EP2340313A2 - Procédé et système de traitement de biomasse - Google Patents

Procédé et système de traitement de biomasse

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Publication number
EP2340313A2
EP2340313A2 EP09796432A EP09796432A EP2340313A2 EP 2340313 A2 EP2340313 A2 EP 2340313A2 EP 09796432 A EP09796432 A EP 09796432A EP 09796432 A EP09796432 A EP 09796432A EP 2340313 A2 EP2340313 A2 EP 2340313A2
Authority
EP
European Patent Office
Prior art keywords
composition
vessel
processing apparatus
fluid
process according
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.)
Withdrawn
Application number
EP09796432A
Other languages
German (de)
English (en)
Inventor
Marcus Brian Mayhall Fenton
Jens Havn Thorup
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.)
Pursuit Marine Drive Ltd
Original Assignee
Pursuit Dynamics PLC
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
Priority claimed from US12/290,700 external-priority patent/US8193395B2/en
Application filed by Pursuit Dynamics PLC filed Critical Pursuit Dynamics PLC
Publication of EP2340313A2 publication Critical patent/EP2340313A2/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/50—Mixing liquids with solids
    • B01F23/51—Methods thereof
    • B01F23/511—Methods thereof characterised by the composition of the liquids or solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/50—Mixing liquids with solids
    • B01F23/59—Mixing systems, i.e. flow charts or diagrams
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3124—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow
    • B01F25/31241—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow the main flow being injected in the circumferential area of the venturi, creating an aspiration in the central part of the conduit
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3124—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow
    • B01F25/31243—Eductor or eductor-type venturi, i.e. the main flow being injected through the venturi with high speed in the form of a jet
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
    • C08H8/00—Macromolecular compounds derived from lignocellulosic materials
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/40—Apparatus specially designed for the use of free, immobilised, or carrier-bound enzymes, e.g. apparatus containing a fluidised bed of immobilised enzymes
    • 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
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/14—Pressurized fluid
    • 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
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C12M43/02—Bioreactors or fermenters combined with devices for liquid fuel extraction; Biorefineries
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/09—Means for pre-treatment of biological substances by enzymatic treatment
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/20—Heating; Cooling
    • 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
    • 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
    • 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
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/06—Glucose; Glucose-containing syrups obtained by saccharification of starch or raw materials containing starch
    • 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
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
    • 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
    • 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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
    • 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
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
    • 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
    • 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

Definitions

  • the present invention provides, inter alia, a biomass treatment process and system suitable for use in the production of biofuels, including, e.g., bioethanol. More specifically, the present invention provides a single process and system for the conversion of both starch and cellulose present in a biomass composition into alcohol.
  • First generation processes typically involve an initial hydration step of mixing ground starch-based feedstock with water to form a slurry.
  • the water may be pre-heated prior to being mixed with the feedstock.
  • the slurry may additionally be heated in a vessel in order to activate the starch, and is then heated again and mixed with a liquefaction enzyme in order to convert the starch to long chain sugars.
  • the activation stage typically uses steam-jacketed tanks or steam sparge heating to heat the slurry to the desired temperature.
  • agitation mixers, slurry recirculation loops, or a combination of the two mix the slurry.
  • these heating methods can result in regions being created in the slurry tank or vessel whose temperature is much greater than the remainder of the tank.
  • starch hydrated early in the process can be damaged, e.g., denatured, if it comes into contact with these high temperature regions, resulting in a lower yield.
  • These arrangements also do not provide particularly efficient mixing, as evidenced by the heat damage problem discussed above and also poor hydration of the starch.
  • the conversion stage may also use steam- or water-jacketed tanks, or tanks heated by sparge heaters, to raise the temperature of the slurry to the appropriate level for the optimum performance of the liquefaction enzyme.
  • jet cookers are employed to heat the incoming slurry into the conversion stage vessel. Not only can the slurry suffer the same heat damage as in the activation stage, but the high temperature regions also contribute to limiting the glucose yield from the process. The excessive heat of these regions promotes Maillard reactions, where the sugar molecules are destroyed due to interaction with proteins also present in the slurry. The combination of these Maillard losses with the shear losses from the transfer pumps limits the glucose yield available.
  • existing liquefaction processes require a long residence time for the slurry in the conversion stage to ensure that as much starch is converted to sugar as possible. This has a negative impact on the time and cost of the production process.
  • Crops with a high starch content have a high value in food applications
  • lignocellulosic biomass composed primarily of lignin, hemi-cellulose and cellulose
  • lignocellulosic biomass is of great significance to producers because lignocellulosic biomass is an extremely abundant biomass. It includes, e.g., all trees and grasses, as well as agricultural residues such as wet and dry distiller's grains, corn fibre, corn cob and sugarcane bagasse.
  • the process of deriving biofuel from lignocellulosic biomass will be hereinafter referred to as a "second generation" process.
  • the second generation process converts the lignocellulosic biomass into alcohol (e.g. ethanol) in three stages: a first pre-treatment stage to disrupt the cellular structure of the biomass, a second hydrolysis stage in which the cellulosic part of the biomass is converted to short-chain sugars, and a third fermentation stage in which these sugars are converted to alcohol.
  • alcohol e.g. ethanol
  • the pre-treatment step is needed to soften the biomass and disrupt its cellular structure, thereby exposing more cellulose and hemi-cellulose material.
  • Disruptive pre-treatment processes are normally chemical or physical in nature.
  • Current chemical pre-treatment processes rely on a catalyst to achieve the desired disruption of the cells of the biomass.
  • This catalyst is commonly an acid or an enzyme.
  • the acid has the disadvantage of being harmful to the environment, whilst enzymes are relatively expensive.
  • the most common physical pre-treatment process is steam explosion, examples of which are disclosed in Neves, U.S. Patent No. 4,425,433 issued January 10, 1984 and Foody, U.S. Patent No. 4,461 ,648 issued July 24, 1984.
  • yeast is used to ferment the sugars.
  • the yeast is temperature sensitive and the biomass must be cooled to around 30 0 C before the yeast can ferment the sugars. Cooling the biomass not only increases the length of the fermentation process, but also increases energy consumption given that the fermented biomass must be re-heated downstream for distillation.
  • the first generation process described above is the one most commonly used in the biofuel industry at present.
  • biofuel processing plants are typically located in close proximity to the areas in which the crops are grown, or in areas with local markets for the two products from the process (e.g. ethanol and animal feed).
  • the starch-based components of the crop e.g. corn kernels
  • the remainder of the crop e.g. stalks and leaves
  • the starch-based components are transported to the processing plant.
  • lignocellulosic material e.g. corn husks, corn cob
  • a solution to this problem would be to also obtain alcohol from the lignocellulosic material present using the second generation process.
  • having both first and second generation processes running alongside one another in a single processing plant has a significant impact on processing costs. Firstly, the set-up costs involved in constructing a processing plant having separate processing lines for the first and second generation processes will be much larger than that for constructing a plant with only a first generation process line. Secondly, the production costs in running the various stages of the two processes alongside one another will also be greater than those associated with running only a first generation process line.
