biomass, sugars e. g., sugar in a saccharified biomass, the sugar fraction of a saccharified biomass, and converting the one or more acids into one or more esters.
  • the method further includes hydrogenating the one or more esters utilizing a catalyst and hydrogen to produce one or more products, such as alcohols.
  • the one or more acids are produced by fermentation of the saccharified biomass sugars.
  • the saccharified biomass sugars are produced by saccharification of a cellulosic or lignocellulosic biomass material with one or more enzymes and/or one or more acids, such as by first using an acid and then using the one or more enzymes.
  • the method can also further include recalcitrance reducing the cellulosic or lignocellulosic material e. g., by electron beam irradiation, e.g., delivering a dose of irradiation is between 10 and 200 Mrad to the material.
  • the catalyst can include a metal such as Pt, Pd, Re, Os, Ru, Rb, Ni, Co, Mo, W, Zn, Cr, Cu oxides of these and combinations of these.
  • a hydrogen pressure between about 5 and 120 atm. while utilizing the catalyst to produce one or more alcohols.
  • the method includes isolating at least one of the carboxylic acids (e.g., butyric acid) prior to converting the one or more acids into one or more esters (e.g., ethyl butyrate).
  • the method can be used to produce esters including ethyl butyrate, butyl butyrate, hexyl butyrate, and octyl butyrate.
  • the alcohol portion of the ester maybe derived from biomass processing or by petrochemical processing.
  • the carboxylic acid and alcohol can be reacted by known chemical processes to obtain the ester.
  • Another aspect of the invention features a method for making a product including converting the product of the fermentation of a saccharified treated lignocellulosic material to an ester, and producing an alcohol by passing the ester over a first catalyst e. g., a catalyst in the presence of hydrogen.
  • the method can further include passing the ester over a second catalyst e. g., a catalyst.
  • the first and the second catalysts can be different kinds of catalysts, for example they can have different compositions (e.g., including supports such as silica and Al 2 O 3 ). Alternatively, the first and second catalyst can be the same kind of catalysts.
  • the method includes applying a first pressure of hydrogen while passing the ester over the first catalyst and applying a second pressure of hydrogen while passing the ester over the second catalyst, wherein the first pressure is higher than the second pressure by at least 0.5 atm.
  • the method can further include heating the first catalyst to a first temperature while passing the ester over the first catalyst and heating the second catalyst to a second temperature while passing the ester over the second catalyst, wherein the first temperature is higher than the second temperature by at least 10° C.
  • the temperature of the second reactor can be higher than the first and the pressure can be increased between the two reactors.
  • the first and second catalysts can include metals in their compositions that include Pt, Pd, Re, Os, Ru, Rb, Ni, Co, Mo, W, Zn, Cr, Cu, oxides of these and combinations of these.
  • the method can include applying a hydrogen pressure between about 5 and 120 atm.
  • the first and/or second catalyst is classified as a reforming catalyst.
  • the product of the fermentation comprises a carboxylic acid.
  • the carboxylic acid can have from 1 to 20 carbons and 1 to 5 carboxylic acid group (e.g., butyric acid, aspartic acid).
  • the product of the fermentation comprises an alcohol.
  • the ester can be, for example, ethyl butyrate, propyl butyrate, butyl butyrate, hexyl butyrate and octyl butyrate and the isomers of the alcohol and the carboxylic acid portion of the ester. That is, butyric acid and butyrate esters can refer to both the normal (n-) and iso isomer.
  • the method can further include fermenting the biomass to at least two products and converting comprises condensing the products to the ester.
  • converting comprises condensing the products to the ester.
  • butyric acid and butanol can be converted to the butyl butyrate and then in turn hydrogenated to 2 moles of butanol.
  • the method includes isolating the fermentation product prior to converting the product.
  • the fermentation product can be contacted with a resin and bonding the fermentation product to the resin.
  • the fermentation product can be removed from the resin by acidifying the fermentation product and extracting the acidified product with a solvent (e.g., alcohol).
  • Some implementations of the method include producing the treated lignocellulosic material by irradiating a lignocellulosic material with an electron beam. For example, irradiation can be done to accomplish a dose of about between 10 and 150 Mrad.
  • the treated biomass is saccharified by contacting the treated biomass with an enzyme.
  • the method can include that the saccharification produces a mixture comprising glucose and xylose and that the fermenting can include fermenting the xylose.
  • the glucose can be fermented to an alcohol (e.g., selectively without fermenting the xylose), and optionally the alcohol can be distilled, prior to fermenting the xylose.
  • xylose can be added to the saccharified treated material (e.g., xylose in addition to that available from the treated saccharified material).
  • the invention in another aspect relates to a method of producing a product including fermenting a first sugar produced from the saccharification of a treated lignocellulosic material with a first organism and fermenting a second sugar produced from the saccharified treated lignocellulosic material with a second organism. Also, optionally distilling the product of the fermentation of the first sugar prior to fermenting the second sugar.
  • the first sugar can be glucose and the second sugar can be xylose.
  • the product of fermenting the first sugar is an alcohol (e.g., ethanol) and the product of fermenting the second sugar is a carboxylic acid (e.g., butyric acid).
  • the method can further include adding xylose to the saccharified material.
  • the following can be added to the saccharified material: acids, bases, buffers, amino acids, vitamins, blackstrap molasses, reinforced clostridia media, metal ions, yeast extract, meat extracts, vegetable extracts, peptones, carbon sources, proteins, Fe, Mn, Mg, Na, Cu, Zn, p-aminobenzoic acids, choline, thiamin, albumin, inositol and combinations of these.
  • the treated lignocellulosic material is produced by irradiating a lignocellulosic material with an electron beam, for example, with a dose of between about 10 and 200 Mrad.
  • the method further includes converting the product from the fermentation of the second sugar to an ester.
  • the ester can be hydrogenated to produce an alcohol.
  • the method includes extracting the product of fermenting the second sugar utilizing an alcohol which include n-hexanol, n-octanol, n-decanol, n-dodecanol, lauryl alcohol, myristyl alcohol, cetyl alcohol, stearyl alcohol, oleyl alcohol, linoleyl alcohol, isomers of these alcohols and combinations of these.
  • an alcohol which include n-hexanol, n-octanol, n-decanol, n-dodecanol, lauryl alcohol, myristyl alcohol, cetyl alcohol, stearyl alcohol, oleyl alcohol, linoleyl alcohol, isomers of these alcohols and combinations of these.
  • Some fermentations are product inhibited so that the amount of a desired fermentation product that can be produced can be limited.
  • the fermentation of sugars to n-butanol by some species of Clostridia is often limited to one or two percent because above these levels it is inhibitory or toxic to the organism. It can be challenging to remove this small amount of n-butanol from the aqueous spent fermentation broth.
  • An intermediate to n-butanol in the fermentation is butyric acid, produced in the acidogenic phase of the fermentation. Butyric acid is generally less inhibitory or less toxic to Clostridia species and thus can be accumulated in higher concentrations than butanol, e.g., 4-7%.
  • Butyric acid also can be less challenging to isolate from the fermentation broth due in part to its higher molecular weight and its partially ionic nature.
  • Butyric acid is a useful product, for example, used in the chemical, food, flavor, fragrances and pharmaceutical industries.
  • Butyric acid can also be directly hydrogenated to n-butanol.
  • butyric acid can be esterified, for example, to ethyl butyrate and this product can be hydrogenated to n-butanol and ethanol under milder conditions than the direct hydrogenation.
  • deriving products, e.g., n-butanol, from biomass as described herein does not require as many high energy catalytic steps as required in the processing of fossil fuels.
  • fossil fuels can have a high concentration of compounds that must be removed prior to or during cracking, for example sulfur compounds that must be removed by hydrodesulfurization.
  • catalysts e.g., reforming catalysts
  • lower temperatures and pressures can be utilized.
  • FIG. 1 is a diagram illustrating exemplary enzymatic hydrolysis of biomass.
  • FIG. 2 is a flow diagram showing processes for manufacturing sugar solutions from a feedstock.
  • FIG. 3 is a flow diagram showing processes for manufacturing sugar solutions from a feedstock showing a second fermentation.
  • FIG. 4 is a diagram illustrating a reaction scheme for converting a sugar to an alcohol with ethyl butyrate as the ester.
  • cellulosic and lignocellulosic feedstock materials for example that can be sourced from biomass (e.g., plant biomass, animal biomass, paper, and municipal waste biomass) and that are often readily available but difficult to process, can be turned into useful products. Included are methods and systems to produce useful primary products, for example, alcohols, acids, and sugars. The invention also relates to methods and systems to convert these primary products to useful secondary products, for example, esters and alcohols (e.g., butanol, ethanol, esters and mixtures of these).
  • biomass e.g., plant biomass, animal biomass, paper, and municipal waste biomass
  • useful primary products for example, alcohols, acids, and sugars.
  • useful secondary products for example, esters and alcohols (e.g., butanol, ethanol, esters and mixtures of these).
  • Enzymes and biomass-destroying organisms that break down biomass contain or manufacture various cellulolytic enzymes (cellulases), ligninases, xylanases, hemicellulases or various small molecule biomass-destroying metabolites.
  • FIG. 1 provides some examples of these biomass-destroying processes.
  • a cellulosic substrate is 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 water-soluble 1,4-linked dimer of glucose. Finally cellobiase cleaves cellobiose to yield glucose.
  • a xylanase e.g., hemicellulase
  • FIG. 2 shows processes for manufacturing sugars and fermentation products from a feedstock (e.g., cellulosic or lignocellulosic materials).
  • a feedstock e.g., cellulosic or lignocellulosic materials.
  • the method includes, optionally, mechanically treating a cellulosic and/or lignocellulosic feedstock. Before and/or after this treatment, the feedstock can be treated with another physical treatment ( 212 ), for example irradiation, sonication, steam explosion, oxidation, pyrolysis or combinations of these, to reduce or further reduce its recalcitrance.
  • a sugar solution e.g., including glucose, xylose and combinations of these, is formed by saccharifying the feedstock ( 214 ).
  • the saccharification can be, for example, accomplished efficiently by the addition of one or more enzymes, e.g., cellulases and xylanases ( 211 ) or one or more enzymes and one or more acids in any order.
  • the sugar solution can be bioprocessed ( 216 ), for example by utilizing an organism to ferment the sugars to a primary product, e.g., an alcohol, a carboxylic acid, a ketone, hydrogen and combinations of these.
  • the fermentation can include more than one organism and comprises more than one fermentation step, for example producing one or more product simultaneously or sequentially.
  • the fermentation can be selective to one sugar.
  • the primary product of the bioprocessing step can be chemically processed ( 224 ).
  • a carboxylic acid can be hydrogenated to an alcohol, esterified and/or esterified and then hydrogenated. Hydrogenation can occur in a batch reactor, or, in a continuous reactor.
  • the chemically processing can include isolation of the product, for example by a column extraction, solvent extraction and/or by distillation. If desired, the steps of measuring lignin content ( 218 ) and setting or adjusting process parameters based on this measurement ( 220 ) can be performed at various stages of the process, for example, as described in U.S. application Ser. No. 12/704,519, filed on Feb. 11, 2011, the complete disclosure of which is incorporated herein by reference.
  • FIG. 3 which is similar to FIG. 2 , but with a different naming scheme.
  • the mixture is fermented at step 217 such that only one of the sugars is fermented to form a first product within a mixture of at least a second (unfermented) sugar, and fermentation solids.
  • the first product at step 225 is isolated by any of the isolation means described herein.
  • the fermentation solids may be separated from at least the second (unfermented) sugar at step 232 .
  • a second fermentation process at step 227 will convert the second sugar to a second product which can be isolated by any of the isolation means described herein at step 230 .
  • first and second sugar can be glucose and xylose, respectively, with the glucose being converted in the first fermentation step.
  • the glucose can be converted to ethanol or lactic acid.
  • the first sugar can be xylose and the second sugar can be glucose.
  • the xylose fermentation product is the first product.
  • FIG. 4 shows an example of a reaction scheme for converting a sugar to an alcohol, specifically butanol.
  • a first step for example, xylose is fermented to n-butyric acid. It should be understood that the iso-butyric acid may also undergo a similar reaction scheme.
  • the butyric acid is contacted with the quaternary amine functionalized resin AmberliteTM 400. Butyrate becomes associated with the quaternary amine groups and is extracted from solution in this second step.
  • the resin and bound butyrate is contacted with a strong acid, e.g., aqueous sulfuric acid, with the effect of protonating the butyrate and forming free butyric acid.
  • a strong acid e.g., aqueous sulfuric acid
  • the butyric acid can then be extracted by ethanol or other alcohol providing butyric acid in an alcoholic solution.
  • the butyric acid and ethanol (optionally additional ethanol can be added) is contacted with an optionally catalyst and heated (e.g., to refluxing temperatures around 80 to 90° C. at atmospheric pressure) so that an esterification reaction occurs producing ethyl butyrate.
  • the ethyl butyrate is hydrogenated to butanol and ethanol utilizing hydrogen and a catalyst (e.g., Re/Al 2 O 3 ).
  • the hydrogenation step can be carried out in any reactor suited for hydrogenations.
  • the fermentation can produce a carboxylic acid, for example, as described in U.S. application Ser. No. 13/177827 filed on Jul. 7, 2011 and U.S. application Ser. No. 13/668358 filed on Nov. 5, 2012, the entire disclosure of which are incorporated herein by reference.
  • the carboxylic acid can be, for example any carboxylic acid with between 1 to 20 carbons and 1 to 5 carboxylic acid (—CO 2 H) groups (e.g., 1 to 10 carbons and 1 to 4 carboxylic acid groups, 1 to 5 carbons and 1 to 3 carboxylic acid groups).
  • carboxylic acids that can be utilized in the methods described herein are acetic acid, propionic acid, tartaric acid, malonic acid, succinic acid, glutaric acid, adipic acid, benzoic acid, phthalic acid, maleic acid, gluconic acid, traumatic acid, muconic acid, butyric acid (e.g., n-butyric acid, isobutyric acid), valeric acid, caproic acid, lauric acid, palmitic acid, stearic acid and arachidic acid.
  • Sugars from biomass can include one or more sugars.
  • some fermenting species can consume more than one sugar simultaneously or sequentially.
  • Some fermenting species prefer one sugar.
  • some organisms may prefer the fermentation of fructose as described in PCT application No. PCT/US12/71097 filed Dec. 20, 2012, designating the US and published in English.
  • the sugar solution can be processed prior to any fermentation step.
  • a saccharified solution as prepared by the methods described herein can be purified and/or processed by filtration (e.g., including rotary vacuum drum filtration), chromatography (e.g., simulated moving bed chromatography), electrodialysis including bipolar electrodialysis, crystallization and combinations of these.
  • processing can include fermenting one sugar in a mixture of two sugars and removal of the fermentation product, leaving a sugar solution of substantially the second sugar which can be more easily utilized, for example isolated and/or fermented (e.g. to a carboxylic acid).
  • a biomass source can provide a higher amount of essentially only one sugar, for example some paper products, cotton and other biomass that is almost entirely a glucose source with little if any xylose.
  • Other biomass sources may provide mostly xylose and/or lignin.
  • Some suitable microorganisms to produce butyrate can include C. saccharobutylacetonicum, C. saccharoperbutylacetonicum, C. saccharobutylicum, C. Puniceum, C. beijernckii, C. acetobutylicum, C. acetobutylicum, C. roseum, C. aurantibutyricum, C. felsineum and C. tyrobutyricum .
  • additives during fermentation for example acids, bases, buffers, amino acids, vitamins, blackstrap molasses, reinforced clostridia media (RCM), metal ions, yeast extract, distillate bottoms, meat extracts, vegetable extracts, peptones, carbon sources and proteins.
  • RCM reinforced clostridia media
  • metal ions for example the addition of metal ions of Fe, Mn, Mg, Na, Cu, Zn and combinations of these can be beneficial.
  • Other additives for example, p-aminobenzoic acids, choline, inositol, thiamin, and albumin can be beneficial.
  • a preferred additive that can be utilized is the distillate bottom from a fermented saccharified lignocellulosic or cellulosic material (e.g., biomass).
  • a fermented saccharified lignocellulosic or cellulosic material e.g., biomass
  • yeast fermentation of a saccharified material as described herein producing ethanol can be distilled to produce a distillation bottom.
  • the distillate bottom containing yeast cells and spent biomass e.g., lignin, non-fermented sugars, proteins
  • the distillate bottom can be optionally purified prior to use, for example, by methods described herein (e.g., rotary vacuum drum filters, simulated moving bed chromatography and improvements to simulated moving bed chromatography, filtration, precipitation).
  • the concentration of solids can be at least about 5 wt. % (e.g., at least about 10 wt. %, at least about 20 wt. %, 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. %, between about 10 and 90 wt. %, between about 20 and 60 wt. %).
  • the distillate bottom be used directly in the distillation or it can be diluted with a solvent (e.g., water) and used as at least 5 wt.
  • distillate bottom to solvent e.g., at least 10 wt. %, at least 20 wt. %, at least 30 wt. %, at least 40 wt. %, between about 10 and 80 wt. %, between about 10 and 60 wt. %, between about 10 and 50 wt. %, between about 20 and 50 wt. %, between about 20 and 40 wt. %).
  • the distillation bottom additive can be used in combination with other additive as herein described and additional sugars (e.g., glucose and/or xylose).
  • the pH of the fermentation media can be an important parameter to control.
  • Buffers for example, phosphate, sulfate and acetate buffers can help maintain a target pH.
  • Addition of acids and bases e. g., ammonium hydroxide, sodium and potassium hydroxides, acetic acid, sulfuric acid, phosphoric acid, nitric acids
  • the pH is optimally between about 2 and 8 (e.g., between about 3 and 8, between about 4 and 8, between about 4 and 7).
  • Maintaining the pH above a critical value, for example above about 3 (e.g., above about 3.5, above about 4) by the addition of a base can often improve the fermentation. This control can be particularly important while using acidogenic bacteria since the acid products can lower the pH during the fermentation to values that are toxic to the organisms.
  • the temperature can also be a controlling and important parameter during fermentation. Optimally the temperature is maintained between about 20 and 50° C. (e.g., between about 20 and 40° C., between about 30 and 40° C.). In some instances lower or higher temperatures from an optimal temperature can be utilized to induce a desired fermentation phase, e.g., acidogenisis, solventogenisis, log growth, sporulation.
  • a desired fermentation phase e.g., acidogenisisis, solventogenisis, log growth, sporulation.
  • the fermentation in the absence of oxygen e.g., under a blanket of an inert gas such as N 2 , Ar, He, CO 2 or mixtures thereof.
  • an inert gas such as N 2 , Ar, He, CO 2 or mixtures thereof.
  • the mixture may have a constant purge of an inert gas flowing through the tank or bioreactor during part of or all of the fermentation.
  • the fermenting or saccharifying organism can be immobilized on a support.
  • a support For example an application of this process is described in U.S. Pat. No. 5,563,069.
  • the organism can be supported on a cellulosic or lignocellulosic material as describe in U.S. patent Ser. No. 12/782,543 the entire disclosure of which is herein incorporated by reference.
  • the product of fermentation can be removed from the fermentation media by any useful means.
  • butyric acid and other fermentation products can be removed/purified by adding base to the fermentation solution, adding acid to the fermented solution, extraction, filtration, centrifugation, distillation, cross flow filtration, membrane filtration, pertraction, electrodialysis, adsorption and/or bonding to a resin or other solid, and combinations of these methods.
  • the product can be dried, for example by contacting the product with molecular sieves or other drying agents (e.g., sodium sulfate, magnesium sulfate).
  • organic acids e.g., butyric acid
  • adsorption/adduct formation/bonding to on a solid support, for example a resin, solid and/or polymer support.
  • the fermented product can be extracted directly from the fermentation solution or from a solution that has been distilled.
  • the extracting solvent can be, for example, an alcohol, an ether, an oil (e.g., castor oil, coconut oil, palm oil).
  • carboxylic acid e.g., butyric acid
  • some particularly useful alcohols are fatty alcohols, for example, having between 6 and 20 carbons and 1 to 5 alcoholic functional groups (e.g., n-hexanol, n-octanol, n-decanol, n-dodecanol, lauryl alcohol, myristyl alcohol, cetyl alcohol, stearyl alcohol, oleyl alcohol, linoleyl alcohol, isomers of these and combinations of these).
  • the acid can be protonated by treating the solution containing the acid with a mineral acid to adjust the pH to about pH 3 (e.g., between about pH 2 and 4) prior to extraction.
  • the acid can be esterified as discussed herein to the ester.
  • the alcohols listed herein can be also utilized to esterify the fermentation derived acid.
  • the esterification can be done in the extraction solution.
  • an alcohol can be added to the extracting solvent. If the extracting solvent is an alcohol then the alcohol can be directly utilized for esterification with or without concentration or dilution of the alcohol.
  • butyric acid derived from the fermentation of a biomass can be protonated by the addition of sulfuric acid to the fermented solution. The butyric acid can be subsequently distilled away from the acidified solution.
  • the distillate can then be extracted in an alcohol (e.g., n-octanol).
  • An acid catalyst can be added to the extracted acid and alcohol and the solution heated to produce an ester.
  • fermented solution can be acidified and then directly extracted with an alcohol (e.g., octanol). The mixture can then be esterified.
  • the resins utilized to adsorb organic acids can be polymers with ion exchange properties, for example having quaternary amine functional groups that can ion exchange with the acidic proton of the acid.
  • organic acids e.g., butyric acid
  • a solution containing the organic acid can be contacted with the ion exchange resin by passing the solution through a packed column (e.g., glass, metal, plastic) of the resin.
  • the solution containing the organic acid can be combined with the resin in a vessel (e.g., in a batch mode) and agitated (e.g., shaken, stirred) for several minutes to several hours (e.g., 1 min to 24 hours, 1 min to 12 hours, 1 min to 8 hours, 1 min to 4 hours, 1 min to 1 hour, 1 hour to 4 hours, 1 hour to 12 hours).
  • agitated e.g., shaken, stirred
  • the organic acid depleted solution can be decanted or filtered from the resin after a sufficient time to adsorb/bond at least some of the organic acid.
  • the amount of butyric acid in the batch separation or column separation methods can be monitored by any useful method, for example, head space analysis, titrations and HPLC.
  • a resin for adsorbing an organic acid can be contacted with the fermenting solution while the fermentation is still processing or after the fermentation is complete.
  • the active fermentation media can be pumped through a column of the resin or the resin can be added to the fermentation broth.
  • the organic acid can, for example, be removed from the resin by contacting the resin and bound organic acid with an acid solution.
  • the acid solution can include a mineral acid (e.g., hydrochloric, sulfuric, phosphoric, nitric) or the acid can be an organic acid (acetic acid, trifluoroacetic acid).
  • a mineral acid e.g., hydrochloric, sulfuric, phosphoric, nitric
  • the acid can be an organic acid (acetic acid, trifluoroacetic acid).
  • acetic acid acetic acid, trifluoroacetic acid
  • the pH of the solution after acidification is optimally between about 1 and 6 (e.g., between about 2 and 5, between about 2 and 4).
  • the solvent can be an alcohol (e.g., methanol, ethanol, propanol, butanol or the fatty acid alcohols previously described), an ether (e.g., diethyl ether, tetrahydrofuran, methyl tert-butyl ether, di-isopropyl ether), acetonitrile, acetone, butyl acetate, dimethylformamide, ethyl acetate and combinations of these. These can be combined in any percentage with water and each other.
  • an alcohol e.g., methanol, ethanol, propanol, butanol or the fatty acid alcohols previously described
  • an ether e.g., diethyl ether, tetrahydrofuran, methyl tert-butyl ether, di-isopropyl ether
  • acetonitrile acetone
  • butyl acetate dimethylformamide
  • ethyl acetate dimethylformamide
  • a preferred method of removing adsorbed organic acid from a resin packed column is elution with acidified alcohol (e.g. ethanol and/or methanol with and added acid) or an acidified alcohol/water solution (e.g., ethanol/water, methanol/water with and added acid). Resins can be recycled after removal of the acid, for example by flushing with excess of the acidified solution followed by flushing with water, optionally deionized water.
  • acidified alcohol e.g. ethanol and/or methanol with and added acid
  • an acidified alcohol/water solution e.g., ethanol/water, methanol/water with and added acid
  • the acidified eluent/extracting solution from the resin processing containing the carboxylic acid can be neutralized by addition of a base. This can produce the salt of the carboxylic acid.
  • the salts of the carboxylic acid can be evaporated to dryness and then oven dried (e.g. at 80 to 100° C.). The salts can be subsequently utilized in esterification reactions, with optionally re-acidification prior to the reaction.
  • the acidic proton of the organic acid can be removed by ion exchange with a cation to form the salt of an organic acid.
  • Some useful exchanging ions include, for example, quaternary ammonium ions, alkali metal ions and alkali earth metal ions, transition metal ion and combinations of these.
  • the salt of the carboxylic acid thus produced can be further processed as previously discussed.
  • esters as discussed herein from carboxylic acids can be done by utilizing any alcohol, for example, alcohols containing 1 to 20 carbon atoms and 1 to 5 alcohol groups (e.g., 1 to 10 carbon atoms and 1-4 alcohol groups, 1 to 10 carbon atoms and 1-2 alcohol groups).
  • alcohols containing 1 to 20 carbon atoms and 1 to 5 alcohol groups e.g., 1 to 10 carbon atoms and 1-4 alcohol groups, 1 to 10 carbon atoms and 1-2 alcohol groups.
  • Some exemplary alcohols are methanol, ethanol, propanol, n-butanol, n-hexanol, n-octanol, n-decanol, n-dodecanol, lauryl alcohol, myristyl alcohol, cetyl alcohol, stearyl alcohol, oleyl alcohol, linoleyl alcohol, diols (e.g., ethylene glycol), triols (e.g., glycerol), polyols, isomers of these and combinations of these. Esterification can be done with an excess of the alcohol, for example in a molar ratio of between about 1 to 50, with or without a diluting solvent.
  • the esterification reaction can be carried out at temperatures between about 80 and 300° C. (e.g., between about 80 and 200° C., between about 80 and 150° C.) and under pressures of between about 1 to 30 atm. (e.g. between about 1 and 20 atm., between about 1 and 10 atm.).
  • the alcohol that is utilized includes alcohol that is derived from the fermentation of saccharified lignocellulosic or cellulosic feeds, for example, as described herein, ethanol and or butanol can be utilized.
  • the alcohol can also be derived from other renewable sugar sources and methods, for example the sources can include, starch and sugars from corn kernels, sugar cane, fruits, legumes and/or beets. Ethanol and butanol are particularly useful alcohols that can be generated by the method described herein.
  • the alcohol may also be obtained from hydrocarbon sources.
  • the esterification reaction is facilitated by utilizing a catalyst, e.g., an acid catalyst.
  • the acid catalyst can be homogeneous or heterogeneous. Some useful homogeneous acid catalysts include sulfuric, phosphoric, nitric, hydrochloric and trifluoroacetic acid. Heterogeneous acid catalysts include resins or functionalized polymers, for example, sulfonated polystyrene resins.
  • the acids can be solid catalysts e.g., as zeolites, sulfonated carbons, alumina, clays, aluminosilicates, heteropolyacids, silica and combinations of these.
  • Dehydrating agents e.g., molecular sieves can be used in addition to the catalysts or after the esterification to remove water formed during the esterification.
  • Other methods for example distillation as a low-boiling azeotrope with toluene can be used to remove water.
  • an acid e.g., butyric acid
  • a resins utilized to adsorb organic acids can then be extracted into a solvent, for example, the solvents previously discussed for removing the protonated acid from a resin.
  • esters can be prepared utilizing an organism.
  • Staphylococci can be combined with carboxylic acids (e.g., butyric acid) and alcohols (e.g., ethyl alcohol) to produce ethyl butyrate.
  • carboxylic acids e.g., butyric acid
  • alcohols e.g., ethyl alcohol
  • esters that can be formed from acids and alcohols derived from sugars by organisms (e.g., S.
  • cerevisiae include isoamyl acetate, ethyl caproate, ethyl caprylate, ethyl caproate, phenylethyl acetate, ethyl laurate, ethyl myristate, and ethyl palmitate.
  • the ester can be separated from excess alcohol, unreacted acid and impurities by any useful method. For example distillation, chromatography, filtration can be useful. If there is any excess acid it can also be removed by passing over/through ion exchange material, for example as previously described.
  • the ester can also be simply utilized as a mixture, mostly of excess alcohol, for example as a direct fuel or fuel additive, e.g., distributed to reformulators, for high octane fuel and/or fuel additive.
  • Other uses as a mixture to the chemical, food, flavor, fragrances and pharmaceutical industries are evident to those skilled in the art.
  • the organic acids produced by the methods herein described can be hydrogenated directly to an alcohol.
  • direct hydrogenation requires very high pressures and the catalysts are often quickly deactivated.
  • the esterification is advantageous in allowing more mild conditions to be utilized for a hydrogenolysis.
  • direct hydrogenation can require pressures in excess of 100 atm., temperatures above 300° C. and catalysts lifetimes of only a few hours before the catalysts need to be regenerated or replaced.
  • the hydrogenolysis of esters can be done at temperatures between about 100 to 300° C. (e.g., 120 to 250° C., 150 to 300° C.), hydrogen pressures less than about 120 atm.
  • catalysts can last for at least an hour (e.g., at least two hours, at least 5 hours, at least 8 hours, at least 16 hours, more than a day, two days, a week, a month, a year) before needing to be regenerated and/or replaced.
  • hour e.g., at least two hours, at least 5 hours, at least 8 hours, at least 16 hours, more than a day, two days, a week, a month, a year
  • the conversion can be expressed as a percentage of the product reacted (e.g., initial product/final product times 100%).
  • the conversion can also be expressed as the rate of consumption of the staring material (e.g., the ester).
  • the selectivity is a measure of the amount of the desired product that is obtained, in comparison to unwanted products (e.g., side products, decomposition products).
  • the selectivity can be expressed as a percentage, for example a percent purity, or as a rate of formation of a desired product vs. the rate of formation of undesired products (or the rate of formation of desired product to the rate of consumption of the starting material).
  • Some unwanted products can be partial reduction products, oligomers and/or thermal decomposition products. Although not always the case, it is often found that there is an inverse relation between the conversion rates and selectivity, so that it can be difficult to drive the reaction quickly to completion with a high selectivity.
  • Catalysts are utilized during the hydrogenolysis.
  • Catalysts can include the metals Pd, Pt, Os, Ru, Rb, Re, Ir, Rh, Ni, Co, Mo, W, Cu, Zn, Cr, oxides of these and combinations of these.
  • promoter or moderators species are added/combined including Cr, Mn, Pb, Zn, Cd, Ag, Ba, Ca, Mg, Sn, Ni, Co, U, As and Ge oxides of these and combinations of these.
  • One or more catalyst and one or more promoter can be combined in any concentration and ratio. The promoters increase the performance of the catalyst, for example increasing the conversion and selectivity.