  • one object of the present invention is to overcome one or more of the aforementioned disadvantages.
  • An amylase enzyme is considered to be any enzyme suitable for converting starch to sugar.
  • a cellulase enzyme is considered to be any enzyme suitable for converting cellulose or hemi-cellulose to sugar.
  • the step of injecting a high velocity transport fluid into the composition through a nozzle may include generating a low pressure region formed downstream of the nozzle.
  • the condensing step may be initiated by the condensing of the transport fluid downstream of the low pressure region.
  • the step of transferring the composition to a holding vessel may include passing the composition through a temperature conditioning unit to raise the temperature of the composition to the first predetermined temperature.
  • the first predetermined temperature may be between 80 and 85 degrees Celsius.
  • the first predetermined temperature may be 83 degrees Celsius.
  • the first predetermined temperature may be between 72 and 80 degrees Celsius, preferably between 76 and 78 degrees Celsius, such as, for example, 75 degrees Celsius, or 77 degrees Celsius.
  • the liquefaction enzyme(s), e.g., amylase and/or cellulase enzymes may be added to the composition prior to the composition being induced into the passage of the fluid processing apparatus.
  • the process may further comprise:
  • liquefaction enzyme e.g., an amylase enzyme
  • another liquefaction enzyme e.g., a cellulase enzyme
  • the process may further comprise the step of cooling the composition to the second predetermined temperature.
  • the first predetermined temperature may be between 80 and 85 degrees Celsius. Preferably, the first predetermined temperature may be 83 degrees Celsius.
  • the second predetermined temperature may be between 50 and 60 degrees Celsius. Preferably, the second predetermined temperature may be 55 degrees Celsius. [0025] Prior to transferring the composition to the second holding vessel, the process may further comprise:
  • the first predetermined temperature may be between 50 and 60 degrees Celsius. Preferably, the first predetermined temperature may be 55 degrees Celsius.
  • the second predetermined temperature may be between 80 and 85 degrees Celsius. Preferably, the second predetermined temperature may be 83 degrees Celsius.
  • the process may further comprise the steps of:
  • the cooling step may comprise passing the composition through a cooling vessel.
  • the cooling vessel may be a mash cooler.
  • the fermentation temperature may be between 30 and 40 degrees
  • the fermentation temperature may be 35 degrees Celsius.
  • fermentation agents include well know agents used to facilitate fermentation processes and include, but are not limited to, gluco-amylase and yeast.
  • the process may further comprise the step of distilling the fermented composition to draw off the alcohol from the remainder of the composition.
  • the process may further comprise the step of:
  • the process may further comprise the steps of:
  • the process may further comprise the steps of:
  • the process may further comprise the steps of:
  • amylase enzyme is added to the composition prior to the induction of the composition into the passage of the first fluid processing apparatus, and the cellulase enzyme is added to the portion of the composition prior to the induction of the portion of the composition into the passage of the second fluid processing apparatus.
  • the process may further comprise the steps of:
  • the fermentation temperature may be between 30 and 40 degrees
  • the fermentation temperature may be 35 degrees Celsius.
  • one or more fermentation agents may be added to the composition.
  • two fermentation agents are added, wherein the fermentation agents are gluco-amylase and yeast.
  • the fermentation of the first and second portions of the composition may be carried out in a single fermentation vessel. Alternatively, the fermentation of the portions of the composition may be carried out in separate fermentation vessels. [0041] The process may further comprise the step of distilling the fermented composition to draw off the alcohol from the remainder of the composition.
  • the process may further comprise the steps of:
  • the process may further comprise the steps of:
  • the second portion of the composition may be the solids content recovered from the separator.
  • the transport fluid may be steam.
  • the working fluid may be water.
  • the biomass may comprise one or more starch-based crops.
  • a system for treatment of a composition including biomass and a working fluid comprising:
  • At least one fluid processing apparatus the apparatus having a passage for receiving a supply of the composition, and a transport fluid nozzle having a nozzle outlet opening into the passage and having a throat portion whose cross sectional area is less than that of the outlet;
  • the system may further comprise a first cooling vessel located intermediate the first holding vessel and the fermentation vessel.
  • the system may further comprise a second holding vessel and a second cooling vessel intermediate the first cooling vessel and the fermentation vessel.
  • the fluid processing apparatus may include one or more additive ports for introducing additives to the composition.
  • An additive port may open into the passage upstream of the nozzle outlet.
  • an additive port may open into the passage immediately downstream of the nozzle outlet.
  • the system may further comprise a further additive port adjacent the second holding vessel.
  • the system may further comprise a second fluid processing apparatus and a second holding vessel downstream of the first holding vessel, the second fluid processing apparatus having a second passage for receiving the composition from the first holding vessel, and a second transport fluid nozzle having a nozzle outlet opening into the second passage and having a throat portion whose cross sectional area is less than that of the outlet.
  • the system comprises a first processing line made up of the first fluid processing apparatus and the first holding vessel, and the system further comprises a second processing line comprising:
  • a second fluid processing apparatus having a second passage for receiving a supply of the composition, and a second transport fluid nozzle having a nozzle outlet opening into the second passage and having a throat portion whose cross sectional area is less than that of the outlet;
  • the system may further comprise a mixing vessel in fluid communication with the inlet to the passage of the fluid processing apparatus, the mixing vessel mixing supplies of biomass and working fluid to form the composition.
  • the system may further comprise a pump upstream of the or each fluid processing apparatus.
  • the system may comprise a plurality of fluid processing apparatus connected in series and/or parallel with one another to form an array.
  • the system may comprise a plurality of second fluid processing apparatus connected in series and/or parallel with one another to form an array.
  • the system may further comprise a temperature conditioning unit for raising the temperature of the composition between the first and/or second fluid processing apparatus and its respective first and/or second holding vessel.
  • the system may further comprise a distillation apparatus downstream of the fermentation vessel.
  • the system may further comprise a distillation apparatus downstream of the inlet of the mixing vessel.
  • the system may further comprise a first return line connecting the distillation apparatus to the inlet of the fluid processing apparatus.
  • the system may further comprise a separation apparatus downstream of the distillation apparatus.
  • the system may further comprise a separation apparatus downstream of the inlet of the mixing vessel.
  • the system may further comprise a second return line which connects the separator to the inlet of the fluid processing apparatus.
  • the separation apparatus may comprise a centrifuge.
  • the system may further comprise a transport fluid supply unit in fluid communication with the or each transport fluid nozzle.
  • the transport fluid supply unit may supply transport fluid to both the first and second fluid processing apparatus.
  • the transport fluid may be steam, and the conditioning unit may be a steam generator.
  • the present invention provides bioethanol produced according to the any of the methods or systems disclosed herein.
  • the present invention includes a process for producing bioethanol from a biomass comprising:
  • FIGURE 1 is a vertical section view of a fluid processing apparatus according to the present invention.
  • FIGURE 2 is a schematic view of a first embodiment of a system for treatment of a biomass composition according to the present invention
  • FIGURE 3 is a schematic view of a second embodiment of a system for treatment of a biomass composition according to the present invention.
  • FIGURE 4 is a schematic view of a third embodiment of a system for treatment of a biomass composition according to the present invention.
  • FIGURE 5 is a schematic view of a fourth embodiment of a system for treatment of a biomass composition according to the present invention.
  • FIGURE 6 is a schematic view of a fifth embodiment of a system for treatment of a biomass composition according to the present invention.
  • FIGURE 7 is a schematic view of a sixth embodiment of a system for treatment of a biomass composition according to the present invention.
  • FIGURE 8 is a graph showing variations in pressure and temperature of a biomass composition as it passes through the fluid processing apparatus shown in Figure 1.
  • Figure 1 is a vertical cross section through a fluid processing apparatus, generally designated 10.
  • the processing apparatus 10 comprises a housing 12 within which is defined a longitudinally extending passage 14.
  • the passage has an inlet 16 and an outlet 18 and is of substantially constant circular cross section. In other words, the cross sectional area of the passage 12 is substantially constant from the inlet 16 to the outlet 18.
  • a protrusion 20 extends axially into the housing 12 from the inlet 16 and defines exteriorly thereof a plenum 22 for the introduction of a compressible transport fluid.
  • the plenum 22 is provided with an inlet 24 which is connectable to a source of transport fluid (not shown in Figure 1).
  • the protrusion 20 defines internally thereof the inlet 16 and an upstream portion of the passage 14.
  • the protrusion 20 has a distal end 26 remote from the inlet 16.
  • the distal end 26 of the protrusion 20 has a thickness which increases and then reduces again so as to define an inwardly tapering surface 28.
  • the housing 12 has a wall 30, which at a location adjacent that of the tapering surface 28 of the protrusion 20 is increasing in thickness.
  • This increase in thickness provides a portion of the wall 30 with a surface 32 which has an inward taper corresponding to that of the tapering surface 28 of the protrusion 20. Between them the tapering surface 28 of the protrusion 20 and the tapering surface 32 of the wall 30 define an annular nozzle 34.
  • the nozzle 34 has a nozzle inlet 36 in flow communication with the plenum 22, a nozzle outlet 40 opening into the passage 14, and a nozzle throat 38 intermediate the nozzle inlet 36 and the nozzle outlet 40.
  • the nozzle throat 38 has a cross sectional area which is less than that of either the nozzle inlet 36 or the nozzle outlet 40.
  • the passage 14 also includes a mixing region 17, which is located in the passage immediately downstream of the nozzle outlet 40.
  • FIG. 2 shows a first preferred embodiment of a system for treatment of a biomass composition which incorporates a fluid processing apparatus of the type shown in Figure 1.
  • a biomass composition is a composition which includes biomass and a working fluid.
  • the preferred working fluid is water, although other fluids suitable for carrying out the process may be used.
  • biomass is used in this specification to describe any biological material that can be used as a fuel or energy source.
  • suitable types of biomass include forest products, untreated wood products, energy crops and short rotation coppice, as well as animal waste, industrial and biodegradable municipal products from food processing and high energy crops such as rape, sugar cane, and maize.
  • biomass for use in the systems and processes of the present invention are starch-based crops such as corn, wheat and barley, for example.
  • the biomass may also be provided for use in the systems and processes of the present invention in a pre-ground form.
  • the treatment system generally designated 50, comprises a fluid processing apparatus 10 and a holding vessel 52 in fluid communication with the outlet 18 of the processing apparatus 10.
  • the holding vessel 52 is preferably insulated and enclosed by a heated water jacket (not shown) and contains a motor- driven agitator (not shown) to mix and agitate the contents of the vessel 52.
  • the system 50 also comprises a cooling vessel 54 in fluid communication with the holding vessel 52, and a fermentation vessel 56 in fluid communication with the cooling vessel 54.
  • a transport fluid supply 58 is connected to the plenum inlet 24 of the processing apparatus 10 so that transport fluid can be supplied thereto.
  • the system may also comprise a pump upstream of the fluid processing apparatus for inducing fluid into the passage 14 of the processing apparatus 10.
  • a temperature conditioning unit (TCU) (not shown) may be included in the system 50 between the fluid processing apparatus 10 and the holding vessel 52.
  • the TCU comprises one or more fluid processing apparatus of the type illustrated in Figure 1. Where there is more than one processing apparatus in the TCU, they are preferably arranged in series.
  • the temperature conditioning unit can gently increase the temperature of any fluid passing from the fluid processing apparatus 10 to the holding vessel 52.
  • the system 50 enclosed within the dotted lines in Figure 2 can be installed into an existing biomass processing line or, where necessary, additional components can be added to the system 50 to create a complete biomass processing line.
  • the system may also comprise a mixing vessel 60 located upstream of the processing apparatus 10 and in fluid communication with the inlet 16 of the apparatus 10.
  • the mixing vessel 60 is preferably enclosed by a heated water jacket (not shown) and has a motor-driven agitator (not shown) for mixing and agitating the contents of the vessel 60.
  • the mixing vessel 60 also includes first and second additive lines 62, 66 which are connected to respective first and second additive supplies 64,68.
  • the system may also comprise third and fourth additive lines 70, 74 which are connected to the fermentation vessel 56 for the supply of fermenting agents thereto from third and fourth additive supplies 72,76.
  • a distillation vessel 80 may be connected in fluid communication with the fermentation vessel 56.
  • the distillation vessel 80 has an outlet 84 and may also include a return line 82 which is in fluid communication with the inlet 16 of the processing apparatus 10, either directly or via the mixing vessel 60 when present, as shown in Figure 2.
  • the system 50 may also comprise a separation vessel 90 connected in fluid communication with the distillation vessel 80.
  • the separation vessel 90 preferably comprises a centrifuge and includes a second return line 92 and a drain line 94.
  • the second return line 92 is also in fluid communication with the inlet 16 of the processing apparatus 10, either directly or via the mixing vessel 60.
  • the drain line 94 allows contents within the separator 90 to be removed or drained.
  • FIG. 3 shows a second embodiment of the system, generally designated 150.
  • the system 150 comprises a fluid processing apparatus 10 of the type shown in Figure 1 , and a first holding vessel 52 in fluid communication with the outlet 18 of the processing apparatus 10.
  • the system 150 also comprises a cooling vessel 54 in fluid communication with the first holding vessel 52, and a fermentation vessel 56 downstream of the cooling vessel 54.
  • a transport fluid supply 58 is connected to the plenum inlet 24 of the processing apparatus 10 so that transport fluid can be supplied thereto.
  • the system 150 further comprises a second holding vessel 152 and a second cooling vessel 154 connected in series with the other components of the system 150 between the first cooling vessel 54 and the fermentation vessel 56.