  • the catalysts and promoters can be used as bulk catalysts (e.g., not on a support).
  • Bulk catalysts can be formed into shapes to increase surface area and allow flow of reactants over its surface. For example in the form of: wool, a mesh, a grid, a wire, a perforated solid with channels, a sponge, beads and/or a powder.
  • the catalysts and promoters can be mixed when utilized in bulk, for example powers of one or more catalyst and powders of one or more promoters can be combined/mixed.
  • the metals or metal with promoter species can be advantageously adsorbed and or bonded onto a support.
  • the support can be, for example, alumina, silica, aluminosilicates, clays, zeolites (e.g., USY and beta zeolite) or other inorganic materials.
  • the supported catalysts typically have between about 0.1 wt. % and 10 wt. % of each metal (e.g., between 0.1 and 1 wt. %), although higher amounts can be used.
  • One or more metal and one or more promoter can be combined with one or more support in all combinations. These supported catalyst may be formed into any convenient form.
  • the catalysts can be homogeneous catalysts, for example tris(triphenylphosphine)rhodium(I) chloride, and similar catalysts wherein the metal is complexed with stabilizing ligand(s) (e.g., amines, phosphines, alcohols, ethers, ketones, carboxylates, acetylacetonates, optionally bis, tri or tetrakis chelating ligands, combinations of these).
  • the catalyst can be the polymer supported analog of a homogeneous catalyst, for example, wherein the ligands are attached to a polymer, e.g., functionalized polystyrenes wherein the functional groups are the ligands previously mentioned.
  • Supported catalysts can be prepared by any useful means, for example, by using the incipient wetness method, a decomposition precipitation method, a solution self-assembly method, and/or by vapor phase deposition/decomposition.
  • a desired metal precursor can be dissolved or suspended in a volume of solvent similar to the pore volume of the support and it is combined with the support.
  • the catalyst can be activated. Activation can include removal of the solvent under vacuum, calcination, for example in the presence of oxygen, nitrogen, hydrogen or other gasses, in any order and repeatedly.
  • the catalysts can be added before the promoter, with the promoter, after the promoter or in combinations of addition steps.
  • the supported catalysts can be formed into beads, or extruded into rods and other shapes. Often these are combined with binders (e.g., inert ceramic material, porous binders).
  • Catalysts can be utilized for hydrogenolysis in a batch mode.
  • the ester is combined, often with a solvent, in a vessel (e.g., a ParrTM reactor).
  • the vessel can be sparged with hydrogen and/or pressurized with hydrogen.
  • the vessels can be equipped with heaters, (e.g., heating jackets) and agitators (e.g., propellers, impellers).
  • the catalysts can also be utilized in a fluidized bed reactor. These require a high gas flow rate, e.g., of an inert gas (e.g., nitrogen, He, Ar) in addition to hydrogen and the ester.
  • the catalyst is fluidized by the rapid flow of gases through the reactor.
  • One or more catalysts can be utilized sequentially or in combination (e.g., mixed together).
  • a loop reactor may be used as it is a design option of a batch reactor, except the liquid in the vessel is recirculated outside of the reactor.
  • the catalysts can be utilized under different reaction conditions, e.g., temperatures, pressures (e.g., hydrogen pressures) and/or agitation (e.g., stirring rates). These combinations can, for example, optimize throughputs and combined conversion/selectivity.
  • the catalysts are utilized in a fixed bed flow reactors (e.g., a flow reactor, packed bed reactor, trickle bed reactor). These reactors are configured as a column packed with the catalysts (e.g., bulk or supported catalyst) through which the reactants (e.g., esters and hydrogen) are flowed.
  • the columns can be heated, for example, by a heating jacket charged with a heating fluid (e.g., water, high pressure water, oil), steam, electric heaters (e.g., resistive heating), or any other heating means.
  • the columns can also be designed to withstand high pressures e.g., at least about 50 psi, at least about 100 psi, at least about 150 psi, at least about 200 psi, at least about 300 psi, at least about 500 psi.
  • the columns can also be equipped with safety equipment e.g., pressure release valves, and high temperature process shut off (e.g., flow shut off, venting).
  • two or more fixed bed reactors can be utilized in series for one flow stream of reactants (e.g., up to 20, up to 10, 2 to 5, 3 to 10, 1 to 3). In some optional configurations some of the reactors are by-passed, for example, to keep them as a backup.
  • Having available backups is particularly useful to avoid down time when one or more of the flow reactors are not operating within acceptable parameters e.g., if catalysts in the reactor are deactivated.
  • Another advantage of utilizing reactors in series is that the reactors can be charged with different catalysts, for example having different selectivity and conversion rates, for optimal throughputs and combined conversion/selectivity.
  • the columns can also be run under different conditions, e.g., flow rates, pressures and temperatures. For example two or more columns can be utilized wherein the difference in temperatures can be about 0 to 10° C. (e.g., about 10 to 200° C., about 50 to 200° C., about 50 to 150° C., about 50 to 100° C.).
  • the difference in pressure when using at least more than one column, can be between about 0 to 5 atm. (e.g. between about 5 and 50 atm., between about 10 and 50 atm., between about 30 and 50 atm.).
  • the hydrogenolysis catalysts as described can be recycled/regenerated.
  • the catalysts are oxidized by heating to high temperature in an oxidizing environment (e.g., in the presence of oxygen) e.g., between about 200 and 800° C. (e.g., 400 to 600° C.).
  • an inert gas e.g., nitrogen, argon, helium
  • the reducing agent for example, can be hydrogen gas made to flow over the catalyst.
  • the hydrogen that is utilized in the processes described herein can be supplied by biogas, for example from the anaerobic digestion of biomass, e.g., treated biomass as described herein.
  • the hydrogen may be cleaned prior to its use for hydrogenation. Contaminants such as carbon monoxide, should be removed.
  • Other sources of hydrogen include locating the hydrogenolysis reactor system close to a hydrogen source, including a pipeline and steam reformer of methane, natural gas or the like.
  • overall selectivity of greater than about 90% can be achieved (e.g., greater than 95%, greater than 98%, greater than 99%) can be achieved.
  • the overall conversion rates are above 80% (e.g., greater than about 90%, greater than about 95%, greater than about 99%).
  • the alcohols produced by the hydrogenolysis can be separated, for example, by distillation if the boiling point is different enough.
  • the hydrogenolysis product of ethyl butyrate, ethanol and butanol can be separated by distillation.
  • the ethanol that is recovered can be re-used for esterification.
  • the mixture of alcohols can even be utilized without separation, for example as a direct fuel or fuel additive.
  • Other uses as a mixture or purified separated products applicable to the chemical, food, flavor, fragrances and pharmaceutical industries will be recognized by those skilled in the art.
  • the hydrogenolysis product is butanol and separation schemes can be used to improve impurities.
  • the feedstock can be treated with electron bombardment 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.
  • Electron bombardment via an electron beam is generally preferred, because it provides very high throughput.
  • Electron beam accelerators are available, for example, from IBA, Belgium, and NHV Corporation, Japan.
  • Electron bombardment may be performed using an electron 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.
  • the nominal energy is about 500 to 800 keV.
  • the electron beam may have a relatively high total beam power (the combined beam power of all accelerating heads, or, if multiple accelerators are used, of all accelerators and all 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 electron beam has a beam power of 1200 kW or more, e.g., 1400, 1600, 1800, or even 3000 kW.
  • the electron 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 temperature rise in the material, thereby preventing burning of the material, and also increases the uniformity of the dose through the thickness of the layer of material.
  • the bed of biomass material has a relatively uniform thickness.
  • 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).
  • the material can be cooled while it is conveyed, for example by a screw extruder, vibratory conveyor or other conveying equipment.
  • cooling while conveying is described in U.S. Provisional Patent Application Nos. 61/774,735, and 61/774,752 the entire description therein is herein incorporated by reference.
  • 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.
  • 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.
  • target e.g., the desired
  • Higher dose rates generally require higher line speeds, to avoid thermal decomposition of the material.
  • 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 corn cob material with a bulk density of 0.5 g/cm 3 ).
  • electron 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.
  • 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.
  • a total dose of 25 to 35 Mrad is preferred, applied ideally over a couple of seconds, e.g., at 5 Mrad/pass with each pass being applied for about one second.
  • Cooling can be applied before, after, or during irradiation.
  • the cooling methods, systems and equipment as described in the following applications can be utilized: U.S. Provisional Application No. 61/774,735, and U.S. Provisional Application No. 61/774,754, the entire disclosures of which are herein incorporated by reference.
  • 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.
  • 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.
  • 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.
  • electrons 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 the speed of light.
  • 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.
  • the cellulosic and/or lignocellulosic material has less than about 25 wt. % 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.
  • two or more electron sources are used, such as two or more ionizing sources.
  • samples can be treated, in any order, with a beam of electrons, followed by gamma radiation and UV light having wavelengths from about 100 nm to about 280 nm.
  • samples are treated with three ionizing radiation sources, such as a beam of electrons, gamma radiation, and energetic UV light.
  • the biomass is conveyed through the treatment zone where it can be bombarded with electrons.
  • a conveyor can be used which includes a circular system where the biomass is conveyed multiple times through the various processes described above.
  • multiple treatment devices e.g., electron beam generators
  • a single electron 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 conveyors can be made of corrosion resistant materials.
  • the conveyors can utilize structural materials that include stainless steel (e.g., 304, 316 stainless steel, HASTELLOY® ALLOYS and INCONEL® Alloys).
  • HASTELLOY® Corrosion-Resistant alloys from Hynes such as HASTELLOY® B-3® ALLOY, HASTELLOY® HYBRID-BC1® ALLOY, HASTELLOY® C-4 ALLOY, HASTELLOY® C-22® ALLOY, HASTELLOY® C-22115® ALLOY, HASTELLOY® C-276 ALLOY, HASTELLOY® C-2000® ALLOY, HASTELLOY® G-30® ALLOY, HASTELLOY® G-35® ALLOY, HASTELLOY® N ALLOY and HASTELLOY® ULTIMET® alloy.
  • Hynes such as HASTELLOY® B-3® ALLOY, HASTELLOY® HYBRID-BC1® ALLOY, HASTELLOY® C-4 ALLOY, HASTELLOY® C-22® ALLOY, HASTELLOY® C-22115® ALLOY, HASTELLOY® C-2
  • the vibratory conveyors can include non-stick release coatings, for example TEFLONTM (DuPont, Delaware, USA).
  • the vibratory conveyors can also include corrosion resistant coatings.
  • coatings that can be supplied from Metal Coatings Corp (Houston, Tex., USA) and others such as Fluoropolymer, XYLAN®, Molybdenum Disulfide, Epoxy Phenolic, Phosphate-ferrous metal coating, Polyurethane-high gloss topcoat for epoxy, inorganic zinc, Poly Tetrafluoroethylene, PPS/RYTON®, fluorinated ethylene propylene, PVDF/DYKOR®, ECTFE/HALAR® and Ceramic Epoxy Coating.
  • the coatings can improve resistance to process gases (e.g., ozone), chemical corrosion, pitting corrosion, galling corrosion and oxidation.
  • the effectiveness in changing the molecular/supermolecular structure and/or reducing the recalcitrance of the carbohydrate-containing biomass depends on the electron energy used and the dose applied, while exposure time depends on the power and dose.
  • the dose rate and total dose are adjusted so as not to destroy (e.g., char or burn) the biomass material.
  • the carbohydrates should not be damaged in the processing so that they can be released from the biomass intact, e.g. as monomeric sugars.
  • the treatment (with any electron 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.
  • the treatment is performed until the material receives a dose of between 0.1-100 Mrad, 1-200, 5-200, 10-200, 5-150, 50-150 Mrad, 5-100, 5-50, 5-40, 10-50, 10-75, 15-50, 20-35 Mrad.
  • the invention can include processing the material in a vault and/or bunker that is constructed using radiation opaque materials.
  • 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 attenuation length of the materials used, which will determine the required thickness for a particular material, blend of materials, or layered structure.
  • materials containing a high compositional percentage (e.g., density) of elements that have a high Z value (atomic number) have a shorter radiation attenuation length and thus if such materials are used a thinner, lighter shielding can be provided.
  • 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%.
  • the halving thickness is about 15.1 mm for concrete and about 0.27 mm for lead, while with an X-ray energy of 1 MeV the halving thickness for concrete 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.
  • the material chosen should have a sufficient Z value and/or attenuation length so that its halving length is less than or equal to the desired wall thickness of the enclosure.
  • 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 resistance, etc.).
  • 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 elements.
  • the radiation opaque materials can be interlocking blocks, for example, lead and/or concrete blocks can be supplied by NELCO Worldwide (Burlington, Mass.), and reconfigurable vaults can be utilized as described in U.S. Provisional Application No. 61/774,744.
  • a radiation opaque material can reduce the radiation passing through a structure (e.g., a wall, door, ceiling, enclosure, a series 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), concrete, dirt, sand and combinations thereof. Radiation opaque materials can include a barrier in the direction of the incident radiation of at least about 1 mm (e.g., 5 mm, 10 mm, 5 cm, 10 cm, 100 cm, 1 m, 10 m).
  • the type of radiation determines 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, selenium, sodium, thallium, and xenon.
  • radioactive nuclei such as isotopes of cobalt, calcium, technetium, chromium, gallium, indium, iodine, iron, krypton, samarium, selenium, sodium, thallium, and xenon.
  • Sources of X-rays include electron beam collision with metal 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 nucleus of a helium 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, americium, and plutonium.
  • various radioactive nuclei such as isotopes of bismuth, polonium, astatine, radon, francium, radium, several actinides, such as actinium, thorium, uranium, neptunium, curium, californium, americium, 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 can be DC (e.g., electrostatic DC or electrodynamic DC), RF linear, magnetic induction linear or continuous wave.
  • DC e.g., electrostatic DC or electrodynamic DC
  • various irradiating devices may be used in the methods disclosed herein, including field ionization sources, electrostatic ion separators, field ionization generators, thermionic emission 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.
  • field ionization sources e.g., electrostatic DC or electrodynamic DC
  • thermionic emission sources e.g., microwave discharge
  • cyclotron type accelerators are available from IBA, Belgium, such as the RHODOTRONTM 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 L3-PSD (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 Laboratories (Russia). Ions and ion accelerators are discussed in Introductory Nuclear Physics, Kenneth S.
  • Electrons may be produced by radioactive nuclei that undergo beta decay, such as isotopes of iodine, cesium, technetium, and iridium.
  • an electron gun can be used as an electron source via thermionic emission and accelerated through an accelerating potential.
  • An electron gun generates electrons, which are then accelerated through a large potential (e.g., greater than about 500 thousand, greater than about 1 million, 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 electrons are initially accelerated in the z direction down the accelerator tube and extracted through a foil window.
  • Scanning the electron beams is useful for increasing the irradiation surface when irradiating materials, e.g., a biomass, that is conveyed through the scanned beam. Scanning the electron beam also distributes the thermal load homogenously on the window and helps reduce the foil window rupture due to local heating by the electron beam. Window foil rupture is a cause of significant down-time due to subsequent necessary repairs and re-starting the electron gun.
  • a beam of electrons can be used as the radiation source.
  • a beam of electrons 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 have 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 emissions 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 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.
  • electrons 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.
  • the energy of each electron of the electron beam is from about 0.3 MeV to about 2.0 MeV (million electron 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 A1, filed Oct. 18, 2011, the entire disclosure of which is herein incorporated by reference.
  • Electron beam irradiation devices may be procured commercially or built.
  • elements or components such inductors, capacitors, casings, power sources, cables, wiring, voltage control systems, current control elements, insulating material, microcontrollers and cooling equipment can be purchased and assembled into a device.
  • a commercial device can be modified and/or adapted.
  • devices and components can be purchased from any of the commercial sources described herein including Ion Beam Applications (Louvain-la-Neuve, Belgium), Wasik Associates Inc. (Dracut, Mass.), NHV Corporation (Japan), the Titan Corporation (San Diego, Calif.), Vivirad High Voltage Corp (Billerica, Mass.) and/or Budker Laboratories (Russia).
  • Typical electron energies can be 0.5 MeV, 1 MeV, 2 MeV, 4.5 MeV, 7.5 MeV, or 10 MeV.
  • Typical electron 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 series 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).
  • 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
  • EPS-1000 e.g., 1000 kV accelerator voltage and 65 or 100 mA beam current.
  • accelerators from NHV's high energy series can be used such as EPS-1500 (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).
  • EPS-1500 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
  • EPS-5000 e.g., 5000 and 30 mA beam current
  • the electron 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 describe herein because of the larger scan width and reduced possibility of local heating and failure of the windows.
  • the extraction system for an electron accelerator can include two window foils.
  • Window foils are described in International App. No. PCT/US2013/064332 (which was filed Oct. 10, 2013 the complete disclosure of which is herein incorporated by reference.
  • 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.
  • the gas is an inert gas such as nitrogen, argon, helium and or carbon dioxide. It is preferred to use a gas rather than a liquid since energy losses to the electron 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 helium).
  • the enclosed conveyor can also be purged with an inert gas so as to maintain an atmosphere at a reduced oxygen level.
  • oxygen levels low avoids the formation of ozone which in some instances is undesirable due to its reactive and toxic nature.
  • 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, helium or carbon dioxide. This can be supplied, for example, from a boil off of a liquid source (e.g., liquid nitrogen or helium), 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. Alternatively, combinations of purging, recirculating and oxygen removal can be done to keep the oxygen levels low.
  • the enclosure 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., electron beam, UV irradiation, microwave irradiation, heating, IR radiation), so that it reacts with the biomass.
  • irradiation e.g., electron beam, UV irradiation, microwave irradiation, heating, IR radiation
  • the biomass itself can be activated, for example by irradiation.
  • the biomass is activated by the electron 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.
  • the gas can be boiled off from a compressed gas such as liquid nitrogen or sublimed from solid carbon dioxide.
  • the gas can be cooled by a chiller or part of or the entire conveyor can be cooled.
  • Some of the effects necessitate shielding and engineering barriers, for example, enclosing the irradiation processes in a concrete (or other radiation opaque material) vault.
  • Another effect of irradiation, vibrational excitation is equivalent to heating up the sample. Heating the sample by irradiation can help in recalcitrance reduction, but excessive heating can destroy the material, as will be explained below.
  • D is the average dose in kGy
  • Cp is the heat capacity in J/g ° C.
  • ⁇ T the change in temperature in ° C.
  • a typical dry biomass material will have a heat capacity close to 2.
  • Wet biomass will have a higher heat capacity dependent on the amount of water since the heat capacity of water is very high (4.19 J/g ° C.).
  • Metals have much lower heat capacities, for example 304 stainless steel has a heat capacity of 0.5 J/g ° C.
  • the temperature change due to the instant adsorption of radiation in a biomass and stainless steel for various doses of radiation is shown below.
  • High temperatures 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 temperatures can become dark, sticky and give off odors indicating decomposition. The stickiness can even make the material hard to convey. The odors can be unpleasant and be a safety issue.
  • keeping the biomass below about 200° C. has been found to be beneficial 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.
  • M FP/D*time
  • F the fraction of power that is adsorbed (unit less)
  • P the emitted power
  • KW Voltage in MeV*Current in mA
  • time the treatment time (sec)
  • D the adsorbed dose (KGy).
  • the throughput (e.g., M, the biomass processed) can be increased by increasing the irradiation time.
  • 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 ⁇ 1 K ⁇ 1 ), heat dissipation is slow, unlike, for example metals (greater than about 10 Wm ⁇ 1 K ⁇ 1 ) which can dissipate energy quickly as long as there is a heat sink to transfer the energy to.
  • the systems and methods include a beam stop (e.g., a shutter).
  • the beam stop can be used to quickly stop or reduce the irradiation of material without powering down the electron beam device.
  • the beam stop can be used while powering up the electron beam, e.g., the beam stop can stop the electron 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.
  • 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 horn), or to any structural support.
  • the beam stop is fixed in relation to the scan horn 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 electrons, 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 electrons.
  • the beam stop can be made of a metal including, but not limited to, stainless steel, lead, iron, molybdenum, silver, gold, titanium, aluminum, tin, or alloys of these, or laminates (layered materials) made with such metals (e.g., metal-coated ceramic, metal-coated polymer, metal-coated composite, multilayered metal materials).
  • a metal including, but not limited to, stainless steel, lead, iron, molybdenum, silver, gold, titanium, aluminum, tin, or alloys of these, or laminates (layered materials) made with such metals (e.g., metal-coated ceramic, metal-coated polymer, metal-coated composite, multilayered metal materials).
  • the beam stop can be cooled, for example, with a cooling fluid such as an aqueous solution or a gas.
  • 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 and gases.
  • the beam stop can be of any shape, including flat, curved, round, oval, square, rectangular, beveled and wedged shapes.
  • the beam stop can have perforations so as to allow some electrons through, thus controlling (e.g., reducing) the levels of radiation across the whole area of the window, or in specific regions of the window.
  • the beam stop can be a mesh formed, for example, 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.
  • Lignocellulosic materials 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, corn cobs, corn stover, soybean stover, corn 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.
  • forestry wastes e.g., sawdust, aspen wood, wood chips
  • grasses
  • the lignocellulosic material includes corncobs.
  • Ground or hammer milled corncobs 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.
  • the entire corn plant is used, including the corn stalk, corn kernels, and in some cases even the root system of the plant.
  • no additional nutrients are required during fermentation of corncobs or cellulosic or lignocellulosic materials containing significant amounts of corncobs.
  • Corncobs, before and after comminution, are also easier to convey and disperse, and have 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 ⁇ -cellulose content such as cotton, and mixtures of any of these.
  • 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 ⁇ -cellulose content such as cotton, and mixtures of any of these.
  • Cellulosic materials can also include lignocellulosic materials which have been partially or fully de-lignified.
  • starchy materials include starch itself, e.g., corn starch, wheat starch, potato starch or rice starch, a derivative of starch, or a material that includes starch, such as an edible food product or a crop.
  • the starchy material can be arracacha, buckwheat, banana, barley, cassava, kudzu, oca, 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.
  • 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 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 flagellates, amoeboids, ciliates, and sporozoa) and plant protists (e.g., algae such alveolates, chlorarachniophytes, cryptomonads, euglenids, glaucophytes, haptophytes, red algae, stramenopiles, and viridaeplantae).
  • protists e.g., animal protists (e.g., protozoa such as flagellates, amoeboids, ciliates, and sporozoa)
  • plant protists e.g., algae such alveolates, chlorarachniophytes, cryptomonads
  • microbial biomass can be obtained from natural sources, e.g., the ocean, lakes, bodies of water, e.g., salt water or fresh water, or on land.
  • microbial biomass can be obtained from culture systems, e.g., large scale dry and wet culture and fermentation systems.
  • the biomass materials such as cellulosic, starchy and lignocellulosic feedstock materials
  • the biomass materials can be obtained from transgenic microorganisms and plants that have been modified with respect to a wild type variety. Such modifications may be, for example, through the iterative steps of selection and breeding to obtain desired traits in a plant.
  • the plants can have had genetic material removed, modified, silenced and/or added with respect to the wild type variety.
  • genetically modified plants can be produced by recombinant DNA methods, where genetic modifications include introducing or modifying specific genes from parental varieties, or, for example, by using transgenic breeding wherein a specific gene or genes are introduced to a plant from a different species of plant and/or bacteria.
  • 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, formaldehyde), irradiation (e.g., X-rays, gamma rays, neutrons, beta particles, alpha particles, protons, deuterons, UV radiation) and temperature shocking or other external stressing and subsequent selection techniques.
  • chemical mutagens e.g., using alkylating agents, epoxides, alkaloids, peroxides, formaldehyde
  • irradiation e.g., X-rays, gamma rays, neutrons, beta particles, alpha particles, protons, deuterons, UV radiation
  • temperature shocking or other external stressing and subsequent selection techniques e.g., temperature shocking or other external stressing and subsequent selection techniques.
  • Other methods of providing modified genes is through error prone PCR
  • Methods of introducing the desired genetic variation in the seed or plant include, for example, the use of a bacterial carrier, biolistics, calcium phosphate precipitation, electroporation, gene splicing, gene silencing, lipofection, microinjection and viral carriers. Additional genetically modified materials have been described in U.S. application Ser. No. 13/396,369 filed Feb. 14, 2012 the full disclosure of which is incorporated herein by reference.
  • the biomass can be in a dry form, 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 have been physically pretreated to have a bulk density of less than about 0.75 g/cm 3 , 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/cm 3 .
  • 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 to Medoff, the full disclosure of which is hereby incorporated by reference.
  • 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)).
  • a mesh or perforated plate with a desired opening size, for example, less than about 6.35
  • 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.
  • material that is larger than the perforations is irradiated and the smaller material is removed by the screening process or recycled.
  • the conveyor itself (for example a part of the conveyor) can be perforated or made with a mesh.
  • 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.
  • mechanoid e.g., a robot equipped with a color, reflectivity or other sensor
  • Optional pre-treatment processing can include heating the material.
  • a portion of the conveyor 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), resistive 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 all the material.
  • 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, CO 2 , Argon) over and/or through the biomass as it is being conveyed.
  • a gas e.g., air, oxygen, nitrogen, He, CO 2 , Argon
  • pre-treatment processing can include cooling the material.
  • Cooling material is described in U.S. Pat. No. 7,900,857 to Medoff, the disclosure of which in incorporated herein by reference.
  • 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.
  • 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.
  • 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 A1 (filed Oct. 26, 2009) and U.S. Pat. App. Pub. 2010/0159569 A1 (filed Dec. 16, 2009), the entire disclosures of which are incorporated herein by reference.
  • Optional materials that can be added include acids and bases.
  • oxidants e.g., peroxides, chlorates
  • polymers e.g., polymerizable monomers (e.g., containing unsaturated bonds)
  • water e.g., water or an organic solvent
  • catalysts e.g., 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 subsequent irradiation step by increasing the efficiency of the irradiation, damping the irradiation or changing the effect of the irradiation (e.g., from electron beams to X-rays or heat).
  • the method may have 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 the conveyor (e.g., the vibratory conveyors 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.
  • the material is delivered to the conveyor using an enclosed material distribution system to help maintain a low oxygen atmosphere 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 electron 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,
  • 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 1 ⁇ 4 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.
  • 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.
  • the biomass can be screened, heated, cooled, and/or combined with additives.
  • 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, heat, and/or the addition of radical scavengers.
  • fluids or gases e.g., oxygen, nitrous oxide, ammonia, liquids
  • 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.
  • a gas e.g., oxygen
  • 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 to Medoff, the entire disclosure of which is incorporate herein by reference.
  • 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.
  • the mechanical treatment may include an initial preparation of the feedstock as received, e.g., size reduction of materials, such as by comminution, e.g., cutting, grinding, shearing, pulverizing or chopping.
  • loose feedstock e.g., recycled paper, starchy materials, or switchgrass
  • Mechanical treatment may reduce the bulk density of the carbohydrate-containing material, increase the surface area of the carbohydrate-containing material and/or decrease one or more dimensions of the carbohydrate-containing material.
  • the feedstock material can be treated with another treatment, for example chemical treatments, such as with an acid (HCl, H 2 SO 4 , H 3 PO 4 ), a base (e.g., KOH and NaOH), a chemical oxidant (e.g., peroxides, chlorates, ozone), irradiation, steam explosion, pyrolysis, sonication, oxidation, chemical treatment.
  • chemical treatments such as with an acid (HCl, H 2 SO 4 , H 3 PO 4 ), 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.
  • 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, H 2 SO 4 , H 3 PO 4 ), radiation, sonication, oxidation, pyrolysis or steam explosion, and then mechanically treated.
  • treatment methods e.g., chemical treatment including and in combination with acid hydrolysis (e.g., utilizing HCl, H 2 SO 4 , H 3 PO 4 ), radiation, sonication, oxidation, pyrolysis or steam explosion, and then mechanically treated.