  • Both the first and second holding vessels 52,152 are preferably insulated and enclosed by heated water jackets (not shown) and each contains a motor-driven agitator to mix and agitate the contents of the vessels 52,152.
  • a first additive supply 164 is connected to the inlet
  • the system 150 may also comprise third and fourth additive lines 70,74 which are connected to the fermentation vessel 56 for the supply of fermenting agents thereto from third and fourth additive supplies 72,76.
  • the system 150 enclosed within the dotted lines in Figure 3 can be installed into an existing biomass processing line or, where necessary, additional components can be added to the system 150 to create a complete biomass processing line.
  • the system may also comprise a mixing vessel 60 located upstream of the processing apparatus 10 and in fluid communication with the inlet 16 of the apparatus 10.
  • the mixing vessel 60 is preferably enclosed by a heated water jacket (not shown) and has a motor-driven agitator (not shown) for mixing and agitating the contents of the vessel 60.
  • the first additive line 162 may be connected to the mixing vessel 60 instead of the inlet of the fluid processing apparatus 10.
  • a distillation vessel 80 may be connected to an outlet 160 of the fermentation vessel 56.
  • the distillation vessel 80 has an outlet 84 and may also include a return line 82 which is in fluid communication with the inlet 16 of the processing apparatus, either directly or via the mixing vessel 60 when present, as shown in Figure 3.
  • the system 150 may also comprise a separation vessel 90 connected in fluid communication with the distillation vessel 80.
  • the separation vessel 90 preferably includes a centrifuge and includes a second return line 92 and a drain line 94.
  • the second return line 92 is also in fluid communication with the inlet 16 of the processing apparatus, either directly or via the mixing vessel 60.
  • the drain line 94 allows contents within the separator 90 to be removed or drained.
  • Figures 4-7 show other preferred embodiments of the system of the present invention. As with the first and second embodiments of the system, these additional embodiments of the system may be supplemented with the mixing, distillation and separation vessels shown in Figures 2 and 3, but these supplementary vessels are not illustrated or described with respect to these further embodiments for reasons of brevity.
  • Figure 4 shows a third embodiment of the system of the present invention, generally designated 250.
  • the system 250 comprises a fluid processing apparatus 10 of the type shown in Figure 1 , and a first holding vessel 52 in fluid communication with the outlet 18 of the processing apparatus 10.
  • the system 250 also comprises a cooling vessel 54 in fluid communication a fermentation vessel 56, both of which are downstream of the first holding vessel 52.
  • a transport fluid supply 58 is connected to the plenum inlet 24 of the processing apparatus 10 so that transport fluid can be supplied thereto.
  • the system 250 further comprises a second fluid processing apparatus 210 and a second holding vessel 252 connected in series with the other components of the system 250 between the first holding vessel 52 and the cooling vessel 54.
  • the second processing apparatus 210 is substantially identical to the first processing apparatus 10 illustrated in Figure 1 , and has a second transport fluid supply 258 connected to its respective plenum inlet.
  • a first additive supply 264 is connected to the inlet
  • the system 250 may also comprise third and fourth additive lines 70,74 which are connected to the fermentation vessel 56 for the supply of fermenting agents thereto from third and fourth additive supplies 72,76.
  • the fermentation vessel 56 has an outlet 260.
  • FIG. 5 shows a fourth embodiment of the system of the present invention, generally designated 350.
  • the system 350 comprises first and second processing lines which are in parallel with one another and connected to a shared fermentation vessel 56 located downstream.
  • the first processing line comprises a first fluid processing apparatus 10 of the type shown in Figure 1 , a first holding vessel 52 in fluid communication with the outlet 18 of the first processing apparatus 10, and a first cooling vessel 54 in fluid communication with the first holding vessel 52.
  • a first transport fluid supply 58 is connected to the plenum inlet 24 of the first processing apparatus 10 so that transport fluid can be supplied thereto.
  • the second processing line comprises a second fluid processing apparatus 310 also of the type shown in Figure 1 , a second holding vessel 352 in fluid communication with the outlet of the second processing apparatus 310, and a second cooling vessel 354 in fluid communication with the second holding vessel 352.
  • the system 350 may include a second transport fluid supply 358 for supplying transport fluid to the plenum inlet of the second processing apparatus 310.
  • Both the first and second cooling vessels 54,354 are in fluid communication with the fermentation vessel 56 located downstream.
  • a first additive supply 364 is connected to the inlet
  • the system 350 may also comprise third and fourth additive lines 70,74 which are connected to the fermentation vessel 56 for the supply of fermenting agents thereto from third and fourth additive supplies 72,76.
  • the fermentation vessel 56 has an outlet 360 which may connect the fermentation vessel 56 with a distillation vessel and separation vessel of the type shown in Figure 2 in order to supplement the system.
  • the system 350 may include respective return lines (not shown) connecting the distillation and separation vessels with the inlet of the second processing apparatus 310.
  • the system 350 may also include a mixing vessel (not shown) upstream of the first and second processing lines, or else dedicated first and second mixing vessels for each of the first and second processing lines.
  • FIGS 6 and 7 show fifth and sixth embodiments of a system in accordance with the present invention.
  • the systems generally designated 450 and 550, are similar to the system 50 shown in Figure 2. They each have a holding vessel 52, a cooling vessel 54 in fluid communication with the holding vessel 52, and a fermentation vessel 56 in fluid communication with the cooling vessel 54. Where the systems 450,550 differ from the systems of the preceding embodiments is in respect of the fluid processing apparatus. Instead of a single fluid processing apparatus upstream of the holding vessel 52, each system 450,550 utilizes an array of fluid processing apparatus. [0081] In the system 450 of the fifth embodiment, an array of fluid processing apparatus 10 is provided in which the apparatus 10 are arranged in series with one another upstream of the holding vessel 52.
  • the array of processing apparatus may share a single transport fluid supply 58, as illustrated in Figure 6, or else each processing apparatus may have its own dedicated transport fluid supply.
  • the system 450 may include first and second additive lines 462,466 which connect respective first and second additive supplies 464,468 to the inlet 16 of the first fluid processing apparatus 10 in the array.
  • third and fourth additive lines 70,74 may be present in the system 450 to connect respective third and fourth additive supplies 72,76 to the fermentation vessel 56.
  • an array of fluid processing apparatus 10 is provided in which first and second pairs of the apparatus 10 are arranged in parallel upstream of the holding vessel 52.
  • the array of processing apparatus may share a single transport fluid supply, or else each pair of processing apparatus may have a respective first and second transport fluid supply 58,558, as shown in Figure 7. Equally, each individual apparatus 10 may have its own dedicated supply of transport fluid.
  • the system 550 may include first and second additive lines 562,566 which connect respective first and second additive supplies 564,568 to the inlets 16 of the first fluid processing apparatus 10 in each pair forming the array.
  • third and fourth additive lines 70,74 may be present in the system 450 to connect respective third and fourth additive supplies 72,76 to the fermentation vessel 56.
  • a first embodiment of the process utilizes the first embodiment of the system 50 illustrated in Figure 2.
  • the composition to be treated includes a mixture of biomass and a working fluid.
  • the biomass may be obtained from a wide variety of sources but it is preferred that the biomass is a starch-based crop (e.g. corn).
  • the working fluid is preferably water.
  • the biomass and working fluid may be mixed together to form the composition at a location remote from the system 50.
  • the system 50 includes the mixing vessel 60
  • the composition can be formed in the mixing vessel 60.
  • the ground starch-based crop is introduced into the working fluid in the mixing vessel 60 at a controlled mass addition flow rate. The introduction of the crop may be done manually or automatically, and may be introduced continuously or as a batch.
  • the mixing of the crop and working fluid leads to the composition forming a slurry.
  • an amylase enzyme and a cellulase enzyme held in the first and second additive supplies 64,68 are also added to the composition via the respective first and second additive supply lines 62,66.
  • the ratio of crop to liquid content in the slurry is 20-40% by weight.
  • one or more PH adjusters e.g. dilute sulphuric acid, ammonia
  • a surfactant can also be added to the slurry at this point.
  • amylase enzyme utilized in each of the embodiments of the treatment process described herein is preferably ⁇ -amylase, with an activity of between 750 and 824 AGU/g.
  • the enzyme activity is presented per unit mass of wet crop or feedstock.
  • the heated water jacket then heats the slurry in the vessel 60 to a temperature of typically 30-60 0 C, most preferably 30-40 0 C, and holds the slurry at this temperature for 30-120 minutes.
  • the motor-driven agitator stirs the slurry with gentle (i.e. low shear) agitation whilst the slurry is held in the mixing vessel 60.
  • the slurry is held at the desired temperature in the mixing vessel 60 for a sufficient period of time to allow the starch content to be prepared for full hydration.
  • the slurry When the slurry has been soaked in the mixing vessel 60 for sufficient time, it is drained from the vessel 60 and induced into the passage 14 of the fluid processing apparatus 10 via the inlet 16.
  • the composition may be induced into the fluid processing apparatus 10 under gravity. Alternatively, if a pump is present, the pump can induce the composition into the fluid processing apparatus 10 under low shear conditions.
  • the slurry will pass into the passage 14 through inlet 16 and out of the outlet 18.
  • a transport fluid which in this non-limiting example is preferably steam, is fed from the transport fluid supply 58 at a preferred pressure of between 5-7 Bar to the plenum inlet 24.
  • Introduction of the transport fluid through the inlet 24 and plenum 22 causes a jet of steam to issue from the nozzle outlet 40 at a very high, preferably supersonic, velocity.
  • a momentum and mass transfer occurs between the two which results in the atomisation of the working fluid component of the slurry to form a vapour and droplet flow regime.
  • the working fluid within the composition is broken down into very small droplets which are dispersed in a continuous vapour phase.
  • This transfer is enhanced through turbulence generated in the mixing region 17 of the passage 14 by the expansion of the steam as it exits the nozzle 34.
  • the steam injected into the mixing region 17 applies a shearing force to the slurry which not only atomises the working fluid component but also disrupts the cellular structure of the ground crop suspended in the slurry. This disruption of the cellular structure separates any starch granules present from the crop whilst at the same time exposing as much of the lignocellulosic material also present in the composition as possible.
  • the temperature and pressure of the composition as it passes through the fluid processing apparatus 10 can be seen in the graph of Figure 8, which shows the profile of the temperature and pressure as the composition passes through various points in the apparatus 10 of Figure 1.
  • the graph has been divided into four sections A-D, which correspond to various sections of the apparatus 10.
  • Section A corresponds to the section of the passage 14 between the inlet 16 and the nozzle 34.
  • Section B corresponds to the upstream section of the mixing region 17 extending between the nozzle 34 and an intermediate portion of the mixing region 17.
  • Section C corresponds to a downstream section of the mixing region 17 extending between the aforementioned intermediate portion of the mixing region 17 and the outlet 18, while section D illustrates the temperature and pressure of the composition as it passes through the outlet 18.
  • the steam is injected into the composition at the beginning of section B of the Figure 8 graph.
  • the injection of the steam preferably at a supersonic velocity, and its expansion upon exiting the nozzle 34, generates a low pressure area in the section of the mixing region 17 immediately downstream of the nozzle 34.
  • the velocity of the steam will reduce and the steam will begin to condense.
  • the steam condensation may continue and form a condensation shock wave in the downstream section of the mixing region 17.
  • the forming of a condensation shock wave causes a rapid increase in pressure of the composition, as can be seen in section C of Figure 8, and the composition condenses back into a liquid phase in section D of Figure 8.
  • the shear force applied to the composition by the injected steam and the subsequent turbulent flow created disrupts the cellular structure of the ground crop suspended in the slurry.
  • the slurry passes through the partial vacuum and condensation shock wave formed in the mixing region 17, it is further disrupted by the changes in pressure occurring, as illustrated by the pressure profile in sections B and C of Figure 8.
  • the granules are almost instantaneously further hydrated, heated and activated due to the introduction of the steam.
  • the apparatus 10 simultaneously pumps and heats the composition to complete the hydration and activate or gelatinise the starch content as the slurry passes through.
  • homogenous swelling of the starch granules will occur due to the granules absorbing water in the presence of heat. This causes the hydrogen bonding between the starch polymers within the granule to loosen, and there is an irreversible breakdown of the crystalline structure inside the granules.
  • the apparatus mixes the amylase and cellulase enzymes into the composition, providing a homogenous distribution and high level of contact with the starch and lignocellulosic material in the liquid phase.
  • the temperature of the composition as it leaves the apparatus 10 is preferably between 74-76X.
  • the temperature at which the composition leaves the apparatus 10 is selected to avoid any heat damage to the composition during the activation of the starch content and disruption of the cells. However, this temperature may be below the temperature for optimal performance of the amylase and cellulase enzymes. The temperature of the composition may therefore need to be raised without subjecting the composition to excessively high temperatures or additional shear forces. This gentle heating may be achieved using the optional temperature conditioning unit (TCU) located between the apparatus 10 and the holding vessel 52.
  • TCU temperature conditioning unit
  • the TCU comprises one or more fluid processing apparatus of the type illustrated in Figure 1.
  • the pressure of the steam supplied to the apparatus making up the TCU is controlled so that it is comparatively low when compared to that of the steam supplied to the fluid processing apparatus 10 upstream of the TCU.
  • a preferred steam input pressure for the apparatus of the TCU is between 0.5-2.0 Bar. Consequently, the transport fluid velocity is much lower so little or no shear force or condensation shock is applied to the composition by the injected steam as the composition passes through the TCU. Instead, the TCU merely uses the low pressure steam to gently raise the temperature of the composition.
  • the composition is preferably at a temperature of between 80-85 0 C, and most preferably 83°C.