  • acid hydrolysis e.g., utilizing HCl, H 2 SO 4 , H 3 PO 4
  • radiation e.g., utilizing HCl, H 2 SO 4 , H 3 PO 4
  • Chemical treatment can remove some or all 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 material, 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.
  • 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, ball mill, colloid mill, conical or cone 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 internal structure of the material that was initiated by the previous processing steps.
  • Mechanical feed preparation systems can be configured to produce streams with specific characteristics such as, for example, specific maximum sizes, specific length-to-width, or specific surface areas ratios.
  • Physical preparation 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 desirable to prepare 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).
  • densifying the material e.g., densification can make it easier and less costly to transport to another site
  • 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).
  • 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 Oct.
  • 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.
  • the material to be processed is in the form of a fibrous material that includes fibers provided by shearing a fiber source.
  • the shearing can be performed with a rotary knife cutter.
  • a fiber source e.g., that is recalcitrant 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.
  • the fiber source can be cut prior to the shearing, e.g., with a shredder.
  • the paper when a paper is used as the fiber source, the paper can be first cut into strips that are, e.g., 1 ⁇ 4- to 1 ⁇ 2-inch wide, using a shredder, e.g., a counter-rotating screw shredder, such as those manufactured by Munson (Utica, N.Y.).
  • a shredder e.g., a counter-rotating screw shredder, such as those manufactured by Munson (Utica, N.Y.
  • the paper can be reduced in size by cutting to a desired size using a guillotine cutter.
  • the guillotine cutter can be used to cut the paper into sheets that are, e.g., 10 inches wide by 12 inches long.
  • 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.
  • 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.
  • 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 all 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.
  • 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.
  • these processes can be applied before, during and or after irradiation.
  • a starting biomass material e.g., plant biomass, animal biomass, paper, and municipal waste biomass
  • useful intermediates and products such as organic acids, salts of organic acids, anhydrides, esters of organic acids and fuels, e.g., fuels for internal combustion engines or feedstocks for fuel cells.
  • 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.
  • the glucan- or xylan-containing cellulose in the feedstock can be 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.
  • a saccharifying agent e.g., an enzyme or acid
  • 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 ethanol manufacturing facility.
  • 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.
  • an enzyme e.g., by combining the materials and the enzyme in a solvent, e.g., in an aqueous solution.
  • 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 molecule biomass-degrading metabolites. These enzymes may be a complex of enzymes that act synergistically to degrade crystalline cellulose or the lignin portions of biomass. Examples of cellulolytic enzymes include: endoglucanases, cellobiohydrolases, and cellobiases (beta-glucosidases).
  • 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 water-soluble 1,4-linked dimer of glucose.
  • cellobiase cleaves cellobiose to yield glucose. The efficiency (e.g., time to hydrolyze and/or completeness of hydrolysis) of this process depends on the recalcitrance of the cellulosic material.
  • the biomass material can be converted to one or more products, such as energy, fuels, foods and materials.
  • 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 ethanol, 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), co-product
  • sugars e.g
  • carboxylic acids 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), aldehydes (e.g., acetaldehyde), alpha and beta unsaturated acids (e.g., acrylic acid) and olefins (e.g., ethylene).
  • 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
  • aldehydes e.g., acetaldehyde
  • alpha and beta unsaturated acids e.g., acrylic acid
  • Alcohols and alcohol derivatives 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.
  • sugar alcohols e.g., erythritol, glycol, glycerol, sorbitol threitol, arabitol, ribitol, mannitol, dulcitol, fucitol, iditol, isomalt, maltitol, lactitol,
  • Other products include methyl acrylate, methyl methacrylate, D- or L-lactic acid, citric acid, formic acid, acetic acid, propionic acid, butyric acid, succinic acid, valeric acid, caproic acid, 3-hydroxypropionic 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 present in the product(s).
  • Such sanitation can be done with electron bombardment, for example, be 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.
  • steam generated from burning by-product streams can be used in a distillation process.
  • electricity generated from burning by-product streams can be used to power electron beam generators used in pretreatment.
  • the by-products used to generate steam and electricity are derived from a number of sources throughout the process.
  • anaerobic digestion of wastewater can produce a biogas high in methane and a small amount of waste biomass (sludge).
  • post-saccharification and/or post-distillate solids e.g., unconverted lignin, cellulose, and hemicellulose remaining from the pretreatment and primary processes
  • the spent biomass e.g., spent lignocellulosic material
  • spent lignocellulosic material e.g., spent lignocellulosic material
  • the spent biomass e.g., spent lignocellulosic material
  • 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 as sequestrants.
  • 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 linoleum paste and as a soil stabilizer.
  • the lignin or lignosulfonates can be used, e.g., concrete mixes, clay and ceramics, dyes and pigments, leather tanning and in gypsum board.
  • the lignin or lignosulfonates can be used, e.g., in asphalt, pigments and dyes, pesticides and wax emulsions.
  • 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.
  • lignin For energy production lignin generally has a higher energy content than holocellulose (cellulose and hemicellulose) since it contains more carbon than holocellulose.
  • dry lignin can have 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.
  • lignin can be densified and converted into briquettes and pellets for burning.
  • the lignin can be converted into pellets by any method described herein.
  • 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 burning 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° C. Prior to pyrolyzing, it can be desirable to crosslink the lignin to maintain structural integrity.
  • the biomass may be transferred to a vessel for saccharification.
  • the biomass can be heated after the biomass is irradiated prior to the saccharification step.
  • the heated means can be created, for example, by IR radiation, microwaves, combustion (e.g., gas, coal, oil, biomass), resistive 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 all the material.
  • the biomass may be heated to temperatures above 90° C. in an aqueous liquid that may have an acid or a base present.
  • the aqueous biomass slurry may be heated to 90 to 150° C., alternatively, 105 to 145° C., optionally 110 to 140° C. or further optionally from 115 to 135° C.
  • the time that the aqueous biomass mixture is held at the peak temperature is 1 to 12 hours, alternately, 1 to 6 hours, optionally 1 to 4 hours at the peak temperature.
  • the aqueous biomass mixture is acidic, and the pH is between 1 and 5, optionally 1 to 4, or alternately, 2 to 3.
  • the aqueous biomass mixture is alkaline and the pH is between 6 and 13, alternately, 8 to 12, or optionally, 8 to 11.
  • the treated biomass materials can be saccharified, generally by combining the material and a cellulase enzyme in a fluid medium, e.g., an aqueous solution.
  • a fluid medium e.g., an aqueous solution.
  • the material is boiled, steeped, or cooked in hot water prior to saccharification, as described in U.S. Pat. App. Pub. 2012/0100577 A1 by Medoff and Masterman, published on Apr. 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.
  • a tank e.g., a tank having a volume of at least 4000, 40,000, or 500,000 L
  • the time required for complete saccharification will depend 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.
  • 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.
  • surfactants can enhance the rate of saccharification.
  • surfactants include non-ionic surfactants, such as a Tween® 20 or Tween® 80 polyethylene glycol surfactants, ionic surfactants, or amphoteric surfactants.
  • 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 evaporation, to increase the concentration of the sugar solution. This reduces the volume to be shipped, and also inhibits microbial growth in the solution.
  • sugar solutions of lower concentrations may be used, in which case it may be desirable to add an antimicrobial additive, e.g., a broad spectrum antibiotic, in a low concentration, e.g., 50 to 150 ppm.
  • an antimicrobial additive e.g., a broad spectrum antibiotic
  • 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.
  • an antibiotic can be included even if the sugar concentration is relatively high.
  • other additives with anti-microbial of preservative properties may be used.
  • the antimicrobial additive(s) are
  • 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.
  • concentration can be increased by adding more carbohydrate-containing material to the solution.
  • a surfactant can be added, e.g., one of those discussed above.
  • Solubility can also be increased by increasing the temperature of the solution. For example, the solution can be maintained at a temperature of 40-50° C., 60-80° C., or even higher.
  • Suitable cellulolytic enzymes include cellulases from species in the genera Bacillus, Coprinus, Myceliophthora, Cephalosporium, Scytalidium, Penicillium, 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.
  • Coprinus cinereus 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.
  • 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).
  • acids, bases and other chemicals 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).
  • strong mineral acids can be utilized (e.g. HCl, H 2 SO 4 , H 3 PO 4 ) and strong bases (e.g., NaOH, KOH).
  • sugars e.g., glucose and xylose
  • sugars can be isolated by precipitation, crystallization, chromatography (e.g., simulated moving bed chromatography, high pressure chromatography), centrifugation, extraction, any other isolation method known in the art, and combinations thereof.
  • the processes described herein can include hydrogenation.
  • glucose and xylose can be hydrogenated to sorbitol and xylitol respectively.
  • Hydrogenation can be accomplished by use of a catalyst (e.g., Pt/gamma-Al 2 O 3 , Ru/C, Raney Nickel, or other catalysts know in the art) in combination with H 2 under high pressure (e.g., 10 to 12000 psi).
  • a catalyst e.g., Pt/gamma-Al 2 O 3 , Ru/C, Raney Nickel, or other catalysts know in the art
  • H 2 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 such (e.g., furfural and furfural-derived products). Chemical transformations of sugar derived products are described in U.S. Prov. App. No. 61/667,481, filed Jul. 3, 2012,
  • Yeast and Zymomonas bacteria 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.
  • the optimum pH for yeast is from about pH 4 to 5
  • 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 temperatures in the range of 20° C. to 40° C. (e.g., 26° C. to 40° C.), however thermophilic microorganisms prefer higher temperatures.
  • 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 N 2 , Ar, He, CO 2 or mixtures thereof.
  • the mixture may have a constant purge of an inert gas flowing through the tank during part of or all of the fermentation.
  • anaerobic condition can be achieved or maintained by carbon dioxide production during the fermentation and no additional inert gas is needed.
  • all or a portion of the fermentation process can be interrupted before the low molecular weight sugar is completely converted to a product (e.g., ethanol).
  • 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 preparation 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 Jul. 15, 2011, the complete disclosure of which is incorporated herein by reference.
  • Fermentation includes the methods and products that are disclosed in International App. No. PCT/US2012/071097 (which was filed Dec. 20, 2012, was published in English as WO 2013/096700 and designated the United States) and International App. No. PCT/US2012/071083 (which was filed Dec. 20, 2012, was published in English as WO 2013/096693 and designated the United States) the contents of both of which are incorporated by reference herein in their entirety.
  • Mobile fermenters can be utilized, as described in International App. No. PCT/US2007/074028 (which was filed Jul. 20, 2007, was published in English as WO 2008/011598 and designated the United States) and has a US issued U.S. Pat. No. 8,318,453, the contents of which are incorporated herein in its entirety.
  • the saccharification equipment can be mobile. Further, saccharification and/or fermentation may be performed in part or entirely during transit.
  • the microorganism(s) used in fermentation can be naturally-occurring microorganisms and/or engineered microorganisms.
  • the microorganism can be a bacterium (including, but not limited to, e.g., a cellulolytic bacterium), a fungus, (including, but not limited to, e.g., a yeast), a plant, a protist, e.g., a protozoa or a fungus-like protest (including, but not limited to, e.g., a slime mold), or an alga.
  • a bacterium including, but not limited to, e.g., a cellulolytic bacterium
  • a fungus including, but not limited to, e.g., a yeast
  • a plant e.g., a protist, e.g., a protozoa or a fungus-like protest (including, but not limited to, e.
  • Suitable fermenting microorganisms have 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. (including, but not limited to, S. cerevisiae (baker's yeast), S. distaticus, S. uvarum ), the genus Kluyveromyces , (including, but not limited to, K. marxianus, K. fragilis ), the genus Candida (including, but not limited to, C. pseudotropicalis , and C.
  • brassicae Pichia stipitis (a relative of Candida shehatae ), the genus Clavispora (including, but not limited to, C. lusitaniae and C. opuntiae ), the genus Pachysolen (including, but not limited to, P. tannophilus ), the genus Bretannomyces (including, 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, D.C., 179-212)).
  • B. clausenii Philippidis, G. P., 1996, Cellulose bioconversion technology, in Handbook on Bioethanol: Production and Utilization, Wyman, C. E., ed., Taylor & Francis, Washington, D.C., 179-212
  • Suitable microorganisms include, for example, Zymomonas mobilis, Clostridium spp. (including, but not limited to, C. thermocellum (Philippidis, 1996, supra), C. saccharobutylacetonicum, C. tyrobutyricum C. saccharobutylicum, C. Puniceum, C. beijernckii , and C. acetobutylicum ), Moniliella spp. (including but not limited to M. pollinis, M. tomentosa, M. madida, M. nigrescens, M. oedocephali, M.
  • Yarrowia lipolytica Aureobasidium sp., Trichosporonoides sp., Trigonopsis variabilis, Trichosporon sp., Moniliellaacetoabutans sp., Typhula variabilis, Candida magnoliae, Ustilaginomycetes sp., Pseudozyma tsukubaensis , yeast species of genera Zygosaccharomyces, Debaryomyces, Hansenula and Pichia , and fungi of the dematioid genus Torula (e.g., T. corallina ).
  • Additional 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.
  • organisms such as bacteria, yeasts and fungi
  • organisms can be utilized to ferment biomass derived products such as sugars and alcohols to succinic acid and similar products.
  • organisms can be selected from; Actinobacillus succinogenes, Anaerobiospirillum succiniciproducens, Mannheimia succiniciproducens, Ruminococcus flaverfaciens, Ruminococcus albus, Fibrobacter succinogenes, Bacteroides fragilis, Bacteroides ruminicola, Bacteroides amylophilus, Bacteroides succinogenes, Mannheimia succiniciproducens, Corynebacterium glutamicum, Aspergillus niger, Aspergillus fumigatus, Byssochlamys nivea, Lentinus degener, Paecilomyces varioti, Penicillium viniferum, Saccharomyces cerevisiae, Enterococcus
  • VKM Y-240 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 Y-934, Kluyveromyces wickerhamii VKM Y-589, Pichia anomala VKM Y-118 , P. besseyi VKM Y-2084, P.
  • microbial strains are publicly available, either commercially or through depositories such as the ATCC (American Type Culture Collection, Manassas, Va., USA), the NRRL (Agricultural Research Service Culture Collection, Peoria, Ill., USA), or the DSMZ (Deutsche Sammlung von Mikroorganismen and Zellkulturen GmbH, Braunschweig, Germany), to name a few.
  • ATCC American Type Culture Collection, Manassas, Va., USA
  • NRRL Agricultural Research Service Culture Collection, Peoria, Ill., USA
  • DSMZ Deutsche Sammlung von Mikroorganismen and Zellkulturen GmbH, Braunschweig, Germany
  • yeasts include, for example, RED STAR®/Lesaffre Ethanol Red (available from Red Star/Lesaffre, USA), FAIT® (available from Fleischmann's Yeast, a division of Burns Philip Food Inc., USA), SUPERSTART® (Lallemand Biofuels and Distilled Spirits, Canada), EAGLE C6 FUELTM or C6 FUELTM (available from Lallemand Biofuels and Distilled Spirits, Canada), GERT STRAND® (available from Gert Strand AB, Sweden) and FERMOL® (available from DSM Specialties).
  • RED STAR®/Lesaffre Ethanol Red available from Red Star/Lesaffre, USA
  • FAIT® available from Fleischmann's Yeast, a division of Burns Philip Food Inc., USA
  • SUPERSTART® Lallemand Biofuels and Distilled Spirits, Canada
  • EAGLE C6 FUELTM or C6 FUELTM available from Lallemand Biofuels and Di
  • the resulting fluids can be distilled using, for example, a “beer column” to separate ethanol and other alcohols from the majority of water and residual solids.
  • the vapor exiting the beer column can be, e.g., 35% by weight ethanol and can be fed to a rectification column.
  • a mixture of nearly azeotropic (92.5%) ethanol and water from the rectification column can be purified to pure (99.5%) ethanol 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 dryer.
  • 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 returned 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 can be processed. Any 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.
  • Various conveying systems can be used to convey the biomass material, for example, as previously discussed, to a vault, and under an electron beam in a vault.
  • Exemplary conveyors are belt conveyors, pneumatic conveyors, screw conveyors, carts, trains, trains or carts on rails, elevators, front loaders, backhoes, cranes, various scrapers and shovels, trucks, and throwing devices can be used.
  • vibratory conveyors can be used in various processes described herein. Vibratory conveyors are described in PCT/US2013/64289 filed Oct. 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.
  • 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 1 ⁇ 2 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 have a uniform thickness, preferably as discussed above.
  • an additional spreading method can be useful.
  • a spreader such as a broadcast spreader, a drop spreader (e.g., a CHRISTY SPREADERTM) or combinations thereof can be used to drop (e.g., place, pour, spill and/or sprinkle) the feedstock over a wide area.
  • the spreader can deliver the biomass as a wide shower or curtain onto the vibratory conveyor.
  • 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 have a width transverse to the direction of conveying smaller than the first conveyor.
  • the second conveyor is a vibratory conveyor, the feedstock is spread by the action of the second and first conveyor.
  • the second conveyor ends in a bias cross cut discharge (e.g., a bias cut 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 can span the entire width of the first vibratory conveyor, or it can span part of this width.
  • 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.
  • combinations of spreaders can be used.
  • 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.
  • 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
  • the rate of conveying is related to the beam current and targeted irradiation dose, for example, for a 1 ⁇ 4 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.
  • a useful irradiation dosage e.g. about 10 Mrad for a single pass
  • the conveyor can move at about 10 ft/min to provide approximately the same irradiation dosage.
  • the rate at which material can be conveyed depends 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 5000 lb/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 depend on the density of the material.
  • the material is conveyed at a rate of about 143 ft3/hr, if the material is 1 ⁇ 4′′ 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.
  • a 1 ⁇ 4′′ thick layer of biomass is conveyed at speeds of between about 5 and 100 ft/min (e.g.
  • 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 specific materials, for example, by size or shape. Some conveyors have 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 series of steps or a stair).
  • conveyors can be used, by themselves or coupled with other equipment or systems, for screening, separating, sorting, classifying, distributing, sizing, inspection, picking, metal 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, special liners (e.g., anti-stick, stainless steel, rubber, custom steal, and or grooved), divided troughs, quench pools, screens, perforated plates, detectors (e.g., metal detectors), high temperature designs, food grade designs, heaters, dryers and or coolers.
  • the trough can be of various shapes, for example, flat bottomed, vee shaped bottom, flanged at the top, curved bottom, flat with ridges in any direction, tubular, half pipe, covered or any combinations of these.
  • the conveyors can be coupled with an irradiation systems and/or equipment.
  • the conveyors can be made of corrosion resistant materials.
  • the conveyors can utilize structural materials that include stainless steel (e.g., 304, 316 stainless steel, HASTELLOY® ALLOYS and INCONEL® Alloys).
  • HASTELLOY® Corrosion-Resistant alloys from Hynes such as HASTELLOY® B-3® ALLOY, HASTELLOY® HYBRID-BC1® ALLOY, HASTELLOY® C-4 ALLOY, HASTELLOY® C-22® ALLOY, HASTELLOY® C-22115® ALLOY, HASTELLOY® C-276 ALLOY, HASTELLOY® C-2000® ALLOY, HASTELLOY® G-30® ALLOY, HASTELLOY® G-35® ALLOY, HASTELLOY® N ALLOY and HASTELLOY® ULTIMET® alloy.
  • Hynes such as HASTELLOY® B-3® ALLOY, HASTELLOY® HYBRID-BC1® ALLOY, HASTELLOY® C-4 ALLOY, HASTELLOY® C-22® ALLOY, HASTELLOY® C-22115® ALLOY, HASTELLOY® C-2
  • the vibratory conveyors can include non-stick release coatings, for example, TUFFLONTM (Dupont, Delaware, USA).
  • the vibratory conveyors can also include corrosion resistant coatings.
  • coatings that can be supplied from Metal Coatings Corp (Houston, Tex., USA) and others such as Fluoropolymer, XYLAN®, Molybdenum Disulfide, Epoxy Phenolic, Phosphate-ferrous metal coating, Polyurethane-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 resistance to process gases (e.g., ozone), chemical corrosion, pitting corrosion, galling corrosion and oxidation.
  • one or more other conveying systems can be enclosed.
  • the enclosed conveyor can also be purged with an inert gas so as to maintain an atmosphere at a reduced oxygen level.
  • oxygen levels low avoids the formation of ozone which in some instances is undesirable due to its reactive and toxic nature.
  • 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, helium or carbon dioxide.
  • This can be supplied, for example, from a boil off of a liquid source (e.g., liquid nitrogen or helium), generated or separated from air in situ, or supplied from tanks.
  • a liquid source e.g., liquid nitrogen or helium
  • the inert gas can be recirculated and any residual oxygen can be removed using a catalyst, such as a copper catalyst bed.
  • a catalyst such as a copper catalyst bed.
  • 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., electron beam, UV irradiation, microwave irradiation, heating, IR radiation), so that it reacts with the biomass.
  • irradiation e.g., electron beam, UV irradiation, microwave irradiation, heating, IR radiation
  • the biomass itself can be activated, for example by irradiation.
  • the biomass is activated by the electron 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.
  • the gas can be boiled off from a compressed gas such as liquid nitrogen or sublimed from solid carbon dioxide.
  • the gas can be cooled by a chiller or part of or the entire conveyor can be cooled.
  • any material, processes or processed materials described 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.
  • composites can be made by combining fibrous materials with a resin or polymer.
  • 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 U.S. Serial No. PCT/US2006/010648, filed Mar. 23, 2006, and U.S. Pat. No. 8,074,910 filed Nov. 22, 2011, the entire disclosures of which are herein incorporated by reference.
  • the biomass material is treated at a first level to reduce recalcitrance, e.g., utilizing accelerated electrons, 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).
  • the biomass can be dried between treatments.
  • the treatments can include applying chemical and biochemical treatments to release the sugars.
  • 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.
  • Mrad e.g., less than about 15 Mrad, less than about 10 Mrad, less than about 5 Mrad, less than about 2 Mrad
  • 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
  • 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).
  • a solvent/solution e.g., with water and/or acidified water
  • the solids can be dried, for example in air and/or under vacuum optionally with heating (e.g., below about 150° C., below about 120° C.) to a water content below about 25 wt. % (below about 20 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 all) and then treated with an enzyme (e.g., a cellulase) to release glucose.
  • the glucose e.g., glucose in solution
  • the solids can then be further processed, for example utilized to make energy or other products (e.g., lignin derived products).
  • a cylindrical tank with a diameter of 32 Inches, 64 Inches in height and fit with ASME dished heads (top and bottom) was used in the saccharification.
  • the tank was also equipped with a hydrofoil mixing blade 16′′ wide. Heating was provided by flowing hot water through a half pipe jacket surrounding the tank.
  • the tank was charged with 200 kg water, 80 kg of biomass, and 18 kg of DuetTM Cellulase enzyme available from Genencor, Palo Alto, and CA.
  • Biomass was corn cob that had been hammer milled and screened to a size of between 10 and 40 mesh.
  • the biomass was irradiated with an electron beam to a total dosage of 35 Mrad.
  • the pH of the mixture was adjusted and maintained automatically throughout the saccharification at 4.8 using Ca(OH) 2 . This combination was heated to 53° C., stirred at 180 rpm for about 24 hours after which the saccharification was considered completed.
  • the glucose concentration was below the detection limit, the ethanol concentration was about 25 g/L, and the xylose concentration was about 30 g/L.
  • Distillate bottoms were prepared by distilling the ethanol from fermented material as described above. In addition, solids were removed by centrifugation. The final amount of dissolved solids was 5 to 10 wt. %. There also were fines in the suspended solid. After the distillation the xylose concentration was about 40 g/L. These bottoms were designated as Distillate Bottoms Lot A. A similarly prepared batch was designated as Lot R.
  • BR2 had 200 mL of P2 media, 120 mL of Distillate Bottoms Lot A, ⁇ 72 grams of xylose and DI water to make up to 600 mL.
  • the Xylose concentration was 72 grams plus ⁇ 4.8 g from the Distillate Bottoms for a concentration of about 128 g/L.
  • the reactors were sparged with N 2 gas and inoculated with 7% (45 mL of C. tyrobutyricum (ATCC 25755).
  • the seed was grown overnight at 37° C. in 300 mL of reinforced clostridia media from 1 mL freezer stocks.
  • the bioreactors were sampled periodically submitted for GC and HPLC analysis. The fermentations were maintained above 6.0 using 3.7N ammonium hydroxide. Table 1 shows data collected for these experiments.
  • P2 based medium was made as described in U.S. Pat. No. 6,358,717 but as a 3 fold concentrate (3 ⁇ ), that is only 1 ⁇ 3 of the water was used to make the solutions.
  • P2 medium is made as follows.
  • the medium is composed of the following separately prepared solutions (in grams per 100 ml of distilled water, unless indicated otherwise): 790 ml of distilled water (solution I), 0.5 g of K 2 HPO 4 , 0.5 g of KH 2 PO 4 , 2.2 g of CH 3 COONH 4 (solution II), 2.0 g of MgSO 4 . 7H 2 O, 0.1 g of MnSO 4 .H 2 O, 0.1 g of NaCl, 0.1 g of FeSO 4 .
  • solution III 7H 2 O (solution III), and 100 mg of p-aminobenzoic acid, 100 mg of thiamine, 1 mg of biotin (solution IV).
  • Solutions I and II were filter sterilized and subsequently mixed to form a buffer solution.
  • Solutions III and IV were filter sterilized. Portions (10 and 1 ml) of solutions III and IV, respectively, were added aseptically to the buffer solution. The final pH of the P2 medium was 6.6.
  • the seed was grown overnight in a modified reinforced clostridia media consisting per liter of 10 g peptone, 10 g beef extract, 5 g NaCl, 0.5 g of L cysteine, 3 g of sodium acetate, 0.5 g of anhydrous agar and 5 g of xylose.
  • the media was made up in 900 ml of di water without xylose; 270 ml was aliquoted into 500 ml bottles.
  • the bottles were sparged, autoclaved, and 30 ml of 50 g/L xylose was injected through a 0.22 micron filter into each bottle.
  • the xylose solution was sparged with N 2 gas prior to injection.
  • a 1 ml freezer stock was used per 300 ml bottle.
  • the pH of the fermentation was maintained above 6.0 using 3.7N NH 4 OH. Samples were taken periodically and analyzed with GC and HPLC.
  • AmberliteTM IRA 400 resin 500 g was washed with water (2 ⁇ 500 mL) in a 5 L round bottom flask. Excess water was removed carefully with a pipette before adding a fermentation broth to the wet resin. Fermentation broth (2 L) containing 44.7 g/L butyric acid was added and the resulting mixture was stirred using a magnetic stirrer for 1.5 h. A small analytical sample was removed and was found to contain 32.5 g/L butyric acid (27% loss) by GC head space analysis. This indicated that 24.5 g of butyric acid was adsorbed onto the resin.
  • the supernatant solution was poured off and the wet resin was loaded onto a glass column with a wire sieve at the bottom to prevent clogging. Fermentation broth was rinsed off the resin with a flow of water (2 L) until the eluent was clear. The resin was then transferred to a 2 L round bottom flask containing a magnetic stirring bar and then treated with 100 mL of 1 N HCl followed by 8 mL of 6 N HCl. The resulting mixture was stirred for 5 minutes and the pH was found to be 2.5, which was then subjected to distillation. A total of five bulb to bulb distillations gave 150-250 mL fractions. In between distillations more water and 1 N HCl was added to the resin.
  • the supernatant solution was poured off and the remaining broth was removed with a 50 mL pipette.
  • the resin was rinsed with water (8 ⁇ 25 mL) and then treated with a 10% solution of H 2 SO 4 in EtOH (50 mL). The resulting mixture was stirred at room temperature for 5 minutes and then the ethanolic solution was removed by pipette.
  • the resin was then rinsed with EtOH (10 ⁇ 25 mL), followed by water (10 ⁇ 25 mL).
  • the EtOH rinse solutions were combined and basified with 20% NaOH (pH 11) and then concentrated by rotary evaporation.
  • the water rinse solutions were treated similarly and both solids were dried further in vacuo at 120° C. to give 6.74 g (72.57% sodium butyrate by LC analysis) from ethanol and 1.90 g (80.44% sodium butyrate by LC analysis) from water.
  • the total recovery from the resin was 66.1%.
  • a crude mixture of solids containing a total of 8.9 g of sodium butyrate was treated with 50 mL of ethanol in a 250 mL round bottom flask and the resulting mixture was cooled in a water bath and slowly treated with concentrated sulfuric acid (16 g) while stirring with a magnetic stirring bar.
  • the round bottom flask was fitted with a reflux condenser and the reaction mixture was boiled for 4 hours under N 2 . After cooling to room temperature the reaction mixture was poured into a separatory funnel containing a 150 mL aqueous solution of Na 2 HPO 4 (40 g). The final pH of the solution after mixing was 7.
  • the top layer was separated out and filtered through glass wool to remove sludge giving 4.5 mL of ethyl butyrate.
  • This sample was combined with other similar samples to give about 29 g of a crude liquid that was distilled to give 23.6 g (88% purity by LC analysis)ethyl butyrate.
  • the impurities were mostly ethanol (9.2%) and ethyl acetate (2%).
  • any numerical range recited herein is intended to include all sub-ranges subsumed therein.
  • a range of “1 to 10” is intended to include all 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.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biotechnology (AREA)
  • Biochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • Microbiology (AREA)
  • Genetics & Genomics (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Analytical Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Biomedical Technology (AREA)
  • Sustainable Development (AREA)
  • Architecture (AREA)
  • Urology & Nephrology (AREA)
  • High Energy & Nuclear Physics (AREA)
  • Emergency Medicine (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Toxicology (AREA)
  • Plasma & Fusion (AREA)
  • Structural Engineering (AREA)
  • Civil Engineering (AREA)
  • Electromagnetism (AREA)
  • Environmental & Geological Engineering (AREA)
  • Materials Engineering (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Processing Of Solid Wastes (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
US14/433,217 2013-03-08 2014-03-07 Processing and transforming biomass Abandoned US20150361457A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US14/433,217 US20150361457A1 (en) 2013-03-08 2014-03-07 Processing and transforming biomass