  • the composition then flows downstream into the holding vessel 52.
  • the water jacket of the holding vessel 52 receives heated water which maintains the slurry at the aforementioned temperature. If no TCU is present in the system 50, the heated water jacket is used to increase the temperature of the slurry to within the desired range and then maintain it.
  • the composition is held in the holding vessel 52 for a sufficient residence time to allow the amylase and cellulase enzymes to convert the starch, cellulose and hemi-cellulose present into sugars.
  • the composition is transferred to the fermentation vessel 56.
  • the methods and systems of the present invention may be used to generate polysaccharides from a biomass, which may, if desired, be further processed into alcohol, such as ethanol, particularly bioethanol.
  • the preferred temperature of the composition for fermentation is between 30 and 40 0 C, and most preferably 35°C.
  • the composition can be passed through the cooling vessel 54, which operates in the same manner as a conventional mash cooler. Alternatively, if the cooling vessel 54 is not present the composition can be left to cool to the desired temperature in the fermentation vessel 56.
  • Fermentation agents are preferably added to the composition either in the fermentation vessel 56 or immediately upstream thereof.
  • the agents are contained in the third and fourth additive supplies 72,76 and delivered into the composition via the respective additive lines 70,74.
  • the fermentation agents used may be gluco-amylase and yeast.
  • the composition can be transferred for subsequent distillation and separation. As previously stated, these subsequent processes may or may not be part of the system and process of the present invention.
  • the distillation vessel 80 the composition is boiled and any alcohol (ethanol) present in the composition evaporates and is drawn off via the outlet 84. Molecular sieves may be provided downstream of the outlet to remove any remaining impurities in the alcohol. Additionally, there may be provided a water recovery system (not shown) located between the distillation vessel 80 and the separator vessel 90. The remainder of the composition which is left in the distillation vessel 80 is known as "whole stillage".
  • This whole stillage is made up of two main constituents: the non-starch elements of the ground crop (also known as “distiller's grains”) and water (also known as “thin stillage”).
  • This whole stillage is transferred from the distillation vessel 80 into the separation vessel 90 so that the distiller's grains and thin stillage can be separated from one another.
  • the separation is preferably achieved using a centrifuge.
  • the separated thin stillage can be added back into the composition via the return line 92 if desired.
  • the distiller's grains can be processed and used as animal feed.
  • the process employed by the second embodiment of the system 150 is similar to that employed by the first embodiment of the system 50.
  • the composition to be treated includes a mixture of biomass and a working fluid.
  • the biomass is preferably is a starch-based crop (e.g. corn) and the working fluid is preferably water.
  • the biomass and working fluid may be mixed together to form the composition at a location remote from the system 150.
  • the system 150 includes the mixing vessel 60, the composition can be formed in the mixing vessel 60.
  • the ground starch-based crop is introduced into the working fluid in the mixing vessel 60 at a controlled mass addition flow rate. The mixing of the crop and working fluid leads to the composition forming a slurry.
  • an amylase enzyme held in the first additive supply 164 is also added to the composition via the first additive supply line 162.
  • the first additive line 162 can supply the amylase enzyme direct to the mixing vessel 60, when present, or else to the inlet 16 of the fluid processing apparatus 10.
  • the percentage of crop to liquid content in the slurry is 20-40% by weight.
  • one or more PH adjusters and/or a surfactant can also be added to the slurry at this point.
  • the heated water jacket then heats the slurry in the vessel 60 to a temperature of typically 30-60 0 C, most preferably 30-40 0 C, and holds the slurry at this temperature for 30-120 minutes.
  • the motor-driven agitator stirs the slurry with gentle (i.e. low shear) agitation whilst the slurry is held in the mixing vessel 60.
  • the slurry is held at the desired temperature in the mixing vessel 60 for a sufficient period of time to allow the starch content to be prepared for full hydration.
  • the slurry When the slurry has been soaked in the mixing vessel 60 for sufficient time, it is drained from the vessel 60 and induced into the passage 14 of the fluid processing apparatus 10 via the inlet 16.
  • the composition may be induced into the fluid processing apparatus 10 under gravity.
  • the pump can induce the composition into the fluid processing apparatus 10. In such a case a low-shear pump is used.
  • the fluid processing apparatus 10 is identical to that used in the first embodiment of the process.
  • the manner of operation of the apparatus 10, the mechanisms taking place therein, and the resultant effects on the composition are as in the first embodiment of the process, as described above with reference to Figures 1 and 8. They will therefore not be described in detail again here.
  • the granules are almost instantaneously further hydrated, heated and activated due to the introduction of the steam.
  • the apparatus 10 simultaneously pumps and heats the composition to complete the hydration and activate or gelatinise the starch content as the slurry passes through.
  • the apparatus mixes the amylase enzyme into the composition, providing a homogenous distribution and high level of contact with the starch material in the liquid phase.
  • the temperature of the composition as it leaves the apparatus 10 is preferably between 74-76°C.
  • a temperature conditioning unit of the type described above may be included in the system 150 in order to gently raise the temperature of the composition in the same manner as described above.
  • the composition is preferably at a temperature of between 80-85 0 C, and most preferably 83°C.
  • the composition is then transferred to the first holding vessel 52.
  • the water jacket of the first holding vessel 52 receives heated water which maintains the slurry at the aforementioned temperature. If no TCU is present in the system 150, the heated water jacket is used to increase the temperature of the slurry to within the desired range and then maintain it.
  • the composition is held in the first holding vessel 52 for a first residence time sufficient to allow the amylase enzyme to convert the starch present in the composition into sugars. At the end of the first residence time, the composition is transferred to the second holding vessel 152.
  • the preferred temperature of the composition when it passes to the second holding vessel 152 is between 50 and 60 0 C, and most preferably 55°C.
  • the composition can be passed through the cooling vessel 54, which operates in the same manner as a conventional mash cooler.
  • the cooling vessel 54 is not present the composition can be left to cool to the desired temperature in the second holding vessel 152.
  • the heated water jacket of the second holding vessel 152 maintains the temperature of the composition within the desired range.
  • a cellulase enzyme is added to the composition in the second holding vessel 152 via the second additive supply 168 and associated supply line 166.
  • the cellulase enzyme is added in order to react with the cellulose and hemicellulose- present in the lignocellulosic material exposed when the composition passed through the fluid processing apparatus 10.
  • the composition is held in the second holding vessel 152 for a second residence time sufficient to allow the cellulase enzyme to convert all of the cellulose and hemi-cellulose present into sugars.
  • the composition is transferred to the fermentation vessel 56.
  • the preferred temperature of the composition for fermentation is between 30 and 40 0 C, and most preferably 35°C.
  • the composition can be passed through the second cooling vessel 154, which operates in the same manner as a conventional mash cooler. Alternatively, if the second cooling vessel 154 is not present the composition can be left to cool to the desired temperature in the fermentation vessel 56.
  • Fermentation agents are preferably added to the composition either in the fermentation vessel 56 or immediately upstream thereof.
  • the agents are contained in the third and fourth additive supplies 72,76 and delivered into the composition via the respective additive lines 70,74.
  • the fermentation agents used may be gluco-amylase and yeast.
  • the composition can be transferred for subsequent distillation and separation.
  • the composition is boiled and any alcohol, such as, e.g., ethanol, present in the composition evaporates and is drawn off via the outlet 84.
  • Molecular sieves may be provided downstream of the outlet to remove any remaining impurities in the alcohol.
  • a water recovery system (not shown) located between the distillation vessel 80 and the separator vessel 90.
  • the remainder of the composition which is left in the distillation vessel 80 is known as "whole stillage". This whole stillage is made up of two main constituents: the non-starch elements of the ground crop (also known as “distiller's grains") and water (also known as "thin stillage").
  • This whole stillage is transferred from the distillation vessel 80 into the separation vessel 90 so that the distiller's grains and thin stillage can be separated from one another.
  • the separation is preferably achieved using a centrifuge.
  • the separated thin stillage can be added back into the composition via the return line 92 if desired.
  • the distiller's grains can be processed and used as animal feed.
  • the process employed by the third embodiment of the system 250, as shown in Figure 4, has similarities with those employed by the first and second embodiments of the system 50, 150.
  • the composition to be treated is formed from a mixture of biomass and a working fluid and prepared in the same manner as described above with respect to the second embodiment. However, it is a cellulase enzyme rather than an amylase enzyme which is initially added to the composition from the first additive supply 264.
  • the composition may be induced into the first fluid processing apparatus 10 under gravity, or a pump can induce the composition into the first fluid processing apparatus 10 under low shear conditions.
  • Both the first and second fluid processing apparatus 10, 210 employed in this process are identical to that used in the first and second embodiments described above.
  • the manner of operation of the apparatus 10, 210, the mechanisms taking place therein, and the resultant effects on the composition are as previously described with reference to Figures 1 and 8. They will therefore not be described in detail again here.
  • the first processing apparatus 10 is used primarily to pre-treat the cellulosic material and mix in the cellulase enzyme.
  • the first processing apparatus 10 also partially separates the starch granules from the crop and partially hydrates the starch granules.
  • the second processing apparatus 210 is used to fully hydrate and activate the starch and mix in the starch enzyme.
  • the apparatus mixes the cellulase enzyme into the composition, providing a homogenous distribution and high level of contact with any cellulose and hemi-cellulose that has been exposed by the disruption of lignocellulosic material by the first processing apparatus 10.
  • the temperature of the composition as it leaves the first apparatus 10 is preferably between 50-60 0 C, and most preferably 55°C. It is then transferred to the first holding vessel 52.
  • the water jacket of the first holding vessel 52 receives heated water which maintains the slurry at the aforementioned temperature.
  • the composition is held in the first holding vessel 52 for a first residence time sufficient to allow the cellulase enzyme to convert the cellulose and hemi-cellulose present in the composition into sugars.
  • the composition is transferred to the second processing apparatus 210, at which point an amylase enzyme is added via the second additive supply 268.
  • the second fluid processing apparatus 210 operates in the same manner as the first processing apparatus 10, with the same effect on the starch content of the composition.
  • the apparatus mixes the amylase enzyme into the composition, providing a homogenous distribution and high level of contact with the starch material in the liquid phase.
  • the temperature of the composition as it leaves the second apparatus 210 is preferably between 74-76 0 C.
  • a temperature conditioning unit may be present to gently raise the temperature of the composition to between 80 and 85°C before the composition is transferred to the second holding vessel 252.
  • the water jacket of the second holding vessel 252 receives heated water which maintains the slurry at the aforementioned temperature.
  • the heated water jacket is used to increase the temperature of the slurry to within the desired range and then maintain it.
  • the composition is held in the second holding vessel 252 for a second residence time sufficient to allow the amylase enzyme to convert the starch present in the composition into sugars. At the end of the second residence time, the composition is transferred to the fermentation vessel 56.
  • the preferred temperature of the composition for fermentation is between 30 and 4O 0 C, and most preferably 35°C.
  • the composition can be passed through the cooling vessel 54, which operates in the same manner as a conventional mash cooler. Alternatively, if the cooling vessel 54 is not present the composition can be left to cool to the desired temperature in the fermentation vessel 56.
  • the fermentation stage is identical to that of the preceding embodiments. Once the fermentation stage has been completed, the composition can be transferred via outlet 260 for subsequent distillation and separation stages, which may also be the same as those of the preceding embodiments.
  • FIG. 5 where the conversion of the starch and cellulose content of the composition into sugars is carried out in first and second process lines running in parallel, before the composition is passed to a shared fermentation vessel 56.
  • a biomass and working fluid composition of the type already described above has an amylase enzyme added to it via first additive supply 364.
  • the resultant composition is introduced to the first process line and firstly to the first processing apparatus 10, whereupon it is atomised by the transport fluid in the same manner as the various fluid processing apparatus already described.
  • the first fluid processing apparatus 10 hydrates and activates the starch content of the composition and homogenously mixes the amylase enzyme into the composition.
  • the temperature of the composition as it leaves the first apparatus 10 is again preferably between 74-76 0 C and is therefore gently heated once out of the first apparatus, either by way of a temperature conditioning unit or by the water- jacketed first holding vessel 52, until within the desired 80-85 0 C range.
  • the composition is then held in the first holding vessel 52 for a first residence time sufficient to allow the amylase enzyme to convert the starch content of the composition into sugars.
  • the composition is then transferred to the fermentation vessel 56 for a fermentation step of the type already described above.
  • a cooling vessel 54 can reduce the temperature of the composition prior to fermentation, or else the composition may be left to cool in the fermentation vessel 56. Following fermentation, the composition is released via outlet 360 for subsequent distillation and separation.
  • Solids and distiller's grains obtained from the separation stage are then mixed with additional working fluid and/or liquid components drawn off during distillation or separation to form a further batch of the biomass composition.
  • a cellulase enzyme is added to this composition, which is then induced into the second process line via the second processing apparatus 310.
  • the second processing apparatus 310 operates in the same manner as those already described, with the result that passing the composition through the second processing apparatus 310 further disrupts the cellular structure of the solid material in the composition and homogenously mixes the cellulase enzyme into the composition.
  • the composition preferably leaves the second apparatus 310 at a temperature of between 50 and 6O 0 C and is transferred to the second holding vessel 352.
  • the composition is held in the second holding vessel 352 for a second residence time sufficient for the cellulase enzyme to convert the cellulose and hemi-cellulose exposed in the second apparatus 310 into sugars.
  • the composition is then transferred for fermentation in the fermentation vessel 56, via a second cooling vessel 354 if necessary.
  • This embodiment of the process could be modified such that portions of the initial composition are fed to both the first and second process lines simultaneously, with the first line converting the starch content and the second line converting the cellulose and hemi-cellulose content into sugars before both portions of the composition are transferred to the fermentation vessel 56. It is therefore not essential that the second process line receives remnants of the composition after the separation stage.