Applications Claiming Priority (17)

Application Number Priority Date Filing Date Title
US201361774750P 2013-03-08 2013-03-08
US201361774723P 2013-03-08 2013-03-08
US201361774735P 2013-03-08 2013-03-08
US201361774761P 2013-03-08 2013-03-08
US201361774775P 2013-03-08 2013-03-08
US201361774752P 2013-03-08 2013-03-08
US201361774746P 2013-03-08 2013-03-08
US201361774740P 2013-03-08 2013-03-08
US201361774731P 2013-03-08 2013-03-08
US201361774773P 2013-03-08 2013-03-08
US201361774780P 2013-03-08 2013-03-08
US201361774754P 2013-03-08 2013-03-08
US201361774744P 2013-03-08 2013-03-08
US201361774684P 2013-03-08 2013-03-08
US201361793336P 2013-03-15 2013-03-15
PCT/US2014/021796 WO2014138594A1 (en) 2013-03-08 2014-03-07 Processing and transforming biomass
US14/433,217 US20150361457A1 (en) 2013-03-08 2014-03-07 Processing and transforming biomass

Publications (1)

Publication Number Publication Date
US20150361457A1 true US20150361457A1 (en) 2015-12-17

Family

ID=51491991

Family Applications (28)

Application Number Title Priority Date Filing Date
US14/758,909 Abandoned US20150368684A1 (en) 2013-03-08 2014-03-07 Processing biomass
US14/433,217 Abandoned US20150361457A1 (en) 2013-03-08 2014-03-07 Processing and transforming biomass
US14/299,010 Active US9637802B2 (en) 2013-03-08 2014-06-09 Upgrading process streams
US14/299,000 Abandoned US20140287469A1 (en) 2013-03-08 2014-06-09 Filtration
US14/299,007 Abandoned US20140286714A1 (en) 2013-03-08 2014-06-09 Processing materials
US14/299,003 Active US9371550B2 (en) 2013-03-08 2014-06-09 Processing materials
US14/299,002 Active US10549241B2 (en) 2013-03-08 2014-06-09 Enclosures for treating materials
US14/299,004 Active US9334518B2 (en) 2013-03-08 2014-06-09 Array for processing materials
US14/299,005 Active US9388442B2 (en) 2013-03-08 2014-06-09 Reconfigureable processing enclosures
US14/299,006 Active US9611516B2 (en) 2013-03-08 2014-06-09 Controlling process gases
US14/299,008 Abandoned US20140284277A1 (en) 2013-03-08 2014-06-09 Processing biomass materials
US14/299,001 Abandoned US20140287470A1 (en) 2013-03-08 2014-06-09 Processing biomass and energy
US15/099,498 Active US9464334B2 (en) 2013-03-08 2016-04-14 Array for processing materials
US15/178,166 Expired - Fee Related US9777430B2 (en) 2013-03-08 2016-06-09 Reconfigurable processing enclosures
US15/178,714 Expired - Fee Related US9816231B2 (en) 2013-03-08 2016-06-10 Processing materials
US15/255,881 Expired - Fee Related US9708761B2 (en) 2013-03-08 2016-09-02 Array for processing materials
US15/434,629 Expired - Fee Related US10294612B2 (en) 2013-03-08 2017-02-16 Controlling process gases
US15/487,565 Active US9925496B2 (en) 2013-03-08 2017-04-14 Upgrading process streams
US15/616,507 Active US10105652B2 (en) 2013-03-08 2017-06-07 Array for processing materials
US15/690,083 Expired - Fee Related US10350548B2 (en) 2013-03-08 2017-08-29 Reconfigurable processing enclosures
US15/730,160 Active US10066339B2 (en) 2013-03-08 2017-10-11 Processing materials
US15/913,740 Active US10543460B2 (en) 2013-03-08 2018-03-06 Upgrading process streams
US16/050,797 Expired - Fee Related US10518220B2 (en) 2013-03-08 2018-07-31 Processing materials
US16/054,229 Expired - Fee Related US10610848B2 (en) 2013-03-08 2018-08-03 Processing materials
US16/134,274 Active US10682623B2 (en) 2013-03-08 2018-09-18 Array for processing materials
US16/586,921 Abandoned US20200038811A1 (en) 2013-03-08 2019-09-28 Enclosures for treating materials
US16/686,709 Abandoned US20200086273A1 (en) 2013-03-08 2019-11-18 Processing materials
US16/704,850 Abandoned US20200156039A1 (en) 2013-03-08 2019-12-05 Upgrading process streams

Family Applications Before (1)

Application Number Title Priority Date Filing Date
US14/758,909 Abandoned US20150368684A1 (en) 2013-03-08 2014-03-07 Processing biomass

Family Applications After (26)

Application Number Title Priority Date Filing Date
US14/299,010 Active US9637802B2 (en) 2013-03-08 2014-06-09 Upgrading process streams
US14/299,000 Abandoned US20140287469A1 (en) 2013-03-08 2014-06-09 Filtration
US14/299,007 Abandoned US20140286714A1 (en) 2013-03-08 2014-06-09 Processing materials
US14/299,003 Active US9371550B2 (en) 2013-03-08 2014-06-09 Processing materials
US14/299,002 Active US10549241B2 (en) 2013-03-08 2014-06-09 Enclosures for treating materials
US14/299,004 Active US9334518B2 (en) 2013-03-08 2014-06-09 Array for processing materials
US14/299,005 Active US9388442B2 (en) 2013-03-08 2014-06-09 Reconfigureable processing enclosures
US14/299,006 Active US9611516B2 (en) 2013-03-08 2014-06-09 Controlling process gases
US14/299,008 Abandoned US20140284277A1 (en) 2013-03-08 2014-06-09 Processing biomass materials
US14/299,001 Abandoned US20140287470A1 (en) 2013-03-08 2014-06-09 Processing biomass and energy
US15/099,498 Active US9464334B2 (en) 2013-03-08 2016-04-14 Array for processing materials
US15/178,166 Expired - Fee Related US9777430B2 (en) 2013-03-08 2016-06-09 Reconfigurable processing enclosures
US15/178,714 Expired - Fee Related US9816231B2 (en) 2013-03-08 2016-06-10 Processing materials
US15/255,881 Expired - Fee Related US9708761B2 (en) 2013-03-08 2016-09-02 Array for processing materials
US15/434,629 Expired - Fee Related US10294612B2 (en) 2013-03-08 2017-02-16 Controlling process gases
US15/487,565 Active US9925496B2 (en) 2013-03-08 2017-04-14 Upgrading process streams
US15/616,507 Active US10105652B2 (en) 2013-03-08 2017-06-07 Array for processing materials
US15/690,083 Expired - Fee Related US10350548B2 (en) 2013-03-08 2017-08-29 Reconfigurable processing enclosures
US15/730,160 Active US10066339B2 (en) 2013-03-08 2017-10-11 Processing materials
US15/913,740 Active US10543460B2 (en) 2013-03-08 2018-03-06 Upgrading process streams
US16/050,797 Expired - Fee Related US10518220B2 (en) 2013-03-08 2018-07-31 Processing materials
US16/054,229 Expired - Fee Related US10610848B2 (en) 2013-03-08 2018-08-03 Processing materials
US16/134,274 Active US10682623B2 (en) 2013-03-08 2018-09-18 Array for processing materials
US16/586,921 Abandoned US20200038811A1 (en) 2013-03-08 2019-09-28 Enclosures for treating materials
US16/686,709 Abandoned US20200086273A1 (en) 2013-03-08 2019-11-18 Processing materials
US16/704,850 Abandoned US20200156039A1 (en) 2013-03-08 2019-12-05 Upgrading process streams

Country Status (21)

Country Link
US (28) US20150368684A1 (es)
EP (13) EP2890805A4 (es)
JP (28) JP6461017B2 (es)
KR (12) KR20150126830A (es)
CN (16) CN105247062A (es)
AP (12) AP2015008692A0 (es)
AU (29) AU2014225480B2 (es)
BR (9) BR112015019231A2 (es)
CA (12) CA2886774A1 (es)
CU (11) CU24286B1 (es)
EA (16) EA030172B1 (es)
IL (12) IL240484A0 (es)
MX (17) MX361291B (es)
MY (7) MY174611A (es)
NZ (14) NZ743055A (es)
PH (16) PH12015500584A1 (es)
PL (1) PL2890798T3 (es)
SG (23) SG10201704485UA (es)
UA (5) UA117234C2 (es)
WO (12) WO2014138548A1 (es)
ZA (1) ZA201705571B (es)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9919939B2 (en) 2011-12-06 2018-03-20 Delta Faucet Company Ozone distribution in a faucet
US10174160B2 (en) 2013-04-26 2019-01-08 Xyleco, Inc. Processing hydroxy-carboxylic acids to polymers
US20190309232A1 (en) * 2016-06-13 2019-10-10 Bio-Think Mixture for supplying a boiler or a diesel engine, comprising diesel fuel or heating oil and esters and alkanes from the transformation of biomass
US10501761B2 (en) 2013-04-26 2019-12-10 Xyleco, Inc. Processing biomass to obtain hydroxylcarboxylic acids
US10543460B2 (en) 2013-03-08 2020-01-28 Xyleco, Inc. Upgrading process streams
US10981735B2 (en) * 2017-05-16 2021-04-20 Sumitomo Chemical Company, Limited Pneumatic conveyance method for methionine
WO2021257080A1 (en) * 2020-06-18 2021-12-23 Recycle Track Systems Inc. Indoor food waste fermentation and recycling process
US11220467B2 (en) 2017-01-11 2022-01-11 Recycle Track Systems, Inc. Indoor food waste fermentation and recycling process
US11458214B2 (en) 2015-12-21 2022-10-04 Delta Faucet Company Fluid delivery system including a disinfectant device