  • the fifth and sixth embodiments of the process employed by the systems shown in Figures 6 and 7 are substantially the same as the first and second embodiments of the process as used by the systems of Figures 2 and 3.
  • the formation of the biomass compositions, the addition of amylase and cellulase enzymes, the residence of the processed composition in one or two holding vessels, and the transfer and subsequent fermentation of the composition are the same in these fifth and sixth embodiments as those earlier embodiments.
  • the single fluid processing apparatus has been replaced by an array of fluid processing apparatus.
  • the array is formed from a number of the processing apparatus arranged in series with one another.
  • the array is formed from two pairs of processing apparatus in series, where each pair is in parallel with the other. It should be appreciated that the number of fluid processing apparatuses and configurations of the same could be used in the process and system of the present invention.
  • cooling vessels, distillation vessels and separation vessels which may be included in the system of the present invention are conventional arrangements. They have therefore not been described in full detail in this specification.
  • the present invention provides a single treatment system and process for the conversion of both the starch and cellulose present in a biomass composition.
  • the present invention maximises the alcohol obtained from the composition, including that from the cellulosic and lignocellulosic material inevitably transported to the processing plant with the collected crop. The cost in transporting this additional material is therefore substantially recouped with the present invention.
  • the present invention provides significant cost savings compared to existing systems in which distinct processes and process lines are needed to convert starch and cellulose content separately.
  • Using a processing apparatus of the type described allows the present invention to heat and activate the starch content of the composition while avoiding the creation of regions of extreme heat, which can damage the starch content. Prevention of these regions also reduces or eliminates Maillard effects caused by the reaction of proteins with the extracted starch. These reactions can prevent conversion of the starch to sugar and therefore reduce yields. Furthermore, the gentle agitation mixing and low shear pumping at a lower temperature also ensures that there are no high shear forces which may damage the starch content of the composition whilst held in one of the holding vessels or being transported between vessels. Such damage limits the ultimate glucose yield available from the feedstock.
  • the processing apparatus also ensures that the components of the composition are more thoroughly mixed than is possible using simple agitator paddles and/or recirculation loops alone.
  • the atomisation of the working fluid further ensures a more homogenous mixing of the composition than previously possible. This improved mixing increases the efficiency of the amylase and cellulase enzymes added to convert the starch and cellulose content to sugars.
  • the shear action and condensation/pressure shock applied to the biomass component of the composition when in the processing apparatus further improves the performance of the present invention as this exposes more of this material present in the biomass.
  • This allows virtually all the starch granules in the feedstock to be separated, thereby providing improved starch activation rates compared to conventional processes as the enzymatic activation is supplemented by the mechanical activation in the processing apparatus.
  • This also allows the process to in particular provide a starch to sugar conversion ratio of substantially 100%.
  • the process of the present invention therefore may only require the composition to pass once through the processing apparatus before it is ready to pass to the holding vessels for the conversion stage.
  • Exposing more starch also means that less of the amylase enzyme is needed to achieve a desired dextrose equivalent value of 12-18 before the composition is transferred to the fermentation processes.
  • the condensation/pressure shock kills bacteria at a relatively low temperature, thereby reducing losses in any subsequent fermentation process.
  • injecting a transport fluid such as steam into the biomass composition to atomise the working fluid and create a vapour and droplet flow regime ensures a greater degree of disruption to the cellular structure of the contents of the composition than that achieved by existing pre-treatment processes.
  • the invention enables a reduced amount of catalyst or additive to obtain the desired degree of disruption when compared with existing chemical pre-treatment processes.
  • the disruption achieved by the transport fluid injection may remove the need for such pre-treatment additives entirely.
  • the transport fluid injection of the processing apparatus ensures continual shear and turbulent forces on the composition.
  • the process of the present invention can therefore be continuous, with no need to contain the process in a stand-alone vessel such as that required in steam explosion pre-treatment processes.
  • the high shear forces imparted by the high velocity transport fluid injection not only assist in the disruption of the cellular structure of the biomass, but also atomise the working fluid component of the composition to ensure intimate and homogenous heating and mixing of the composition with the enzymes. Such improved heating and mixing reduces the amount of time and quantity of enzymes required to achieve the necessary chemical reactions in the holding vessels.
  • cooling vessels Whilst one or more cooling vessels have been described as forming part of the system of the present invention, it is to be understood that these cooling vessels are preferable, rather than essential, components of the system. Whilst cooling vessels allow the temperature of the composition to be lowered between the holding vessels and the fermentation vessels, this cooling could be carried out within the holding vessels or fermentation vessels themselves. Such cooling vessels may include, for example, heat exchangers, chillers, direct injection coolers, cascade coolers, or the like.
  • the processing apparatus may be modified to include one or more additive ports, thereby allowing the enzymes to be added directly into the processing apparatus instead of the mixing vessel.
  • An additive port may be provided which opens into the passage of the apparatus upstream of the nozzle outlet. Alternatively, or additionally, an additive port may be provided which opens into the passage immediately downstream of the nozzle into the mixing region of the passage.
  • the arrays of processing apparatus utilized in the fifth and sixth embodiments of the system may replace the individual processing apparatus shown in the other illustrated embodiments.
  • two or more of these multiple processing apparatus may share a single transport fluid supply.
  • all of the processing apparatus present in the system may share a single transport fluid supply.
  • the mixing vessel is a preferred, rather than essential, component of the system of the present invention. Equally, the initial step in the treatment process of forming the composition of biomass and working fluid in the mixing vessel is not essential. If the mixing vessel is not present, the composition may be formed at a remote location and then pumped into the system of the present invention for treatment.
  • the first embodiment of the system and process may be modified such that the temperature of the composition during its residence time in the holding vessel may be between 72 and 80 0 C, and preferably between 76 and 78 0 C.
  • the preferred transport fluid used in the process and system of the present invention is steam.
  • alternative transport fluids may be used.
  • An alternative hot, condensable gas such as carbon dioxide, for example, may be used instead.
  • the process of the present invention is not limited to the use of the specific ⁇ -amylase enzyme described above.
  • Alternative amylase enzymes such as ⁇ -amylase or ⁇ -amylase may be employed instead.
  • more than one of each type of amylase enzyme and cellulase enzyme may be added to the composition.
  • Other enzymes i.e., enzymes other than amylase, cellulase, or hemi-cellulase, which are capable of acting on biomass in substantially the same manner as amylase, cellulase, or hemi-cellulase are also contemplated by and within the scope of the present invention.

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Abstract

La présente invention concerne des procédés et systèmes de traitement de biomasse, et, par exemple, la fabrication de biocombustibles, tels que du bioéthanol, à partir de biomasse. L'invention concerne plus particulièrement un procédé consistant: (a) à faire passer dans un passage d'un appareil de traitement fluidique au moins une première partie d'