Families Citing this family (149)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008055468B4 (de) * 2008-12-01 2010-09-02 Nukem Technologies Gmbh Verfahren und Anordnung zur Herstellung von Brennstoffkernen
EP2585606A4 (en) 2010-06-26 2016-02-17 Virdia Ltd SUGAR MIXTURES, METHODS OF PRODUCTION AND USE THEREOF
IL206678A0 (en) 2010-06-28 2010-12-30 Hcl Cleantech Ltd A method for the production of fermentable sugars
IL207329A0 (en) 2010-08-01 2010-12-30 Robert Jansen A method for refining a recycle extractant and for processing a lignocellulosic material and for the production of a carbohydrate composition
IL207945A0 (en) 2010-09-02 2010-12-30 Robert Jansen Method for the production of carbohydrates
GB2524906B8 (en) 2011-04-07 2016-12-07 Virdia Ltd Lignocellulose conversion processes and products
US9617608B2 (en) 2011-10-10 2017-04-11 Virdia, Inc. Sugar compositions
AU2013256049B2 (en) 2012-05-03 2017-02-16 Virdia, Inc. Methods for treating lignocellulosic materials
US9493851B2 (en) 2012-05-03 2016-11-15 Virdia, Inc. Methods for treating lignocellulosic materials
EP2894469B1 (en) * 2012-09-04 2019-03-06 Atonarp Inc. Membrane exchange unit and systems having membrane exchange units
WO2014059131A1 (en) * 2012-10-10 2014-04-17 Xyleco, Inc. Equipment protecting enclosures
US10689196B2 (en) 2012-10-10 2020-06-23 Xyleco, Inc. Processing materials
US9505566B2 (en) * 2013-04-02 2016-11-29 National Research Council Of Canada Powder feeder method and system
FR3015311B1 (fr) * 2013-12-24 2016-01-01 Agronomique Inst Nat Rech Procede de fractionnement d'un tourteau d'oleagineux et applications de ce procede
WO2015142541A1 (en) 2014-03-21 2015-09-24 Xyleco, Inc. Method and structures for processing materials
MX2017000870A (es) * 2014-07-21 2017-03-08 Xyleco Inc Procesamiento de biomasa.
DE102014011315A1 (de) * 2014-08-04 2016-02-04 Michael Niederbacher Flüssigsubstratbehälter für eine Biogasanlage
US20160051965A1 (en) * 2014-08-19 2016-02-25 Jeff R. Angel Absorbant and digester for carbon-based substances such as oil
WO2016043789A1 (en) 2014-09-19 2016-03-24 Medorff Marshall Saccharides and saccharide compositions and mixtures
FR3027821B1 (fr) * 2014-10-31 2018-11-16 Centralesupelec Procede de purification d'oses.
WO2016094878A1 (en) * 2014-12-12 2016-06-16 Virdia, Inc. Methods for converting cellulose to furanic products
CN112226466A (zh) 2015-01-07 2021-01-15 威尔迪亚公司 萃取和转化半纤维素糖的方法
AU2016243181A1 (en) * 2015-03-31 2017-08-31 Xyleco, Inc. Processing of biomass materials
PT3286373T (pt) * 2015-04-23 2023-08-24 Univ Maine System Métodos para a produção de nanocelulose com alto teor de sólidos
WO2016205014A1 (en) * 2015-06-17 2016-12-22 Exxonmobil Research And Engineering Company Zif-containing adsorbent materials and uses thereof
US9777303B2 (en) 2015-07-23 2017-10-03 Fluid Quip Process Technologies, Llc Systems and methods for producing a sugar stream
US10010282B2 (en) 2015-07-24 2018-07-03 Kurin, Inc. Blood sample optimization system and blood contaminant sequestration device and method
DE102015011285A1 (de) * 2015-08-27 2017-03-02 Daimler Ag Bodenstation zum Laden eines Kraftfahrzeugs
US10113122B2 (en) 2015-08-31 2018-10-30 University Of New Brunswick Process for upgrading heavy hydrocarbon liquids
KR102250734B1 (ko) * 2015-09-25 2021-05-11 에스케이이노베이션 주식회사 원유 내의 유기산 및 금속의 제거 방법
WO2017053053A1 (en) * 2015-09-25 2017-03-30 The Government Of The United States Of America, As Represented By The Secretary Of The Navy Catalyst-free removal of nox and other contaminants from combustion exhausts using intense pulsed electron beams
KR101697186B1 (ko) * 2015-10-02 2017-01-17 한국수력원자력 주식회사 이송유닛 및 이를 포함하는 공기 처리 장치
CN105525957B (zh) * 2015-11-20 2018-08-14 吕桐华 用蒸汽替代熔盐热力系统及热电联产的方法
LU92897B1 (fr) * 2015-12-10 2017-06-19 Libourne Company Ltd Dispositif pour le traitement des eaux usées
KR101733082B1 (ko) * 2015-12-29 2017-05-08 한국화학연구원 바이오매스로부터 추출성 성분을 효율적으로 제거 혹은 회수하는 방법
US10099155B2 (en) 2016-02-26 2018-10-16 Crown Iron Works Company Screen for extractor system
CA3016380C (en) * 2016-03-03 2023-03-21 Recover Energy Services Inc. Gas tight horizontal decanter for drilling waste solids washing
CN106010677A (zh) * 2016-06-01 2016-10-12 卞佳林 一种以油茶为原料制备生物燃料的方法
CN106366137A (zh) * 2016-08-27 2017-02-01 山东绿健生物技术有限公司 一种异构化乳糖液的脱盐脱色方法
CN106490443A (zh) * 2016-09-23 2017-03-15 北京甸甸丰生物科技有限公司 一种含有植物提取物用于食品保鲜的制剂
CA2982067A1 (en) 2016-10-07 2018-04-07 Ying Zheng Catalytic process for co-processing of lignocellulosic biomass and heavy petroleum fuels
US20190289882A1 (en) * 2016-10-18 2019-09-26 Paul BRESLIN Glucose beverage comprising exogenous flavor source and color
FR3058999B1 (fr) * 2016-11-24 2019-10-25 Novasep Process Procede de purification utilisant une resine de faible granulometrie
IL249923B (en) 2017-01-03 2018-03-29 Shohat Tsachi Smart trash can
WO2018151693A1 (en) * 2017-02-15 2018-08-23 Polkar Orman Ürünleri̇ Ve Enerji̇ A.Ş Green mdf production technique from sustainable source and energy
MA40103B1 (fr) * 2017-03-08 2018-11-30 Mustapha Benmoussa Procédé de préparation d'un revêtement pour améliorer l'efficacité et la qualité des engrais.
CN106746148B (zh) * 2017-03-17 2023-08-01 成都源蓉科技有限公司 一种磁加载沉淀过滤净化系统
RU2669297C2 (ru) * 2017-03-22 2018-10-09 Федеральное государственное унитарное предприятие "Проектно-конструкторское бюро" НИИСХ Северо-Востока Установка для получения патоки из зерна злаковых культур
CN106861659A (zh) * 2017-04-12 2017-06-20 明光市国星凹土有限公司 一种用于水处理的凹凸棒土油品脱色剂及其制备方法
US20180368343A1 (en) * 2017-06-22 2018-12-27 Greg O'Rourke Sustainable Growing System and Method
CN107246800A (zh) * 2017-07-08 2017-10-13 深圳市汇美新科技有限公司 轮式刮板及带该轮式刮板的凝结室
US10485253B2 (en) 2017-08-21 2019-11-26 Mustapha Benmoussa Method of microalgal biomass processing for high-value chemicals production, the resulting composition of butyrogenic algal slowly fermenting dietary fiber, and a way to improve colon health using a slowly fermenting butyrogenic algal dietary fiber
KR102003918B1 (ko) * 2017-11-28 2019-10-17 한국과학기술연구원 에너지 저소비형 당과 산의 분리방법
CN107879028A (zh) * 2017-12-01 2018-04-06 中冶焦耐(大连)工程技术有限公司 一种高温物料密闭筛分输送一体化装置
WO2019152411A1 (en) * 2018-01-30 2019-08-08 Global Spirits Filtration Company, LLC Systems and methods for making ethanol products
CA3002039A1 (en) * 2018-02-05 2019-08-05 Noram Engineering And Constructors Ltd. Removal of dissolved carbohydrates from a sulfuric acid solution
US11519013B2 (en) 2018-03-15 2022-12-06 Fluid Quip Technologies, Llc System and method for producing a sugar stream with front end oil separation
US11053557B2 (en) 2018-03-15 2021-07-06 Fluid Quip Technologies, Llc System and method for producing a sugar stream using membrane filtration
US11505838B2 (en) 2018-04-05 2022-11-22 Fluid Quip Technologies, Llc Method for producing a sugar stream
US10480038B2 (en) 2018-04-19 2019-11-19 Fluid Quip Technologies, Llc System and method for producing a sugar stream
CN108547079B (zh) * 2018-06-08 2023-10-10 北京鹏盛天纤科技有限公司 一种脱脂棉绿色连续式生产集成装置和工艺
CN108840108A (zh) * 2018-06-26 2018-11-20 河南禾力能源股份有限公司 一种糠醛渣负压吸收入锅炉上料机装置
CN108970562B (zh) * 2018-08-01 2020-05-05 沈阳师范大学 一种带有消毒功能的光催化剂的反应器
CN109097138B (zh) * 2018-08-13 2020-11-13 泰州港润投资发展有限公司 一种生物质燃料原材料制作设备及其生物质燃料制作工艺
CN109243656B (zh) * 2018-08-17 2022-04-26 西南科技大学 一种藻类人工结皮治理氡及子体铀矿冶气载放射性污染的方法
US11274464B2 (en) * 2018-09-13 2022-03-15 Baker Engineering & Risk Consultants, Inc. Fragment-, overpressure-, radiation-, and toxic-resistant emergency safety shelter
RU2690339C1 (ru) * 2018-10-22 2019-05-31 Федеральное государственное бюджетное образовательное учреждение высшего образования "Тамбовский государственный технический университет" (ФГБОУ ВО "ТГТУ") Электродиализатор с охлаждением разделяемого раствора
CN109503096A (zh) * 2018-10-29 2019-03-22 赵顺全 一种助滤剂材料的制备方法
CN109294893B (zh) * 2018-10-30 2024-03-19 北京建筑大学 一种白酒酿造副产物黄水的资源化利用系统及方法
CN109439371B (zh) * 2018-11-12 2024-03-22 国能龙源环保有限公司 一种生物质气化的高温冷灰器
KR102085144B1 (ko) * 2018-11-20 2020-03-04 곽병열 분쇄와 살균을 이용한 친환경적 동물 사체 처리 장치 및 방법
KR20210097102A (ko) * 2018-12-03 2021-08-06 서텍스 메디컬 인크. 방사선 색전술 마이크로스피어의 전달을 위한 장치
US20220049200A1 (en) * 2018-12-10 2022-02-17 Sung Min Lee Apparatus for producing fermented soybean meal
WO2020124168A1 (en) * 2018-12-21 2020-06-25 Leaf Resources Limited Separation method
FI129229B (en) 2019-02-07 2021-09-30 Fazer Ab Oy Karl Method for the utilization of biomass
CN110044759A (zh) * 2019-03-18 2019-07-23 中国水利水电科学研究院 一种草地地上-地下双重生物量测量装置
CN112512992B (zh) * 2019-03-20 2022-03-01 维生素C60生化学研究公司 碳簇制造用的成型体及其制造方法
WO2020205212A1 (en) 2019-03-29 2020-10-08 Carbon, Inc. Dual cure resin for the production of moisture-resistant articles by additive manufacturing
CN110002607A (zh) * 2019-04-16 2019-07-12 上海泰缘生物科技股份有限公司 一种微生态激活系统及其制备的微生态激活袋
JP7196752B2 (ja) * 2019-04-25 2022-12-27 トヨタ自動車株式会社 電動車両
KR20220006564A (ko) 2019-05-09 2022-01-17 인베스티가시오네스 포레스탈레스 비오포레스트 에세.아. 펄프 및 종이 제조 공장으로부터의 유출물을 처리하기 위한 플랜트로부터 물 및 화학물질을 회수하는 방법
US11291104B2 (en) 2019-05-31 2022-03-29 Fermi Research Alliance, Llc Permanent magnet e-beam/x-ray horn
US10880984B2 (en) 2019-05-31 2020-12-29 Fermi Research Alliance, Llc Permanent magnet e-beam/x-ray horn
US11717584B2 (en) 2019-05-31 2023-08-08 Fermi Research Alliance, Llc Supported X-ray horn for controlling e-beams
CN110438019B (zh) * 2019-06-06 2021-04-06 浙江工业大学 一种复合菌剂及其发酵餐厨垃圾制备有机液体肥料的应用
US11479960B1 (en) * 2019-06-11 2022-10-25 Weller Construction, Inc. Oncology vault structure
US11226297B2 (en) 2019-06-12 2022-01-18 Raytheon Company X-ray dosage mitigation for semiconductors and material inspection systems
JP6604525B1 (ja) * 2019-06-17 2019-11-13 株式会社太洋サービス バイオマス原料保管方法および保管システム
US11639010B2 (en) 2019-07-08 2023-05-02 Fermi Research Alliance, Llc Electron beam treatment for invasive pests
IN201941029553A (es) * 2019-07-22 2019-08-09
CN110413953B (zh) * 2019-07-30 2023-07-14 深圳市智物联网络有限公司 物质数量确定方法、系统、装置及计算机可读存储介质
KR102094431B1 (ko) * 2019-08-02 2020-03-31 안평욱 현미당화농축액 제조방법
CN110644817B (zh) * 2019-09-18 2021-07-16 陕西地建土地工程技术研究院有限责任公司 一种野外科学观测研究温室及其建筑方法
JP6661141B1 (ja) * 2019-09-26 2020-03-11 株式会社太洋サービス バイオマス原料保管方法およびバイオマス原料保管システム
EP3997113A4 (en) * 2019-10-02 2023-06-28 Chiaranussati, Suchad Humus treatment process with active neurological substances
CN110755884B (zh) * 2019-11-14 2022-01-18 山东睿智医药科技有限公司 一种反向吸附提取生物产品的方法
KR102185321B1 (ko) * 2019-11-27 2020-12-02 한국지질자원연구원 방사성탄소 연대측정 시료를 위한 aba법에 의한 전자동 화학전처리 장치
CN111228855A (zh) * 2020-01-14 2020-06-05 无锡市疾病预防控制中心 一种菠萝肉基质生物炭填料固相萃取柱的制备方法
US11731926B2 (en) 2020-03-11 2023-08-22 Lanzatech, Inc. Process for purification of products
MY193502A (en) * 2020-03-11 2022-10-17 Lanzatech Inc Process for purification of products
US11244262B2 (en) * 2020-03-17 2022-02-08 Freeport-Mcmoran Inc. Methods and systems for deploying equipment required to meet defined production targets
KR102314179B1 (ko) * 2020-04-29 2021-10-18 경상국립대학교산학협력단 에테폰을 포함하는 메탄가스 발생 저감용 비료 조성물 및 이의 용도
CN111587797B (zh) * 2020-06-16 2022-06-14 烟台大学 一种花青素植物提取废弃物制备的天然指示猫砂
CN111717551B (zh) * 2020-06-23 2022-05-17 美巢集团股份公司 卸料设备及其加湿装置
CN111635302B (zh) * 2020-07-08 2021-06-15 江南大学 一种多柱连续色谱除盐以纯化羟基乙酸的方法
CN112006913A (zh) * 2020-08-13 2020-12-01 宁夏明德中药饮片有限公司 一种熟地黄饮片蒸煮制备工艺
TWI722956B (zh) * 2020-08-17 2021-03-21 傑明科技有限公司 結合微粒凝結成長及慣性衝擊技術的pm2.5控制設備
US10995351B1 (en) 2020-09-14 2021-05-04 Fluid Quip Technologies, Llc System and method for producing a carbohydrate stream from a cellulosic feedstock
WO2022066565A1 (en) 2020-09-25 2022-03-31 Carbon, Inc. Epoxy dual cure resin for the production of moisture-resistant articles by additive manufacturing
CN112520436B (zh) * 2020-10-12 2022-06-24 嘉兴学院 一种固态发酵箱及其使用方法
CN112293394B (zh) * 2020-10-30 2022-11-25 海南德安欣有害生物防治科技有限公司 一种捕鼠装置及捕鼠方法
CN112264194B (zh) * 2020-11-04 2022-06-07 昆明冶金研究院有限公司 一种高硫铁易泥化细粒复杂嵌布铜钼矿高效浮选捕收剂及其制备方法与应用
RU205872U1 (ru) * 2020-11-26 2021-08-11 Роман Сергеевич Соколов Шахтная зерносушилка с функцией обеззараживания зерна
CN112692042B (zh) * 2020-12-08 2022-05-24 广西博世科环保科技股份有限公司 一种铝电解槽废耐火材料处理工艺及其系统
RU2752939C1 (ru) * 2020-12-11 2021-08-11 Артемий Геннадьевич Будин Устройство для снижения выбросов угарного газа и оксида азота при утилизации ТБО методом сжигания
RU204776U1 (ru) * 2020-12-21 2021-06-09 Федеральное государственное бюджетное образовательное учреждение высшего образования "Рязанский государственный агротехнологический университет имени П.А. Костычева" (ФГБОУ ВО РГАТУ) Ленточная центрифуга
CN112845078B (zh) * 2020-12-31 2023-04-25 湖北润楚生物科技有限公司 一种风选机通风管道灰尘处理装置
US20240079598A1 (en) * 2021-02-05 2024-03-07 Denka Company Limited Carbon black, carbon black production method, composition for electrode, electrode, and secondary battery
CN116419955A (zh) * 2021-02-05 2023-07-11 电化株式会社 炭黑、炭黑的制造方法、电极用组合物、电极及二次电池
RU2760160C1 (ru) * 2021-02-19 2021-11-22 Государственное бюджетное образовательное учреждение высшего образования Нижегородский государственный инженерно-экономический университет Установка для получения зерновой патоки
CN112973212B (zh) * 2021-02-22 2022-08-05 宜宾丝丽雅股份有限公司 一种粘胶生产用滤芯的清洗方法
CN113018905B (zh) * 2021-03-03 2022-07-05 东阳市易源环保科技有限公司 一种基于硅胶和白土吸附回收的废油净化装置
CN113308923B (zh) * 2021-05-28 2022-06-10 北京三联虹普新合纤技术服务股份有限公司 一种用于制备Lyocell纤维的浆粕均化与调质系统
CN117500777A (zh) * 2021-06-16 2024-02-02 Gs加德士公司 从发酵液中获得目标化合物的方法
EP4358847A1 (en) 2021-06-23 2024-05-01 Kimtron, Inc. System and method for ultra-close proximity irradiation of rotating biomass
CA3226449A1 (en) * 2021-07-21 2023-01-26 Alliance Bioenergy Plus, Inc., Dba Blue Biofuels System and method to convert cellulosic materials into sugar
CN113663626B (zh) * 2021-08-30 2022-09-20 江西科技学院 用于铜矿渣废弃料的光催化降解装置及使用方法
CN113732020A (zh) * 2021-09-08 2021-12-03 中国科学院地理科学与资源研究所 一种餐厨垃圾回收系统
CN113893578A (zh) * 2021-09-08 2022-01-07 四川雅华生物有限公司 一种水解液的分离提纯系统及工艺方法
CN114053933B (zh) * 2021-09-30 2024-03-19 国高材高分子材料产业创新中心有限公司 一种溶液自动配制系统及其配制方法
CN113797839B (zh) * 2021-11-18 2022-02-08 山东沃赛新材料科技有限公司 硅酮密封胶生产用粉尘处理装置
CN114195339B (zh) * 2021-11-22 2024-03-29 深圳市政水环境技术有限公司 污泥碳源化回用同步污泥减量方法、装置及系统
CN114210124A (zh) * 2021-11-29 2022-03-22 国家电网有限公司 一种特高压换流站自动绝缘油处理装置
CN114229359A (zh) * 2021-12-15 2022-03-25 福建天马科技集团股份有限公司 一种大黄鱼苗料专用的生产输送设备
CN114479975A (zh) * 2021-12-29 2022-05-13 王子音 生物质能源原料分离式加工设备
JP2023116943A (ja) * 2022-02-10 2023-08-23 セイコーエプソン株式会社 セルロースの糖化方法
CN115074164B (zh) * 2022-05-07 2023-10-03 塔里木大学 难浮选烟煤中关键有害元素一体化清洁脱除方法
KR102661850B1 (ko) * 2022-06-14 2024-04-26 씨제이제일제당 (주) 아미노산 호환 생산을 위한 재구성이 가능한 복수개의 배관을 포함하는 아미노산 생산 시스템 및 구성 방법
KR102532786B1 (ko) * 2022-07-11 2023-05-18 (주)한신엔지니어링 분체 이송 시스템
CN115254602B (zh) * 2022-08-02 2023-10-10 中粮山萃花生制品(威海)有限公司 一种坚果筛选装置及其使用方法
CN115487928B (zh) * 2022-08-17 2023-09-19 山东戴瑞克新材料有限公司 一种带氮气保护的粉碎过滤装置
WO2024054500A1 (en) * 2022-09-08 2024-03-14 Growcentia, Inc. Compositions for enhancing plant growth based on microbe-free broth
CN115555033B (zh) * 2022-10-09 2023-06-23 绍兴上虞催化剂有限责任公司 氨合成用废催化剂回收利用装置
CN115591463B (zh) * 2022-11-01 2024-05-17 南京海合源农业科技服务有限公司 一种食蟾虫脂质体制备装置
CN116120114B (zh) * 2022-12-09 2024-01-12 杭州楠大环保科技有限公司 一种厨房垃圾资源化利用生产新型肥料的方法
US11920794B1 (en) 2022-12-15 2024-03-05 Ge Infrastructure Technology Llc Combustor having thermally compliant bundled tube fuel nozzle
US11939878B1 (en) 2022-12-15 2024-03-26 Ge Infrastructure Technology Llc Turbomachine component having self-breaking supports
KR102655814B1 (ko) 2023-12-29 2024-04-17 삼성물산 주식회사 추가하중을 이용한 보강말뚝의 선행하중 재하시스템 및 이를 이용한 선행하중 재하방법
KR102655813B1 (ko) 2023-12-29 2024-04-08 삼성물산 주식회사 보강말뚝의 선행하중 재하시스템 및 이를 이용한 선행하중 재하방법

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080248540A1 (en) * 2007-04-03 2008-10-09 The Ohio State University Methods of producing butanol
WO2011031104A2 (ko) * 2009-09-14 2011-03-17 지에스칼텍스 주식회사 바이오 연료물질 및 바이오 화학물질 제조방법
US20110287498A1 (en) * 2009-01-26 2011-11-24 Xyleco, Inc. Processing biomass
US20110300596A1 (en) * 2008-12-12 2011-12-08 Sk Innovation Co., Ltd. Preparation method for alcohol from carboxylic acid by one-step process

Family Cites Families (439)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2422373A (en) 1943-08-18 1947-06-17 Gulf Oil Corp Rotary filter
US2674381A (en) 1946-08-27 1954-04-06 Ajax Flexible Coupling Co Inc Discrete material conveyer and distributor
US2606867A (en) * 1948-09-16 1952-08-12 Fmc Corp Gaseous phase photohalogenation of hydrocarbons
US2820165A (en) * 1951-07-13 1958-01-14 High Voltage Engineering Corp Means for cooling the windows of acceleration tubes for electrostatic generators
GB721235A (en) 1952-06-12 1955-01-05 High Voltage Engineering Corp Improvements in or relating to method of irradiating matter with electrons
US2985589A (en) 1957-05-22 1961-05-23 Universal Oil Prod Co Continuous sorption process employing fixed bed of sorbent and moving inlets and outlets
US2993120A (en) 1959-01-14 1961-07-18 High Voltage Engineering Corp Electron irradiation
US3132251A (en) * 1960-10-27 1964-05-05 Budd Co Irradiation vault
US3434850A (en) * 1966-07-29 1969-03-25 Us Interior Process for preserving fish by irradiation
JPS5028515B2 (es) 1971-09-30 1975-09-16
US3939286A (en) 1973-01-29 1976-02-17 Jelks James W Process for oxidizing and hydrolyzing plant organic matter particles to increase the digestability thereof by ruminants
JPS5077799A (es) * 1973-11-15 1975-06-25
US3934144A (en) 1974-04-11 1976-01-20 United States Steel Corporation X-ray machine for rapid and precise inspection of mixed sizes of pneumatic tires
US4049546A (en) * 1974-11-11 1977-09-20 Rohm And Haas Company Decolorization of effluents from pulp mills
DE2503010A1 (de) * 1975-01-25 1976-07-29 Werner & Pfleiderer Vorrichtung zur kontinuierlichen strahlenbehandlung von wirbelfaehigen und mischbaren stoffen
DE2538080C3 (de) * 1975-08-27 1978-05-24 Werner & Pfleiderer, 7000 Stuttgart Vorrichtung zur kontinuierlichen Strahlenbehandlung von wirbelfähigen und mischbaren Stoffen
JPS5346598A (en) * 1976-10-07 1978-04-26 Ebara Corp Cooling system and device of particle accelerator irradiation aperture
US4206034A (en) * 1977-02-17 1980-06-03 Exxon Research & Engineering Co. Wax separation process
US4086152A (en) * 1977-04-18 1978-04-25 Rp Industries, Inc. Ozone concentrating
DE2721316C3 (de) * 1977-05-04 1979-10-11 Gebrueder Sulzer Ag, Winterthur (Schweiz) Vorrichtung zum Bestrahlen fließbaren Gutes, insbesondere Klärschlamm, mittels Elektronenstrahlung
LU77536A1 (es) * 1977-06-14 1978-09-28
US4268505A (en) 1978-04-13 1981-05-19 Kureha Kagaku Kogyo Kabushiki Kaisha Pharmaceutical composition comprising a nitrogen-containing polysaccharide and an antibiotic agent, and a method of treating an infectious disease therewith
DE2962383D1 (en) 1978-06-15 1982-05-06 Ici Plc Anti-inflammatory 1-phenyl-2-aminoethanol derivatives, pharmaceutical compositions thereof for topical use, and processes for their manufacture
US4337152A (en) 1978-09-27 1982-06-29 Frebar Holding Ag Aeration apparatus and method
US4305000A (en) 1978-11-03 1981-12-08 Tetra Pak Developpement Ltd. Process of and apparatus for cold-cathode electron-beam generation for sterilization of surfaces and similar applications
US4275163A (en) 1978-11-20 1981-06-23 The United States Of America As Represented By The Secretary Of The Army Cellulase-producing microorganism
SU956478A1 (ru) 1978-11-27 1982-09-07 Предприятие П/Я М-5885 Способ получени фурфурилового спирта
EP0020101A1 (en) * 1979-05-25 1980-12-10 Bateman Equipment Limited Vacuum belt filter including vacuum sealing means
US4243750A (en) 1979-05-29 1981-01-06 National Distillers And Chemical Corp. Process for the hydrolysis of starch and the continuous fermentation of the sugars obtained therefrom to provide ethanol
US4274163A (en) 1979-07-16 1981-06-23 The Regents Of The University Of California Prosthetic fixation technique
DE2950014A1 (de) 1979-12-12 1981-06-19 Bayer Ag, 5090 Leverkusen Verfahren und vorrichtung fuer einen waschprozess im anschluss an das spinnen von chemiefasern
JPS5830274B2 (ja) * 1980-01-14 1983-06-28 日本原子力研究所 有機性廃棄物の新規堆肥化法
US4316747A (en) * 1980-03-18 1982-02-23 New York University Process for the chemical conversion of cellulose waste to glucose
DK187280A (da) 1980-04-30 1981-10-31 Novo Industri As Ruhedsreducerende middel til et fuldvaskemiddel fuldvaskemiddel og fuldvaskemetode
US4321328A (en) * 1980-12-05 1982-03-23 Hoge William H Process for making ethanol and fuel product
US4362965A (en) 1980-12-29 1982-12-07 The United States Of America As Represented By The Secretary Of The Army Composite/laminated window for electron-beam guns
JPS5858077B2 (ja) * 1981-11-12 1983-12-23 新燃料油開発技術研究組合 セルロ−ス質材酵素加水分解の前処理方法
US4482046A (en) 1982-04-15 1984-11-13 General Kinematics Corporation Flexible trough vibratory conveyor
US4664812A (en) * 1983-11-10 1987-05-12 Max Klein Liquid filtration apparatus and process
JPS60164494A (ja) * 1984-02-07 1985-08-27 Res Assoc Petroleum Alternat Dev<Rapad> セルロ−ス質材酵素加水分解の前処理方法
JPS6178390A (ja) * 1984-09-25 1986-04-21 Japan Atom Energy Res Inst セルロ−ス廃資源の糖化発酵における前処理方法
DE3518997C1 (de) * 1985-05-25 1986-08-21 Hermann Berstorff Maschinenbau Gmbh, 3000 Hannover Schneckenstrangpresse mit einer Zylindertemperiereinrichtung
JPS624129A (ja) * 1985-06-27 1987-01-10 Mitsubishi Heavy Ind Ltd 空気輸送装置
US4844878A (en) * 1985-10-04 1989-07-04 Fuel Tech, Inc. Process for the reduction of nitrogen oxides in an effluent
US4760264A (en) 1986-01-16 1988-07-26 Barrett Lawrence G Irradiator and method of using irradiator to irradiate
FR2596192B1 (fr) * 1986-03-20 1992-03-13 Conservatome Dispositif industriel polyvalent pour traitement par irradiation gamma
US5143834A (en) * 1986-06-11 1992-09-01 Glassner David A Process for the production and purification of succinic acid
US5247069A (en) 1986-06-13 1993-09-21 Oncogen Ligands and methods for augmenting B-cell proliferation
DE3769931D1 (de) * 1986-11-26 1991-06-13 Ebara Corp Verfahren zur behandlung eines nebenproduktes bei der bestrahlung eines abgases, dem ammoniak zugesetzt wurde.
JPS63185444A (ja) 1987-01-27 1988-08-01 Dynic Corp 電子線照射装置
USRE33935E (en) 1987-04-06 1992-05-26 Apparatus and method for feeding sintering raw mix
US5015274A (en) * 1987-05-07 1991-05-14 Mello Manufacturing, Inc. High efficiency industrial vacuum cleaner and filter element
JPH0622536B2 (ja) * 1987-07-01 1994-03-30 株式会社豊振科学産業所 粉粒体等の殺菌装置
US4968325A (en) * 1987-08-24 1990-11-06 Centre Quebecois De Valorisation De La Biomasse Fluidized bed gasifier
US4813532A (en) 1988-01-15 1989-03-21 Allen Fruit Co., Inc. Natural frequency vibratory conveyor
US4885247A (en) * 1988-04-19 1989-12-05 Michigan Biotechnology Institute Recovery and purification of lactate salts from whole fermentation broth by electrodialysis
IT1219942B (it) 1988-05-13 1990-05-24 Fidia Farmaceutici Esteri polisaccaridici
US6740731B2 (en) 1988-08-08 2004-05-25 Cargill Dow Polymers Llc Degradation control of environmentally degradable disposable materials
US6323307B1 (en) 1988-08-08 2001-11-27 Cargill Dow Polymers, Llc Degradation control of environmentally degradable disposable materials
DE3914502A1 (de) * 1989-05-02 1990-11-15 Goldschmidt Ag Th Verfahren zur erzielung und aufrechterhaltung einer sauerstoffarmen, inerten atmosphaere in einer behandlungskammer sowie vorrichtung zur durchfuehrung des verfahrens
US5055205A (en) 1989-05-24 1991-10-08 Alar Engineering Corporation Pressurized continuous operating rotary drum filter and method
US5024145A (en) 1989-08-28 1991-06-18 Flakee Mills, Inc. Vibratory bulk material processor and method
US5055204A (en) 1989-08-29 1991-10-08 Bogart John D Soil and sludge treatment apparatus and method including agitation, aeration and recirculation
US5131525A (en) 1989-10-17 1992-07-21 General Kinematics Corporation Vibratory conveyor
IL96555A0 (en) 1989-12-08 1991-09-16 Union Carbide Chem Plastic Process and apparatus for de-polluting circulated air
US5181715A (en) 1989-12-15 1993-01-26 Canon Kabushiki Kaisha Sheet conveying unit and system using the same
FI86440C (fi) 1990-01-15 1992-08-25 Cultor Oy Foerfarande foer samtidig framstaellning av xylitol och etanol.
US7109005B2 (en) 1990-01-15 2006-09-19 Danisco Sweeteners Oy Process for the simultaneous production of xylitol and ethanol
JPH0427386A (ja) 1990-05-24 1992-01-30 Kao Corp プロテアーゼ耐性セルラーゼ、これを産生する微生物及び該セルラーゼの製造法
US5530255A (en) 1990-08-17 1996-06-25 Raychem Corporation Apparatus and methods for electron beam irradiation
KR950000074B1 (ko) 1991-03-28 1995-01-09 금호석유화학 주식회사 이산화황과 핵치환 트리알킬게르밀스티렌(Trialkeylgermylstyrene)의 다원공중합체
WO1993005186A1 (en) 1991-09-11 1993-03-18 Easter James M Iii Process for the disposal of municipal waste and manufacture of fuel alcohol
IT1254119B (it) 1991-09-13 1995-09-08 Fidia Esteri di derivati carbossilici di polisaccaridi
JPH0530800U (ja) * 1991-09-30 1993-04-23 日新ハイボルテージ株式会社 電子線照射装置
US5244553A (en) 1991-10-31 1993-09-14 North Carolina State University Method for recovering acid from an acid-sugar hydrolyzate
US5247058A (en) 1992-01-24 1993-09-21 Cargill, Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US6326458B1 (en) 1992-01-24 2001-12-04 Cargill, Inc. Continuous process for the manufacture of lactide and lactide polymers
US5142023A (en) 1992-01-24 1992-08-25 Cargill, Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US6005067A (en) 1992-01-24 1999-12-21 Cargill Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US5258488A (en) 1992-01-24 1993-11-02 Cargill, Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US5247059A (en) 1992-01-24 1993-09-21 Cargill, Incorporated Continuous process for the manufacture of a purified lactide from esters of lactic acid
ES2214654T3 (es) * 1992-02-06 2004-09-16 Jeremy Wickins Tratamiento de aguas cloacales.
BR9207135A (pt) 1992-05-29 1996-11-19 Kvaerner Pulping Tech Um processo para recuperar energia de um gas combustivel
JP3167800B2 (ja) 1992-07-31 2001-05-21 株式会社東芝 オンライン文字入力装置
US5378898A (en) * 1992-09-08 1995-01-03 Zapit Technology, Inc. Electron beam system
US5457269A (en) * 1992-09-08 1995-10-10 Zapit Technology, Inc. Oxidizing enhancement electron beam process and apparatus for contaminant treatment
ES2123668T3 (es) 1992-10-02 1999-01-16 Cargill Inc Papel que tiene un recubrimiento de polimero de lactida estable en estado fundido y procedimiento para su fabricacion.
DE69330046T2 (de) 1992-10-02 2001-11-15 Cargill Inc Schmelzstabiles lactidpolymergewebe und verfahren zu seiner herstellung
US5338822A (en) 1992-10-02 1994-08-16 Cargill, Incorporated Melt-stable lactide polymer composition and process for manufacture thereof
US6005068A (en) 1992-10-02 1999-12-21 Cargill Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US5426024A (en) 1992-10-23 1995-06-20 Centro De Investigacion Y De Estudios Avanzados Del Instituto Politecnico Nacional Fermentation method and fermentor
US5401973A (en) * 1992-12-04 1995-03-28 Atomic Energy Of Canada Limited Industrial material processing electron linear accelerator
JPH0651900U (ja) * 1992-12-18 1994-07-15 日新ハイボルテージ株式会社 電子線照射装置
FI96225C (fi) * 1993-01-26 1996-05-27 Cultor Oy Menetelmä melassin fraktioimiseksi
US5396074A (en) 1993-03-19 1995-03-07 The Titan Corporation Irradiation system utilizing conveyor-transported article carriers
US5562777A (en) 1993-03-26 1996-10-08 Arkenol, Inc. Method of producing sugars using strong acid hydrolysis of cellulosic and hemicellulosic materials
IT1262513B (it) 1993-05-11 1996-07-02 Proel Tecnologie Spa Impianto itinerante per irraggiamento a fasci di elettroni accelerati con sistemi elettronici.
IT1262524B (it) 1993-07-23 1996-07-02 Marco Maltagliati Procedimento per il miglioramento delle caratteristiche di oli combustibili, in particolare di oli da pirolisi di biomasse
DE4326146A1 (de) 1993-08-04 1995-02-09 Koeberlein Josef Masch Vibrations-Linear-Förderer
JPH07155191A (ja) * 1993-12-08 1995-06-20 Musashino Kagaku Kenkyusho:Kk 乳酸の発酵方法
US6268196B1 (en) 1993-12-17 2001-07-31 Genencor International, Inc. Method and compositions for treating cellulose containing fabrics using truncated cellulase enzyme compositions
CA2142230A1 (en) 1994-03-21 1995-09-22 Samuel V. Nablo Data reduction system for real time monitoring of radiation machinery
US5574129A (en) 1994-05-10 1996-11-12 The Japan Steel Works, Ltd. Process for producing lactic acid polymers and a process for the direct production of shaped articles from lactic acid polymers
US5581998A (en) * 1994-06-22 1996-12-10 Craig; Joe D. Biomass fuel turbine combuster
JP3488524B2 (ja) 1994-12-12 2004-01-19 日本原子力研究所 電子ビーム照射設備の照射窓装置
JP3569329B2 (ja) 1994-12-12 2004-09-22 日本原子力研究所 電子ビーム照射設備の照射窓装置
US5621270A (en) 1995-03-22 1997-04-15 Litton Systems, Inc. Electron window for toxic remediation device with a support grid having diverging angle holes
JP3965220B2 (ja) * 1995-09-14 2007-08-29 サンエイ糖化株式会社 有機酸の製造方法
US5849401A (en) 1995-09-28 1998-12-15 Cargill, Incorporated Compostable multilayer structures, methods for manufacture, and articles prepared therefrom
CA2159531A1 (en) 1995-09-29 1997-03-30 Courtland B. Lawrence Method for monitoring absorbed dose in an electron beam
KR0152482B1 (ko) * 1995-09-29 1998-10-01 최차용 발효에 의한 균주 대사산물의 연속적 제조 방법
JP3291437B2 (ja) * 1995-10-17 2002-06-10 株式会社荏原製作所 電子ビーム加速器の窓箔冷却方法および装置
US5753474A (en) 1995-12-26 1998-05-19 Environmental Energy, Inc. Continuous two stage, dual path anaerobic fermentation of butanol and other organic solvents using two different strains of bacteria
AU1524597A (en) * 1996-01-11 1997-08-01 Energy And Environmental Research Corporation Improved advanced reburning methods for high efficiency nox control
US5898261A (en) * 1996-01-31 1999-04-27 The United States Of America As Represented By The Secretary Of The Air Force Fluid-cooled particle-beam transmission window
JPH09222500A (ja) * 1996-02-19 1997-08-26 Iwasaki Electric Co Ltd 電子線照射装置
US6452051B1 (en) 1996-02-22 2002-09-17 Cargill, Inc. Process for the production of a condensation products of a carboxylic acid
JPH09262528A (ja) * 1996-03-27 1997-10-07 Nissin High Voltage Co Ltd 電子線照射処理装置
CA2627832C (en) * 1996-03-28 2012-12-11 Dsm Ip Assets B.V. Preparation of microbial polyunsaturated fatty acid containing oil from pasteurised biomass
HU221997B1 (hu) * 1996-04-02 2003-03-28 Urban Stricker Berendezés ömlesztett anyagok hőkezelésére
US5998402A (en) 1996-04-19 1999-12-07 American Home Products Corporation 2-phenyl-1-[4-(2-aminoethoxy)-benzyl]-indoles as estrogenic agents
US6620385B2 (en) * 1996-08-20 2003-09-16 Ebara Corporation Method and apparatus for purifying a gas containing contaminants
IL119387A (en) 1996-10-09 2001-06-14 Cargill Inc Process for the recovery of lactic acid by liquid-liquid extraction with a basic extractant
US6160173A (en) 1996-10-09 2000-12-12 Cargill Incorporated Process for the recovery of lactic acid esters and amides from aqueous solutions of lactic acid and/or salts thereof
DE59704688D1 (de) 1996-10-12 2001-10-25 Koenig & Bauer Ag Fördereinrichtung
US6011008A (en) 1997-01-08 2000-01-04 Yissum Research Developement Company Of The Hebrew University Of Jerusalem Conjugates of biologically active substances
US20030129274A1 (en) * 1997-03-13 2003-07-10 Garwood Anthony J.M. Irradiation in enclosed conduit method and apparatus
WO1998050611A1 (en) 1997-05-02 1998-11-12 Cargill, Incorporated Degradable polymer fibers; preperation; product; and methods of use
US5994706A (en) 1997-05-09 1999-11-30 Titan Corporation Article irradiation system in which article-transporting conveyor is closely encompassed by shielding material
US6183814B1 (en) 1997-05-23 2001-02-06 Cargill, Incorporated Coating grade polylactide and coated paper, preparation and uses thereof, and articles prepared therefrom
US5916780A (en) 1997-06-09 1999-06-29 Iogen Corporation Pretreatment process for conversion of cellulose to fuel ethanol
US5916929A (en) 1997-06-23 1999-06-29 E-Beam Services, Inc. Method for irradiating organic polymers
US5968362A (en) * 1997-08-04 1999-10-19 Controlled Enviromental Systems Corporation Method for the separation of acid from sugars
JP3231678B2 (ja) * 1997-09-30 2001-11-26 岡谷電機産業株式会社 オゾン発生器
US6229046B1 (en) 1997-10-14 2001-05-08 Cargill, Incorported Lactic acid processing methods arrangements and products
DE19756171A1 (de) * 1997-12-17 1999-07-01 Basf Ag Verfahren zur Hydrierung von Carbonsäuren oder deren Anhydriden oder Estern zu Alkoholen
JPH11192078A (ja) * 1997-12-29 1999-07-21 Yasuma Kk 低エネルギー電子線による植物性食品の殺菌方法
US5876505A (en) 1998-01-13 1999-03-02 Thermo Fibergen, Inc. Method of producing glucose from papermaking sludge using concentrated or dilute acid hydrolysis
US5882737A (en) 1998-03-20 1999-03-16 Eckhoff; Paul S. Apparatus and method for radiation processing of materials
JPH11266894A (ja) * 1998-03-25 1999-10-05 Towa Chem Ind Co Ltd Ｄ−キシロースの製造方法
US6114495A (en) 1998-04-01 2000-09-05 Cargill Incorporated Lactic acid residue containing polymer composition and product having improved stability, and method for preparation and use thereof
US6140458A (en) 1998-04-28 2000-10-31 Mitsui Chemicals, Inc. Preparation process of polyester
JP3648537B2 (ja) * 1998-05-25 2005-05-18 株式会社Ｎｈｖコーポレーション 電子線照射装置
US6127687A (en) 1998-06-23 2000-10-03 Titan Corp Article irradiation system having intermediate wall of radiation shielding material within loop of conveyor system that transports the articles
US7193129B2 (en) 2001-04-18 2007-03-20 Mendel Biotechnology, Inc. Stress-related polynucleotides and polypeptides in plants
ID29093A (id) 1998-10-16 2001-07-26 Lanisco Holdings Ltd Konversi mendalam yang menggabungkan demetalisasi dan konversi minyak mentah, residu atau minyak berat menjadi cairan ringan dengan senyawa-senyawa oksigenat murni atau tak murni
US6545398B1 (en) 1998-12-10 2003-04-08 Advanced Electron Beams, Inc. Electron accelerator having a wide electron beam that extends further out and is wider than the outer periphery of the device
BR0007813A (pt) * 1999-01-11 2001-11-06 Ebara Corp Aparelho de reação de irradiação com feixe de elétrons
US6589760B1 (en) * 1999-02-10 2003-07-08 Eastman Chemical Company Methods of separating a corn fiber lipid fraction from corn fiber
US6528800B1 (en) 1999-03-03 2003-03-04 Steris, Inc. Particulate curing system
JP2000254486A (ja) 1999-03-09 2000-09-19 Nissin High Voltage Co Ltd 電子線照射装置と電子線照射方法及び被処理物
US7074603B2 (en) * 1999-03-11 2006-07-11 Zeachem, Inc. Process for producing ethanol from corn dry milling
ES2400285T3 (es) * 1999-03-11 2013-04-08 Zeachem, Inc. Proceso para producir etanol
JP2000304900A (ja) * 1999-04-22 2000-11-02 Natl Food Res Inst 電子線照射装置と粒状体殺菌方法
US6217630B1 (en) 1999-05-03 2001-04-17 Cargill, Incorporated Conditioned fertilizer product, method for conditioning fertilizer, and method for using conditioned fertilizer product
KR100395076B1 (ko) 1999-06-22 2003-08-19 미쯔이카가쿠 가부시기가이샤 폴리하이드록시카르복시산의 제조방법
US7537826B2 (en) 1999-06-22 2009-05-26 Xyleco, Inc. Cellulosic and lignocellulosic materials and compositions and composites made therefrom
US20020102672A1 (en) 1999-10-04 2002-08-01 Joseph Mizrahi Process for producing a purified lactic acid solution
JP2001108800A (ja) * 1999-10-05 2001-04-20 Nissin High Voltage Co Ltd 電子線照射装置
US6713773B1 (en) 1999-10-07 2004-03-30 Mitec, Inc. Irradiation system and method
US6528617B1 (en) 1999-10-27 2003-03-04 Mitsui Chemicals, Inc. Process for producing aliphatic polyester excellent in stability
TR200201914T2 (tr) * 1999-11-05 2002-11-21 Saudi American Minerals, Inc. Kömüre yapılan muamele
CA2400336C (en) 2000-02-17 2010-04-27 Forskningscenter Riso A method for processing lignocellulosic material
JP2001235600A (ja) * 2000-02-22 2001-08-31 Nissin High Voltage Co Ltd 電子線照射装置の窓箔と電子線照射装置
US6653641B2 (en) * 2000-02-24 2003-11-25 Mitec Incorporated Bulk material irradiation system and method
JP2001242297A (ja) 2000-02-28 2001-09-07 Nissin High Voltage Co Ltd 電子線照射方法及び装置
ATE331233T1 (de) 2000-03-20 2006-07-15 California Inst Of Techn Anwendung eines wellenfrontsensors bei linsen mit nach der herstellung modifizierbarer brechkraft
US6707049B1 (en) 2000-03-21 2004-03-16 Mitec Incorporated Irradiation system with compact shield
JP2003531750A (ja) * 2000-05-03 2003-10-28 デイビス − スタンダード コーポレイション 木材繊維を処理するためのツイン・スクリュー押出機およびその方法
JP3777080B2 (ja) * 2000-05-08 2006-05-24 株式会社Ｎｈｖコーポレーション 電子線照射装置
JP2001318200A (ja) 2000-05-08 2001-11-16 Nissin High Voltage Co Ltd 電子線照射装置
US6623705B2 (en) * 2000-06-20 2003-09-23 Advanced Electron Beams, Inc. Gas conversion system
JP2002045159A (ja) * 2000-08-04 2002-02-12 Mitsubishi Heavy Ind Ltd 電子線殺菌装置
US6588363B1 (en) 2000-08-17 2003-07-08 Paul J. Svejkovsky Seasoning system and method
JP2002085029A (ja) * 2000-09-07 2002-03-26 Nisshin Seifun Group Inc 電子線照射装置
JP3804042B2 (ja) * 2000-09-07 2006-08-02 株式会社日清製粉グループ本社 電子線照射装置
JP2002096049A (ja) * 2000-09-25 2002-04-02 Waya Izumida 生ごみ処理方法および装置
US6800197B1 (en) 2000-10-12 2004-10-05 Genencor International, Inc. Continuously operable rotating drum pressure differential filter, method and systems
US20090203079A1 (en) 2000-10-20 2009-08-13 Board Of Trustees Of Michigan State University Transgenic monocot plants encoding beta-glucosidase and xylanase
CN1290735A (zh) * 2000-11-06 2001-04-11 卢朴真 柴草燃气及其生产方法和装置
US6628750B1 (en) 2000-11-09 2003-09-30 Steris Inc. System for electron and x-ray irradiation of product
JP2002210434A (ja) 2000-11-17 2002-07-30 Mitsubishi Heavy Ind Ltd ハロゲン化有機化合物の分解処理方法およびその装置
MXPA03004324A (es) 2000-11-20 2004-01-26 Cargill Inc Acido 3-hidroxipropionico y otros compuestos organicos.
US8690971B2 (en) * 2001-01-10 2014-04-08 State Line Holdings, LLC. Method of improving combustion of solid fuels using evenly distributed catalysts or other agents
US6455301B1 (en) 2001-01-12 2002-09-24 Food Industry Research And Develpment Institute Erythritol—producing Moniliella strains
JP2002224656A (ja) * 2001-01-31 2002-08-13 Toda Constr Co Ltd 汚染土壌の処理方法および処理装置
US6780448B1 (en) 2001-02-06 2004-08-24 David Howard Pasteurization of food products
JP2002238590A (ja) * 2001-02-14 2002-08-27 Tsukishima Kikai Co Ltd 乳酸の製造方法
EP1232780B2 (de) * 2001-02-20 2014-10-29 Sefar AG Filtertuch
EP1389338B1 (en) 2001-03-20 2012-10-03 Hitachi Zosen Corporation Electron beam irradiation apparatus
US20020135290A1 (en) * 2001-03-21 2002-09-26 Advanced Electron Beams, Inc. Electron beam emitter
FI20010977A (fi) * 2001-05-09 2002-11-10 Danisco Sweeteners Oy Kromatografinen erotusmenetelmä
US6973758B2 (en) * 2001-05-14 2005-12-13 Rad Technology, Llc Shielded structure for radiation treatment equipment and method of assembly
US6575084B2 (en) 2001-06-01 2003-06-10 Surebeam Corporation, Inc. System for, and method of, irradiating food products
US6608882B2 (en) 2001-06-13 2003-08-19 Surebeam Corporation System for, and method of, irradiating articles particularly articles with variable dimensions
DE60226931D1 (de) 2001-07-16 2008-07-17 Canon Kk Verfahren zur Herstellung von Polyester, Verfahren zur Herstellung von substituierter alpha-Hydroxycarbonsäure und Clostridium beijerinckii-Stamm HICA432
CA2454823A1 (en) * 2001-07-24 2003-02-06 Arkenol, Inc. Separation of xylose and glucose
JP2003111356A (ja) 2001-10-01 2003-04-11 Mitsubishi Electric Corp 空気冷却式全閉形回転電機
US6750461B2 (en) 2001-10-03 2004-06-15 Si Diamond Technology, Inc. Large area electron source
US6690020B2 (en) * 2001-10-04 2004-02-10 Surebeam Corporation Compact self-shielded irradiation system and method
US6932286B2 (en) 2001-11-07 2005-08-23 Fred P. Smith Combination drop and broadcast spreader
US7019155B2 (en) 2001-11-13 2006-03-28 Invista North America S.A.R.L. Hydrogenation of tetrahydroxybutane to tetrahydrofuran
US6777689B2 (en) 2001-11-16 2004-08-17 Ion Beam Application, S.A. Article irradiation system shielding
US6583423B2 (en) 2001-11-16 2003-06-24 Ion Beam Applications, S.A. Article irradiation system with multiple beam paths
JP3875550B2 (ja) * 2001-12-17 2007-01-31 清水建設株式会社 滅菌無害化施設
CN1171839C (zh) * 2001-12-21 2004-10-20 淄博广通化工有限责任公司 α,ω- 长碳链二元醇的生产方法
FI114553B (fi) * 2001-12-31 2004-11-15 Danisco Sweeteners Oy Menetelmä sokereiden ottamiseksi talteen
MXPA04006894A (es) 2002-01-18 2004-10-15 Cargill Inc Alanina 2,3 - aminomutasa.
PT1468093E (pt) * 2002-01-23 2009-04-15 Royal Nedalco B V Fermentação de açúcares pentose
US20030203454A1 (en) 2002-02-08 2003-10-30 Chotani Gopal K. Methods for producing end-products from carbon substrates
US6838678B1 (en) 2002-04-10 2005-01-04 Seagate Technology Llc Apparatus for inline continuous and uniform ultraviolet irradiation of recording media
US20040005674A1 (en) 2002-04-30 2004-01-08 Athenix Corporation Methods for enzymatic hydrolysis of lignocellulose
US20050260311A1 (en) * 2002-06-03 2005-11-24 Garwood Anthony J Decontamination methods for meat using carbonic acid at high pressures
WO2004003934A1 (en) * 2002-07-01 2004-01-08 Elekta Ab (Publ) A mobile building unit as well as a building and a method for constructing the building
US7356115B2 (en) 2002-12-04 2008-04-08 Varian Medical Systems Technology, Inc. Radiation scanning units including a movable platform
CA2404798C (en) 2002-09-24 2007-02-20 Edward W. Chan Nozzle/mixer assembly
WO2004038032A1 (en) * 2002-10-22 2004-05-06 Purac Biochem B.V. Separation of biomass from lactic acid containing fermentation products by means of flocculation
EP1415702A1 (en) * 2002-10-28 2004-05-06 PURAC Biochem BV Method of separating multivalent ions and lactate ions from a fermentation broth
US6808600B2 (en) 2002-11-08 2004-10-26 Kimberly-Clark Worldwide, Inc. Method for enhancing the softness of paper-based products
US7391784B1 (en) 2002-12-30 2008-06-24 3Com Corporation Method and system for communicating state information between devices of a communications network
US7083955B2 (en) 2003-01-13 2006-08-01 Purac Biochem Bv Preparation of lactic acid from a pentose-containing substrate
US7704460B2 (en) * 2003-02-03 2010-04-27 Advanced Electron Beams, Inc. Gas separation device
US20040222157A1 (en) 2003-02-18 2004-11-11 Minhas Bhupender S. Process for the recovery of sulfuric acid using polymeric membranes
US7604967B2 (en) 2003-03-19 2009-10-20 The Trustees Of Dartmouth College Lignin-blocking treatment of biomass and uses thereof
JP4372442B2 (ja) * 2003-03-28 2009-11-25 東京エレクトロン株式会社 電子ビーム処理方法及び電子ビーム処理装置
US20070215821A1 (en) 2003-05-01 2007-09-20 Stirling Andrew J Shielded Irradiation Zone Of Production Line
US7217545B2 (en) 2003-05-14 2007-05-15 Wessex Incorporated Method for production of lactic acid
JP3962360B2 (ja) * 2003-06-13 2007-08-22 日本スピンドル製造株式会社 使用済み濾布の無害化装置
CN1199976C (zh) * 2003-07-03 2005-05-04 华东理工大学 电渗析法分离生物质水解液中糖和酸
PL1649068T3 (pl) * 2003-07-16 2013-07-31 Amalgamated Res Llc Sposób oczyszczania materiału sacharozowego o wysokiej czystości
JP4309196B2 (ja) * 2003-07-25 2009-08-05 日揮株式会社 擬似移動層クロマト分離方法
WO2005017159A2 (en) * 2003-08-14 2005-02-24 Dsm Ip Assets B.V. Microbial production of l-ascorbic acid
US20050112248A1 (en) * 2003-11-26 2005-05-26 Galloway Richard A. Electron beam carcass irradiation system
MX306561B (es) * 2004-01-29 2013-01-09 Zeachem Inc Recuperacion de acidos organicos.
NO321595B1 (no) * 2004-02-27 2006-06-06 Visuray As Apparat og framgangsmate for innsamling av radioaktivt materiale fra en lagringsbeholder
US7098009B2 (en) 2004-03-04 2006-08-29 University Of Florida Research Foundation, Inc. Production of chemicals from lignocellulose, biomass or sugars
CN100528304C (zh) * 2004-03-17 2009-08-19 Ge爱奥尼克斯公司 用于有机产物的生产线和处理
PT3219806T (pt) * 2004-03-25 2020-06-30 Novozymes Inc Métodos para degradar ou converter polissacarídeos da parede celular de plantas
JP2007532587A (ja) * 2004-04-13 2007-11-15 アイオゲン エナジー コーポレイション リグノセルロース処理における無機塩回収方法
US20050269254A1 (en) * 2004-05-24 2005-12-08 Roitman Lipa L [Air and Water Purifying System And Filter Media]
DE102004026152A1 (de) * 2004-05-28 2005-12-15 Basf Ag Fermentative Herstellung von Feinchemikalien
JP4866845B2 (ja) * 2004-06-16 2012-02-01 ザ テキサス エイ・アンド・エム ユニヴァーシティ システム カルボン酸及びアルコールへのバイオマスの転換用の方法及び系
US8146894B2 (en) 2004-06-21 2012-04-03 Hills Blair H Apparatus for mixing gasses and liquids
TW200613560A (en) * 2004-06-29 2006-05-01 Procter & Gamble Solvent extraction of polyhydroxyalkanoates from biomass
WO2006007691A1 (en) 2004-07-16 2006-01-26 Iogen Energy Corporation Method of obtaining a product sugar stream from cellulosic biomass
FR2874931B1 (fr) * 2004-09-08 2006-11-24 Aventis Pharma Sa Procede de production de polysaccharide k5
US7402428B2 (en) 2004-09-22 2008-07-22 Arborgen, Llc Modification of plant lignin content
DK176540B1 (da) 2004-09-24 2008-07-21 Cambi Bioethanol Aps Fremgangsmåde til behandling af biomasse og organisk affald med henblik på at udvinde önskede biologisk baserede produkter
CN101035632B (zh) * 2004-09-30 2011-06-08 埃欧金能量有限公司 一种预处理木质纤维素原料的连续方法
US7909895B2 (en) * 2004-11-10 2011-03-22 Enertech Environmental, Inc. Slurry dewatering and conversion of biosolids to a renewable fuel
WO2006073521A2 (en) 2005-01-03 2006-07-13 Western Oil Sands, Inc. Nozzle reactor and method of use
EP1690828A1 (en) 2005-02-11 2006-08-16 Nederlandse Organisatie voor toegepast-natuurwetenschappelijk onderzoek TNO Recovery of sulphuric acid
JP2006238728A (ja) 2005-03-01 2006-09-14 Nippon Paper Chemicals Co Ltd 製紙排水からの糖類の製造方法
JP2008532021A (ja) 2005-03-04 2008-08-14 エフピーイノベイションズ 可視・近赤外分光測定法により化学パルプのカッパー価を測定する方法
EP2508263B1 (en) 2005-03-24 2015-11-25 Xyleco, Inc. Method of densifying fibrous material
AT501149B8 (de) 2005-03-24 2007-02-15 Voest Alpine Ind Anlagen Verfahren und vorrichtung zur behandlung von abgas aus sinteranlagen
JP2006281174A (ja) * 2005-04-05 2006-10-19 Matsushita Electric Ind Co Ltd 排水のリサイクル処理方法及び排水リサイクル処理装置並びに排水リサイクル処理システム
US7781191B2 (en) * 2005-04-12 2010-08-24 E. I. Du Pont De Nemours And Company Treatment of biomass to obtain a target chemical
JP5804666B2 (ja) * 2005-04-12 2015-11-04 イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニーＥ．Ｉ．Ｄｕ Ｐｏｎｔ Ｄｅ Ｎｅｍｏｕｒｓ Ａｎｄ Ｃｏｍｐａｎｙ バイオマスの処理および利用における別の供給流れの集中
WO2006113683A2 (en) 2005-04-19 2006-10-26 Archer-Daniels-Midland Company Process for the production of animal feed and ethanol and novel feed
WO2006115226A1 (ja) 2005-04-22 2006-11-02 Mitsubishi Chemical Corporation バイオマス資源由来ポリエステル及びその製造方法
CN1320122C (zh) * 2005-06-02 2007-06-06 江南大学 一种从木糖母液或木糖水解液提取木糖和木糖醇的方法
JP2007007604A (ja) * 2005-07-01 2007-01-18 Sanki Eng Co Ltd 電子線照射装置
RU2432368C2 (ru) 2005-07-19 2011-10-27 Инбикон А/С Способ превращения целлюлозного материала в этанол
WO2007019505A2 (en) * 2005-08-05 2007-02-15 The Trustees Of Dartmouth College Method and apparatus for saccharide precipitation from pretreated lignocellulosic materials
JP2007051996A (ja) 2005-08-19 2007-03-01 Ngk Insulators Ltd 電子線照射装置
US7608689B2 (en) 2005-09-30 2009-10-27 Novozymes, Inc. Methods for enhancing the degradation or conversion of cellulosic material
FI20051145A0 (fi) 2005-11-11 2005-11-11 Kemira Oyj Uusi massa ja menetelmä massan valmistamiseksi
US20070134781A1 (en) 2005-12-12 2007-06-14 Agblevor Foster A Method for producing bioethanol from a lignocellulosicbiomass and recycled paper sludge
JP2007217158A (ja) * 2006-02-20 2007-08-30 Nippon Spindle Mfg Co Ltd 粉粒体の空気輸送装置
US7913854B2 (en) 2006-03-07 2011-03-29 Bratten Jack R Filter apparatus and method with simplified filter belt indexing and sealing
DE102006026521A1 (de) * 2006-06-06 2007-12-13 Uhde Gmbh Bodenkonstruktion für horizontale Koksöfen
CN101490269B (zh) * 2006-07-14 2013-09-18 Scf科技公司 制备生物乙醇及其它发酵产品的方法和设备
US20080026431A1 (en) * 2006-07-19 2008-01-31 Taisei Corporation Method for saccharification of woody biomass
AP2724A (en) 2006-07-21 2013-08-31 Xyleco Inc Conversion systems for biomass
CA2661284A1 (en) 2006-08-11 2008-02-21 Cargill, Incorporated System for gluten replacement in food products
BRPI0716212A2 (pt) 2006-08-30 2013-10-15 Cargill Inc Beta-alanina/alfa-cetoglutarato aminotransferase para produção de ácido 3-hidroxipropiônico
US7629156B2 (en) * 2006-09-28 2009-12-08 E.I. Du Pont De Nemours And Company Ethanol production in fermentation of mixed sugars containing xylose
US8038744B2 (en) 2006-10-02 2011-10-18 Clark Steve L Reduced-emission gasification and oxidation of hydrocarbon materials for hydrogen and oxygen extraction
AT504230B1 (de) 2006-10-03 2008-06-15 Jungbunzlauer Austria Ag Verfahren zur herstellung von erythrit
US7670813B2 (en) * 2006-10-25 2010-03-02 Iogen Energy Corporation Inorganic salt recovery during processing of lignocellulosic feedstocks
US20100124583A1 (en) * 2008-04-30 2010-05-20 Xyleco, Inc. Processing biomass
RU2432400C2 (ru) 2006-10-26 2011-10-27 Ксилеко, Инк. Переработка биомассы
KR101171922B1 (ko) 2006-10-26 2012-08-07 질레코 인코포레이티드 바이오매스 처리방법
CN101202127B (zh) * 2006-12-14 2010-05-19 同方威视技术股份有限公司 一种建造射线屏蔽室的模块式屏蔽方法
JP4928254B2 (ja) 2006-12-28 2012-05-09 日本製紙株式会社 セルロース含有物の糖化方法
KR101108789B1 (ko) * 2007-02-09 2012-03-13 씨제이제일제당 (주) 열대과일 바이오매스 부산물로부터 제조된 자일로스와아라비노스를 포함하는 가수분해 당화액을 이용한자일리톨의 제조방법
ITMI20070350A1 (it) * 2007-02-23 2008-08-24 Univ Milano Bicocca Metodo di lavorazine a plasma atmosferico per il trattamento dei materiali
US20090007484A1 (en) 2007-02-23 2009-01-08 Smith David G Apparatus and process for converting biomass feed materials into reusable carbonaceous and hydrocarbon products
CN101765663B (zh) * 2007-03-14 2014-11-05 托莱多大学 生物质预处理
WO2008124162A2 (en) * 2007-04-09 2008-10-16 University Of Georgia Research Foundation, Inc. Substrate-selective co-fermentation process
EP2158167A4 (en) 2007-05-31 2012-05-23 Lignol Innovations Ltd AT THE SAME TIME ANAEROUS CONCLUSION AND FERMENTATION OF LIGNOCELLULOSIC MATERIALS
KR100873700B1 (ko) 2007-06-25 2008-12-12 사단법인 한국가속기 및 플라즈마 연구협회 전자빔을 이용한 바이오 연료 제조 방법
WO2009009323A1 (en) * 2007-07-06 2009-01-15 Best Energies, Inc. Improved homoacidogenic fermentation and indirect process for producing alcohols
KR100879317B1 (ko) * 2007-07-06 2009-01-19 한국과학기술연구원 부티르산의 화학 촉매 반응에 의한 부탄올 제조방법
US7774472B2 (en) 2007-07-23 2010-08-10 Novell, Inc. System and method for cross-authoritative configuration management
WO2009018469A1 (en) * 2007-07-31 2009-02-05 Hoffman Richard B System and method of preparing pre-treated biorefinery feedstock from raw and recycled waste cellulosic biomass
US8980599B2 (en) * 2007-08-02 2015-03-17 Iogen Energy Corporation Method for the production of alcohol from a pretreated lignocellulosic feedstock
JP4992019B2 (ja) * 2007-08-10 2012-08-08 公益財団法人地球環境産業技術研究機構 酸とアルカリの製造方法
RU2505588C2 (ru) * 2007-08-17 2014-01-27 Милан ПТАШЕК Топливо, способ и установка для получения тепловой энергии из биомассы
US7807419B2 (en) * 2007-08-22 2010-10-05 E. I. Du Pont De Nemours And Company Process for concentrated biomass saccharification
US7819976B2 (en) * 2007-08-22 2010-10-26 E. I. Du Pont De Nemours And Company Biomass treatment method
CN101835727B (zh) * 2007-08-30 2013-08-07 埃欧金能源公司 从糖的水溶液中除去钙并获得硫酸盐的方法
US7993616B2 (en) * 2007-09-19 2011-08-09 C-Quest Technologies LLC Methods and devices for reducing hazardous air pollutants
CN101392009B (zh) * 2007-09-21 2011-05-11 山东龙力生物科技股份有限公司 木糖生产工艺
US20090087518A1 (en) * 2007-09-27 2009-04-02 Kevin Moore Heteromorphic Lysine Feed Granules
JP5498005B2 (ja) * 2007-10-11 2014-05-21 志朗 坂 有機酸を経由したアルコール類の製造方法
CN101821397A (zh) * 2007-10-12 2010-09-01 丹尼斯科美国公司 从发酵微生物中提高有机物产生的方法和组合物
US8250955B2 (en) 2007-10-22 2012-08-28 Formax, Inc. Food article transfer mechanism for a food article slicing machine
DE102007052471A1 (de) * 2007-11-02 2009-05-07 Krones Ag Kontinuierliches Brauen
JP2009119678A (ja) * 2007-11-14 2009-06-04 National Printing Bureau 厚膜印刷物の作製方法
GB0725308D0 (en) * 2007-12-28 2008-02-06 Holliday R Combined heater and conveyor
US20100323063A1 (en) * 2008-01-04 2010-12-23 Corn Products International, Inc. Process for the preparation of isomaltooligosaccharide-hydrogenated
GB0801787D0 (en) * 2008-01-31 2008-03-05 Reclaim Resources Ltd Apparatus and method for treating waste
CN101497903B (zh) * 2008-02-01 2011-12-07 唐传生物科技（厦门）有限公司 一种选择性转化分流生物制品的方法
US8641910B2 (en) * 2008-02-05 2014-02-04 Syngenta Participations Ag Systems and processes for producing biofuels from biomass
JP2009233958A (ja) * 2008-03-26 2009-10-15 Dainippon Printing Co Ltd 防湿化粧シート
KR101588052B1 (ko) * 2008-03-28 2016-01-25 에스케이이노베이션 주식회사 발효액으로부터 부티르산을 추출하고 부티르산을 바이오연료로 화학적으로 전환하는 방법
US9638414B2 (en) * 2008-04-07 2017-05-02 Wastedry Llc Systems and methods for processing municipal wastewater treatment sewage sludge
CN101294169B (zh) * 2008-04-28 2012-01-11 河南金丹乳酸科技股份有限公司 钠盐发酵电渗析提取乳酸新工艺
RU2015127761A (ru) * 2008-04-30 2015-10-20 Ксилеко, Инк. Переработка биомассы
US8212087B2 (en) * 2008-04-30 2012-07-03 Xyleco, Inc. Processing biomass
US7931784B2 (en) 2008-04-30 2011-04-26 Xyleco, Inc. Processing biomass and petroleum containing materials
US8236535B2 (en) 2008-04-30 2012-08-07 Xyleco, Inc. Processing biomass
US8911833B2 (en) 2008-04-30 2014-12-16 Xyleco, Inc. Textiles and methods and systems for producing textiles
US7867359B2 (en) 2008-04-30 2011-01-11 Xyleco, Inc. Functionalizing cellulosic and lignocellulosic materials
US7867358B2 (en) 2008-04-30 2011-01-11 Xyleco, Inc. Paper products and methods and systems for manufacturing such products
US7846295B1 (en) 2008-04-30 2010-12-07 Xyleco, Inc. Cellulosic and lignocellulosic structural materials and methods and systems for manufacturing such materials
EP2128226A1 (en) 2008-05-19 2009-12-02 Furanix Technologies B.V Fuel component
JP4678066B2 (ja) 2008-05-21 2011-04-27 東レ株式会社 脂肪族ポリエステル樹脂の製造方法および脂肪族ポリエステル樹脂組成物
US8025098B2 (en) 2008-06-18 2011-09-27 Xyleco, Inc. Processing hydrocarbons
AU2009260197B2 (en) 2008-06-18 2014-03-27 Xyleco, Inc. Processing materials with ion beams
CA2765878A1 (en) * 2008-06-19 2009-12-23 Microcoal, Inc. System and method for treatment of materials by electromagnetic radiation (emr)
WO2009155601A2 (en) 2008-06-20 2009-12-23 Edenspace Systems Corporation Processing cellulosic biomass
JP5233452B2 (ja) * 2008-07-08 2013-07-10 王子ホールディングス株式会社 糖化発酵システム
US7900857B2 (en) 2008-07-17 2011-03-08 Xyleco, Inc. Cooling and processing materials
CA2731256A1 (en) * 2008-07-24 2010-01-28 Biogasol Ipr Aps Increased ethanol production in recombinant bacteria
JP2010041923A (ja) 2008-08-08 2010-02-25 Oji Paper Co Ltd 酵素糖化方法ならびにエタノール製造方法
CN101381084B (zh) 2008-08-15 2011-01-12 浙江大学 一种含硫氰酸钠废硅藻土的无害化处置方法
WO2010039782A1 (en) * 2008-09-30 2010-04-08 Global Resource Corporation Microwave-based conveying devices and processing of carbonaceous materials
LT2350174T (lt) 2008-10-28 2018-01-10 Xyleco, Inc. Medžiagų apdorojimo būdas
JP2012507584A (ja) * 2008-11-03 2012-03-29 ツァイトン チン 燃焼可能な固体粉末含有の混合燃料と該混合燃料を使用可能なエンジン
NZ708507A (en) * 2008-11-17 2016-01-29 Xyleco Inc Processing biomass
WO2010059796A2 (en) 2008-11-20 2010-05-27 E. I. Du Pont De Nemours And Company Process for producing a sugar solution by combined chemical and enzymatic saccharification of polysaccharide enriched biomass
US8306093B2 (en) 2008-12-01 2012-11-06 Qualcomm Incorporated Method and apparatus for multipath mitigation
CA2745633A1 (en) * 2008-12-02 2010-06-10 The Texas A&M University System Alternative paths to alcohols and hydrocarbons from biomass
FR2939446B1 (fr) 2008-12-05 2011-04-22 Valagro Carbone Renouvelable Utilisation de coton recycle pour produire de l'ethanol, et procede de production.
NZ594092A (en) 2008-12-19 2013-04-26 Xyleco Inc Processing biomass
US8241873B2 (en) * 2008-12-19 2012-08-14 E I Du Pont De Nemours And Company Organic solvent pretreatment of biomass to enhance enzymatic saccharification
EP2376645A4 (en) 2009-01-14 2012-12-19 Iogen Energy Corp IMPROVED METHOD FOR THE PRODUCTION OF GLUCOSE FROM LIGNOCELLULOSE RAW MATERIALS
CN101486637A (zh) * 2009-02-09 2009-07-22 常茂生物化学工程股份有限公司 从发酵液中提取丁二酸的方法
EA201891046A1 (ru) * 2009-02-11 2019-07-31 Ксилеко, Инк. Осахаривание биомассы
NZ599844A (en) * 2009-02-11 2013-12-20 Xyleco Inc Processing biomass
US20100203607A1 (en) * 2009-02-11 2010-08-12 Xyleco, Inc. Processing biomass
AU2010216616A1 (en) * 2009-02-23 2011-10-20 Kirin Holdings Kabushiki Kaisha Manufacturing method for substances from Candida utilis that can use xylose as carbon source
CA2754108A1 (en) 2009-03-05 2010-09-10 Metabolix, Inc. Propagation of transgenic plants
US20110111456A1 (en) * 2009-04-03 2011-05-12 Xyleco, Inc. Processing biomass
CN101532038A (zh) * 2009-04-24 2009-09-16 北京金骄生物质化工有限公司 一种利用植物秸秆制备燃料乙醇的方法
CN101555495B (zh) * 2009-05-18 2014-03-19 徐守才 乙醇导向秸秆生物炼制全封闭集成系统
US20100294960A1 (en) * 2009-05-19 2010-11-25 Innovative American Technology, Inc. Modular radiation shield
US8636402B2 (en) 2009-05-20 2014-01-28 Xyleco, Inc. Processing biomass
WO2010135380A1 (en) 2009-05-20 2010-11-25 Xyleco, Inc. Processing hydrocarbon-containing materials
AU2010249670B2 (en) 2009-05-20 2015-05-07 Xyleco, Inc. Bioprocessing
NZ705401A (en) 2009-05-20 2016-03-31 Xyleco Inc Processing biomass
EA022004B1 (ru) * 2009-05-20 2015-10-30 Ксилеко, Инк. Способ осахаривания биомассы
RU2012101623A (ru) * 2009-06-18 2013-07-27 Конинклейке Филипс Электроникс, Н.В. Мобильный визуализирующий блок с изолированием от окружающей среды
CN102471694B (zh) * 2009-07-01 2014-06-04 西尔卡集团私人有限公司 将木质纤维素材料转化为有用的化学品的方法
JP2011024545A (ja) 2009-07-29 2011-02-10 Nippon Paper Industries Co Ltd セルロース含有物から糖を製造する方法
ES2458554T3 (es) * 2009-08-24 2014-05-06 Abengoa Bioenergy New Technologies, Inc. Procedimientos de producción de etanol y coproductos a partir de biomasa celulósica
JP2011050359A (ja) * 2009-09-04 2011-03-17 Musashino Chemical Laboratory Ltd 新規微生物および該微生物由来の酵素、ならびにこれらを用いた糖化液の製造方法
ES2557317T3 (es) 2009-09-07 2016-01-25 Council Of Scientific&Industrial Research (An Indian Registered Body Incorporated Under The Registration Of Societies Act (Act Xxxi Of 1860) Procedimiento de producción integrada de etanol y savia de algas marinas a partir de Kappaphycus alvarezii
US8026087B2 (en) * 2009-09-23 2011-09-27 Russell W Spitz Method of continuously producing ethanol and electricity from a sustainable renewable biomass feedstock
CN101659681B (zh) 2009-09-30 2012-10-03 济南圣泉唐和唐生物科技有限公司 木糖制品的生产方法
CN101665524B (zh) * 2009-09-30 2013-05-29 济南圣泉唐和唐生物科技有限公司 L-阿拉伯糖的生产方法
US8518213B2 (en) * 2009-10-09 2013-08-27 Api Intellectual Property Holdings, Llc Process for producing alcohol and other bioproducts from biomass extracts in a kraft pulp mill
BR112012008513B1 (pt) * 2009-10-13 2019-03-19 Purdue Research Foundation Processo para a conversão de biomassa em etanol, processo para a separação de material contendo energia das correntes de processo do processo de conversão de biomassa em etanol e processo para a recuperação de um material combustível queimável
WO2011052824A1 (ko) 2009-10-30 2011-05-05 씨제이제일제당(주) 전기투석 및 직접회수방법을 이용한 당화액으로부터의 경제적인 자일로스의 제조공정
CN101928733B (zh) * 2009-11-05 2012-08-29 王建设 一种秸秆类物质或农林废弃物生产生物丁醇的方法及装置
WO2011063500A1 (en) 2009-11-24 2011-06-03 National Research Council Of Canada Process for preparing furfural from xylose
CA2783198A1 (en) 2009-12-07 2011-06-16 Edward Delaney Methods for purifying monosaccharide mixtures containing ionic impurities
CN104073523A (zh) 2010-01-15 2014-10-01 希乐克公司 冷却和加工材料
JP5581069B2 (ja) * 2010-01-29 2014-08-27 株式会社藤井基礎設計事務所 酸回収方法、糖液の製造方法、及び発酵方法
JP2011183372A (ja) * 2010-02-10 2011-09-22 Tsukada Laboratory:Kk 生ゴミ処理装置及び生ゴミ処理システム
AP2016009365A0 (en) * 2010-02-17 2016-08-31 Xyleco Inc Processing biomass
US20110204000A1 (en) 2010-02-25 2011-08-25 Conocophillips Company Method for removing selenium from water
DK2548965T3 (en) 2010-03-15 2018-11-19 Toray Industries Process for preparing a sugar solution
US8573222B2 (en) 2010-03-21 2013-11-05 David Weintraub Intrauterine device and inserter for the same
JP5728817B2 (ja) * 2010-03-30 2015-06-03 東レ株式会社 キシロース糖液の製造方法
CA2788898A1 (en) * 2010-03-30 2011-10-06 Dupont Nutrition Biosciences Aps Separation process
CN101781579A (zh) * 2010-04-07 2010-07-21 王治刚 一种生物质的气化方法及生物质气化炉
WO2011133536A1 (en) 2010-04-19 2011-10-27 The University Of Toledo Aldose-ketose transformation for separation and/or chemical conversion of c6 and c5 sugars from biomass materials
US20110252698A1 (en) 2010-04-20 2011-10-20 River Basin Energy, Inc. Method of Drying Biomass
US8906235B2 (en) * 2010-04-28 2014-12-09 E I Du Pont De Nemours And Company Process for liquid/solid separation of lignocellulosic biomass hydrolysate fermentation broth
SG10201602578VA (en) * 2010-05-24 2016-05-30 Xyleco Inc Processing biomass
US8697404B2 (en) * 2010-06-18 2014-04-15 Butamax Advanced Biofuels Llc Enzymatic production of alcohol esters for recovery of diols produced by fermentation
US20110314728A1 (en) 2010-06-24 2011-12-29 River Basin Energy, Inc. Method of Simultaneously Drying Coal and Torrefying Biomass
US8710279B2 (en) * 2010-07-09 2014-04-29 Celanese International Corporation Hydrogenolysis of ethyl acetate in alcohol separation processes
KR101303289B1 (ko) 2010-07-15 2013-09-03 주식회사 시뮬레이션테크 배기가스 오염물 저감시스템과 그 모니터링 방법
KR101923598B1 (ko) * 2010-07-19 2018-11-29 질레코 인코포레이티드 바이오매스의 가공처리
CN101899486B (zh) * 2010-07-20 2012-10-03 天津科技大学 利用模拟移动床分离提纯低聚木糖的方法
BR112013004261B1 (pt) * 2010-08-31 2021-04-06 Oji Holdings Corporation Método para o tratamento de sacarificação enzimática de uma matéria-prima a base de lignocelulose
IL207945A0 (en) * 2010-09-02 2010-12-30 Robert Jansen Method for the production of carbohydrates
WO2012041382A1 (de) * 2010-09-30 2012-04-05 Beat Schild-Kessler Schmuckobjekt sowie anordnung aus einem schmuckobjekt und einem reststück
JP2012078019A (ja) * 2010-10-01 2012-04-19 Mitsubishi Heavy Ind Ltd バイオマス貯蔵ユニット及び前処理ユニット
CN101979643A (zh) * 2010-10-01 2011-02-23 曾爱民 一种大米果葡糖浆的制备工艺
CN103180450B (zh) * 2010-10-20 2016-10-26 希乐克公司 通过用电子束照射来处理木质纤维素材料的方法
JP2012098052A (ja) * 2010-10-29 2012-05-24 Japan Organo Co Ltd クロマト分離方法およびクロマト分離装置
US20130292331A1 (en) * 2010-11-09 2013-11-07 The University Of Toledo Ionic liquid recovery and purification in biomass treatment processes
CN102070402A (zh) * 2010-12-14 2011-05-25 清华大学 一种1，3-丙二醇发酵液的脱盐方法
JP5819607B2 (ja) * 2010-12-28 2015-11-24 活水プラント株式会社 減圧熱分解処理装置及び連続油化炭化設備
JP2012148921A (ja) * 2011-01-19 2012-08-09 Kassui Plant Kk 超微粉炭化物の製造設備
CN103459604A (zh) 2011-02-14 2013-12-18 希乐克公司 加工生物质
JP2014507148A (ja) 2011-02-14 2014-03-27 ザイレコ，インコーポレイテッド 紙供給原料処理
JP5829819B2 (ja) * 2011-03-07 2015-12-09 川崎重工業株式会社 電気透析方法
FR2974116B1 (fr) 2011-04-14 2015-08-21 IFP Energies Nouvelles Procede de production d'ethanol et de solvants a partir de biomasse lignocellulosique avec recyclage d'un vin butylique obtenu par fermentation des pentoses
US9862893B2 (en) * 2011-05-12 2018-01-09 Virent, Inc. Process for purifying lignocellulosic feedstocks
CN102220395B (zh) * 2011-05-23 2013-05-29 北京坡华生化技术有限公司 小麦淀粉生物制糖工艺
LT2718449T (lt) * 2011-06-09 2018-01-10 Xyleco, Inc. Biomasės apdorojimas
RU112680U1 (ru) 2011-07-08 2012-01-20 Общество с ограниченной ответственностью "Сахара" Линия по производству глюкозно-фруктозного сиропа из крахмалсодержащего сырья
CN103702754B (zh) * 2011-07-29 2017-04-26 东丽株式会社 助滤剂的制造方法
US8425632B2 (en) * 2011-08-08 2013-04-23 Perlman Consulting LLC Composite fuel for fires
WO2013022334A1 (en) 2011-08-08 2013-02-14 Soo Keng Lee Process for the production of organic acids from an integration of solar or fuel cell with electrodialysis system
WO2013085644A1 (en) * 2011-12-08 2013-06-13 Shaw Global Services, Llc Fluid treatment system
WO2013089990A1 (en) * 2011-12-14 2013-06-20 Celanese International Corporation Phasing reactor product from hydrogenating acetic acid into ethyl acetate feed to produce ethanol
SG11201402951QA (en) 2011-12-22 2014-08-28 Xyleco Inc Processing biomass
MY169799A (en) 2011-12-22 2019-05-16 Xyleco Inc Processing biomass for use in fuel cells related applications
BR112014015994A2 (pt) 2011-12-30 2018-05-22 Du Pont processo.
CN102556608B (zh) * 2012-01-12 2014-03-26 冀州中科能源有限公司 一种耐高温的螺旋输送器
KR101361462B1 (ko) * 2012-04-05 2014-02-11 현대자동차주식회사 유산 제조 장치 및 방법
AU2013256049B2 (en) 2012-05-03 2017-02-16 Virdia, Inc. Methods for treating lignocellulosic materials
DE102012209434A1 (de) * 2012-06-04 2013-12-05 EVONTA - Service GmbH Verfahren und Vorrichtung zur Desinfektion rieselfähiger Produkte, vorzugsweise Saatgut, mit beschleunigten Elektronen
UA118174C2 (uk) 2012-07-02 2018-12-10 Ксілеко, Інк. Спосіб обробки біомаси
UA116630C2 (uk) * 2012-07-03 2018-04-25 Ксілеко, Інк. Спосіб перетворення цукру на фурфуриловий спирт
CN202670653U (zh) * 2012-07-13 2013-01-16 湖北宜都运机机电设备有限责任公司 高温水冷螺旋输送机
AU2013329153B2 (en) * 2012-10-10 2017-09-14 Xyleco, Inc. Treating biomass
WO2014059131A1 (en) 2012-10-10 2014-04-17 Xyleco, Inc. Equipment protecting enclosures
NZ743055A (en) 2013-03-08 2020-03-27 Xyleco Inc Equipment protecting enclosures
CN105142768B (zh) * 2013-04-26 2019-07-30 希乐克公司 将羟基羧酸加工成聚合物
JP6033162B2 (ja) * 2013-05-13 2016-11-30 日立造船株式会社 遮蔽体および電子線容器滅菌設備

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080248540A1 (en) * 2007-04-03 2008-10-09 The Ohio State University Methods of producing butanol
US20110300596A1 (en) * 2008-12-12 2011-12-08 Sk Innovation Co., Ltd. Preparation method for alcohol from carboxylic acid by one-step process
US20110287498A1 (en) * 2009-01-26 2011-11-24 Xyleco, Inc. Processing biomass
WO2011031104A2 (ko) * 2009-09-14 2011-03-17 지에스칼텍스 주식회사 바이오 연료물질 및 바이오 화학물질 제조방법

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Ezeji et al., Bioresource Technol. 99: 5232-5242 (2008). *
Grimmler et al., J. Biotechnol. 150: 315-323 (2010). *

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9919939B2 (en) 2011-12-06 2018-03-20 Delta Faucet Company Ozone distribution in a faucet
US10947138B2 (en) 2011-12-06 2021-03-16 Delta Faucet Company Ozone distribution in a faucet
US10543460B2 (en) 2013-03-08 2020-01-28 Xyleco, Inc. Upgrading process streams
US10174160B2 (en) 2013-04-26 2019-01-08 Xyleco, Inc. Processing hydroxy-carboxylic acids to polymers
US10501761B2 (en) 2013-04-26 2019-12-10 Xyleco, Inc. Processing biomass to obtain hydroxylcarboxylic acids
US11458214B2 (en) 2015-12-21 2022-10-04 Delta Faucet Company Fluid delivery system including a disinfectant device
US20190309232A1 (en) * 2016-06-13 2019-10-10 Bio-Think Mixture for supplying a boiler or a diesel engine, comprising diesel fuel or heating oil and esters and alkanes from the transformation of biomass
US11220467B2 (en) 2017-01-11 2022-01-11 Recycle Track Systems, Inc. Indoor food waste fermentation and recycling process
US10981735B2 (en) * 2017-05-16 2021-04-20 Sumitomo Chemical Company, Limited Pneumatic conveyance method for methionine
WO2021257080A1 (en) * 2020-06-18 2021-12-23 Recycle Track Systems Inc. Indoor food waste fermentation and recycling process

Also Published As

Publication number Publication date
US20140284494A1 (en) 2014-09-25
AU2018233024A1 (en) 2018-10-11
MX2015010414A (es) 2015-10-29
EA034454B1 (ru) 2020-02-10
AU2019257501A1 (en) 2019-11-21
IL240480A0 (en) 2015-09-24
NZ751099A (en) 2020-04-24
EP2890795A1 (en) 2015-07-08
AU2018202134A1 (en) 2018-04-19
CA2886129A1 (en) 2014-09-12
SG10201607261RA (en) 2016-10-28
MX2015011318A (es) 2016-03-03
MY174011A (en) 2020-03-03
SG10201609476WA (en) 2016-12-29
JP2016516398A (ja) 2016-06-09
US9371550B2 (en) 2016-06-21
EP2890803A4 (en) 2016-08-17
US10549241B2 (en) 2020-02-04
US9816231B2 (en) 2017-11-14
CN105008039A (zh) 2015-10-28
CA2886776A1 (en) 2014-09-12
AU2020201563A1 (en) 2020-03-19
EA201892059A1 (ru) 2019-02-28
NZ751089A (en) 2019-11-29
UA117471C2 (uk) 2018-08-10
US20150368684A1 (en) 2015-12-24
JP2016517267A (ja) 2016-06-16
MX363016B (es) 2019-03-04
PH12017501313A1 (en) 2018-06-25
AU2014225493A1 (en) 2015-04-02
KR20150127043A (ko) 2015-11-16
WO2014138545A1 (en) 2014-09-12
AU2018202977B2 (en) 2019-10-10
US20140287470A1 (en) 2014-09-25
JP2016514959A (ja) 2016-05-26
AU2019200695A1 (en) 2019-02-21
CU24295B1 (es) 2017-12-08
SG11201502296YA (en) 2015-04-29
JP6371780B2 (ja) 2018-08-08
EP2890806A4 (en) 2016-06-22
CN104995307A (zh) 2015-10-21
JP2018187630A (ja) 2018-11-29
PH12015500578A1 (en) 2015-05-11
US20170036186A1 (en) 2017-02-09
EP2888035A4 (en) 2016-07-27
US20200086273A1 (en) 2020-03-19
WO2014138543A1 (en) 2014-09-12
EA201591323A1 (ru) 2016-01-29
US10610848B2 (en) 2020-04-07
WO2014138540A1 (en) 2014-09-12
MX2015010810A (es) 2015-11-26
MX2015010890A (es) 2015-12-03
MX2019015773A (es) 2020-11-11
WO2014138553A1 (en) 2014-09-12
JP2016510691A (ja) 2016-04-11
US9388442B2 (en) 2016-07-12
AU2017219157A1 (en) 2017-09-21
US20140287469A1 (en) 2014-09-25
EA201591329A1 (ru) 2016-01-29
US10543460B2 (en) 2020-01-28
MX2015011241A (es) 2016-02-03
IL240482A0 (en) 2015-09-24
AP2015008694A0 (en) 2015-08-31
CN104995349A (zh) 2015-10-21
US20170044713A1 (en) 2017-02-16
US20180038048A1 (en) 2018-02-08
MY193219A (en) 2022-09-26
EP2890798A4 (en) 2016-06-29
US9637802B2 (en) 2017-05-02
US20140284501A1 (en) 2014-09-25
CN105189765A (zh) 2015-12-23
PH12018501376A1 (en) 2019-11-11
SG10201704485UA (en) 2017-06-29
US10105652B2 (en) 2018-10-23
JP2016512161A (ja) 2016-04-25
MY174611A (en) 2020-04-30
SG11201502353TA (en) 2015-04-29
AP2015008688A0 (en) 2015-08-31
CA2887112A1 (en) 2014-09-12
PH12015500598A1 (en) 2015-05-11
BR112015019381A2 (pt) 2017-06-27
US20200156039A1 (en) 2020-05-21
AP2015008692A0 (en) 2015-08-31
US20170268169A1 (en) 2017-09-21
CU24261B1 (es) 2017-07-04
AU2014225446A1 (en) 2015-04-02
AU2017279627B2 (en) 2019-09-19
US20140284205A1 (en) 2014-09-25
EP2890844A1 (en) 2015-07-08
AU2014225493B2 (en) 2018-12-13
NZ706072A (en) 2018-12-21
US20140318969A1 (en) 2014-10-30
EA201890356A3 (ru) 2018-11-30
EP2890798B1 (en) 2019-08-28
JP2016515043A (ja) 2016-05-26
CU24346B1 (es) 2018-05-08
SG11201502351VA (en) 2015-04-29
BR112015019373A2 (pt) 2017-07-18
KR20150127039A (ko) 2015-11-16
AU2018201169A1 (en) 2018-03-08
JP2016511206A (ja) 2016-04-14
CA2886290A1 (en) 2014-09-12
JP2019201642A (ja) 2019-11-28
MX357448B (es) 2018-07-10
JP2018118247A (ja) 2018-08-02
EP2890805A4 (en) 2016-06-22
CN105247062A (zh) 2016-01-13
WO2014138535A1 (en) 2014-09-12
US20170036185A1 (en) 2017-02-09
EP2890803A1 (en) 2015-07-08
UA117234C2 (uk) 2018-07-10
EP3564713A1 (en) 2019-11-06
SG10201705491WA (en) 2017-08-30
CA2886133A1 (en) 2014-09-12
EP2890805A1 (en) 2015-07-08
PH12015500582A1 (en) 2015-05-04
ZA201705571B (en) 2017-11-29
PH12015500581B1 (en) 2015-05-04
AU2018201758B2 (en) 2019-11-21
MY171792A (en) 2019-10-29
MX2015011239A (es) 2016-05-31
BR112015019380A2 (pt) 2017-12-12
UA119744C2 (uk) 2019-08-12
EA201591311A1 (ru) 2016-01-29
SG11201502374VA (en) 2015-04-29
CU24333B1 (es) 2018-04-03
CA2886464A1 (en) 2014-09-12
KR20150129670A (ko) 2015-11-20
SG10201800241TA (en) 2018-02-27
SG11201502397TA (en) 2015-04-29
EA031662B1 (ru) 2019-02-28
IL240484A0 (en) 2015-09-24
US20190039023A1 (en) 2019-02-07
PH12015500584B1 (en) 2015-05-11
JP2020054999A (ja) 2020-04-09
AP2015008695A0 (en) 2015-08-31
JP6400611B2 (ja) 2018-10-03
AU2020200386A1 (en) 2020-02-13
AU2014225483B2 (en) 2017-09-28
EA030078B1 (ru) 2018-06-29
EA201591307A1 (ru) 2016-02-29
SG11201502385RA (en) 2015-04-29
MX2018006847A (es) 2022-12-13
JP2020109116A (ja) 2020-07-16
CN105452474A (zh) 2016-03-30
EA201890344A3 (ru) 2018-11-30
BR112015019230A2 (pt) 2017-08-22
EA030172B1 (ru) 2018-06-29
EA201890344A2 (ru) 2018-06-29
AU2018202977A1 (en) 2018-05-17
CU24383B1 (es) 2019-03-04
AU2014225446B2 (en) 2017-12-21
EA201892115A2 (ru) 2019-02-28
JP2020073261A (ja) 2020-05-14
SG11201502358XA (en) 2015-04-29
US10294612B2 (en) 2019-05-21
EA032483B1 (ru) 2019-06-28
EA201591305A1 (ru) 2016-01-29
EP2890795A4 (en) 2016-05-25
EP2888605A4 (en) 2016-05-04
EA201890375A2 (ru) 2018-06-29
US20140284277A1 (en) 2014-09-25
US9925496B2 (en) 2018-03-27
EA201591315A1 (ru) 2016-01-29
EP2890786A1 (en) 2015-07-08
PL2890798T3 (pl) 2020-03-31
SG11201502287VA (en) 2015-04-29
KR20150126831A (ko) 2015-11-13
AU2014225567B2 (en) 2017-11-30
BR112015019232A2 (pt) 2017-07-18
EP2890806A1 (en) 2015-07-08
IL240718A0 (en) 2015-10-29
PH12018500152A1 (en) 2018-08-20
EA201890356A2 (ru) 2018-06-29
JP2020037106A (ja) 2020-03-12
US20200038811A1 (en) 2020-02-06
AU2014225489B2 (en) 2017-06-01
AU2018202832B2 (en) 2019-11-21
JP6640258B2 (ja) 2020-02-05
KR20150127590A (ko) 2015-11-17
JP6419094B2 (ja) 2018-11-07
EA201890375A3 (ru) 2018-10-31
BR112015019241A2 (pt) 2020-10-20
JP6585781B2 (ja) 2019-10-02
MX2015010657A (es) 2015-12-17
US20180016745A1 (en) 2018-01-18
CU20150106A7 (es) 2016-06-29
EP2890798A1 (en) 2015-07-08
JP2016510690A (ja) 2016-04-11
NZ743055A (en) 2020-03-27
US9464334B2 (en) 2016-10-11
NZ706073A (en) 2020-08-28
JP2016512162A (ja) 2016-04-25
AP2015008693A0 (en) 2015-08-31
PH12015500583A1 (en) 2015-05-11
JP2018184400A (ja) 2018-11-22
PH12015500581A1 (en) 2015-05-04
AU2019200695B2 (en) 2019-12-05
CN105008531A (zh) 2015-10-28
NZ751359A (en) 2019-09-27
WO2014138549A1 (en) 2014-09-12
JP2016517268A (ja) 2016-06-16
NZ706074A (en) 2019-11-29
AU2017219157B2 (en) 2019-02-21
JP2018138301A (ja) 2018-09-06
EP2888744A1 (en) 2015-07-01
AP2015008691A0 (en) 2015-08-31
SG11201502217YA (en) 2015-04-29
CU24339B1 (es) 2018-04-03
EA201591303A1 (ru) 2016-05-31
IL240722A0 (en) 2015-10-29
CN107955820A (zh) 2018-04-24
SG10201709592PA (en) 2018-01-30
JP2019071887A (ja) 2019-05-16
US20170216775A1 (en) 2017-08-03
CN110066716A (zh) 2019-07-30
JP2016514958A (ja) 2016-05-26
JP2019068835A (ja) 2019-05-09
AP2015008682A0 (en) 2015-08-31
KR20150127588A (ko) 2015-11-17
PH12015500595A1 (en) 2015-08-10
AU2014225485B2 (en) 2018-11-08
BR112015019231A2 (pt) 2017-08-22
PH12015500584A1 (en) 2015-05-11
MX2019008816A (es) 2019-09-26
NZ706118A (en) 2019-09-27
SG10201806136RA (en) 2018-08-30
AU2014225485A1 (en) 2015-04-02
WO2014138598A1 (en) 2014-09-12
KR20150127051A (ko) 2015-11-16
CU20150099A7 (es) 2016-11-29
PH12015500578B1 (en) 2015-05-11
SG10201707931PA (en) 2017-11-29
KR20150127042A (ko) 2015-11-16
MX2015010766A (es) 2015-11-30
WO2014138550A1 (en) 2014-09-12
EP2890470A1 (en) 2015-07-08
EA201591308A1 (ru) 2016-02-29
US10682623B2 (en) 2020-06-16
US9708761B2 (en) 2017-07-18
NZ706109A (en) 2019-09-27
CU20150103A7 (es) 2016-04-25
CN104995532A (zh) 2015-10-21
IL240483A0 (en) 2015-09-24
US20180193801A1 (en) 2018-07-12
EA201591299A1 (ru) 2016-05-31
UA116121C2 (uk) 2018-02-12
CU24262B1 (es) 2017-07-04
BR112015019232B1 (pt) 2019-09-03
AU2019201641A1 (en) 2019-05-09
AP2015008690A0 (en) 2015-08-31
AP2015008681A0 (en) 2015-08-31
AU2018201758A1 (en) 2018-04-05
CN105324165A (zh) 2016-02-10
US20160222476A1 (en) 2016-08-04
SG11201502470RA (en) 2015-04-29
SG10201706331QA (en) 2017-09-28
IL240712A0 (en) 2015-10-29
AU2014225490A1 (en) 2015-04-02
US10066339B2 (en) 2018-09-04
NZ706106A (en) 2019-08-30
CU20150108A7 (es) 2016-07-29
MX2018014943A (es) 2020-09-14
MX2015010768A (es) 2015-11-30
AU2014225440A1 (en) 2015-04-02
AU2014225489A1 (en) 2015-04-02
MY175452A (en) 2020-06-29
EP2888605A1 (en) 2015-07-01
EP2890844A4 (en) 2016-08-24
US10518220B2 (en) 2019-12-31
JP6590701B2 (ja) 2019-10-16
JP2020072652A (ja) 2020-05-14
MY173447A (en) 2020-01-25
JP6360081B2 (ja) 2018-07-18
US20140286714A1 (en) 2014-09-25
AU2014225480A1 (en) 2015-04-02
MX2015010415A (es) 2015-10-29
MX360386B (es) 2018-10-31
KR20150127049A (ko) 2015-11-16
AP2015008689A0 (en) 2015-08-31
AU2014225483A1 (en) 2015-04-02
EA030216B1 (ru) 2018-07-31
US20190010662A1 (en) 2019-01-10
US9777430B2 (en) 2017-10-03
CN105264083A (zh) 2016-01-20
CN104995349B (zh) 2019-03-12
PH12018500008A1 (en) 2018-08-20
PH12015500603A1 (en) 2015-05-11
AU2017279627A1 (en) 2018-01-18
BR112015019228A2 (pt) 2017-12-12
NZ751363A (en) 2020-08-28
PH12015500601A1 (en) 2015-05-11
CU20170035A7 (es) 2017-06-05
BR112015019380B1 (pt) 2020-04-07
AU2014225480B2 (en) 2020-01-23
US20140284203A1 (en) 2014-09-25
AU2018202832A1 (en) 2018-05-10
NZ706099A (en) 2020-04-24
CA2886459A1 (en) 2014-09-12
IL240481A0 (en) 2015-09-24
JP2019034853A (ja) 2019-03-07
MX368602B (es) 2019-10-09
EA201892115A3 (ru) 2019-05-31
EP2890470A4 (en) 2016-06-29
CU20150101A7 (es) 2016-03-31
CA2886774A1 (en) 2014-09-12
CN105452474B (zh) 2020-05-01
IL240719A0 (en) 2015-10-29
CA2886360A1 (en) 2014-09-12
CN109504726A (zh) 2019-03-22
WO2014138548A1 (en) 2014-09-12
UA116122C2 (uk) 2018-02-12
EP2890796A4 (en) 2016-08-24
CN105324165B (zh) 2017-09-22
AU2014225488B2 (en) 2018-06-28
AU2019275544A1 (en) 2020-01-02
KR20150126830A (ko) 2015-11-13
US20170165628A1 (en) 2017-06-15
KR20150127047A (ko) 2015-11-16
JP2018202414A (ja) 2018-12-27
AU2014225491A1 (en) 2015-04-02
WO2014138594A1 (en) 2014-09-12
WO2014138551A1 (en) 2014-09-12
MX2015010416A (es) 2015-11-16
PH12015500579A1 (en) 2015-05-11
EP2888035A1 (en) 2015-07-01
EP2890796A1 (en) 2015-07-08
CU20150104A7 (es) 2016-03-31
CA2886372A1 (en) 2014-09-12
EA031776B1 (ru) 2019-02-28
IL240713A0 (en) 2015-10-29
EA201591312A1 (ru) 2016-01-29
AU2018202134B2 (en) 2020-01-30
AU2018202639A1 (en) 2018-05-10
CN110292897A (zh) 2019-10-01
JP6461017B2 (ja) 2019-01-30
AP2015008686A0 (en) 2015-08-31
MY171272A (en) 2019-10-07
AU2014225444A1 (en) 2015-04-02
MX354629B (es) 2018-03-14
JP6397832B2 (ja) 2018-09-26
AU2014225488A1 (en) 2015-04-02
US10350548B2 (en) 2019-07-16
WO2014138600A1 (en) 2014-09-12
EP2888744A4 (en) 2016-07-27
NZ706082A (en) 2019-10-25
BR112015019238A2 (pt) 2020-10-20
CA2886053A1 (en) 2014-09-12
SG10201707491VA (en) 2017-10-30
BR112015019381B1 (pt) 2018-08-14
MX2019012102A (es) 2020-07-22
CN105008531B (zh) 2020-02-21
CN105164760A (zh) 2015-12-16
US9334518B2 (en) 2016-05-10
IL260267A (en) 2018-07-31
EP2890786A4 (en) 2016-05-04
MX2015011319A (es) 2015-12-03
PH12015500596A1 (en) 2015-05-11
PH12015500600A1 (en) 2015-05-11
CU20150100A7 (es) 2016-11-29
JP2020078795A (ja) 2020-05-28
SG10201800050TA (en) 2018-02-27
US9611516B2 (en) 2017-04-04
JP2016516017A (ja) 2016-06-02
MX370719B (es) 2019-12-20
CU20150107A7 (es) 2016-04-25
CN105026572A (zh) 2015-11-04
SG11201502332PA (en) 2015-04-29
AU2014225440B2 (en) 2018-01-25
JP2019058907A (ja) 2019-04-18
CU20150105A7 (es) 2016-04-25
US20180339270A1 (en) 2018-11-29
CA2886046A1 (en) 2014-09-12
CU24347B1 (es) 2018-05-08
AP2015008687A0 (en) 2015-08-31
EA201591306A1 (ru) 2016-01-29
AU2014225491B2 (en) 2018-02-15
KR20150127050A (ko) 2015-11-16
MX366814B (es) 2019-07-25
CU20150098A7 (es) 2016-08-31
CU24286B1 (es) 2017-12-08
AU2019202963A1 (en) 2019-05-16
MX361291B (es) 2018-11-30
IL240721A0 (en) 2015-10-29
NZ751076A (en) 2020-07-31
US20140284495A1 (en) 2014-09-25
SG11201502410WA (en) 2015-04-29
AU2014225444B2 (en) 2018-01-25
AU2014225567A1 (en) 2015-04-02
AU2018202639B2 (en) 2019-09-26
AU2018201169B2 (en) 2019-10-31
AU2020200148A1 (en) 2020-01-30

Similar Documents

Publication Publication Date Title
AU2018202639B2 (en) Processing And Transforming Biomass
AU2018203843B2 (en) Processing Biomass
AU2017276162B2 (en) Treating Biomass
CA2858286A1 (en) Production of sugar and alcohol from biomass
CA2978343A1 (en) Processing of biomass materials
OA17470A (en) Processing and transforming biomass.
EA033687B1 (ru) Обработка и преобразование биомассы для получения спиртов
OA17372A (en) Treating biomass.
OA16929A (en) Processing biomass.

Legal Events

Date Code Title Description
AS Assignment

Owner name: XYLECO, INC., MASSACHUSETTS

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:MEDOFF, MARSHALL;MASTERMAN, THOMAS CRAIG;FINN, MICHAEL W.;AND OTHERS;SIGNING DATES FROM 20130322 TO 20130402;REEL/FRAME:044864/0177

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: DOCKETED NEW CASE - READY FOR EXAMINATION

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION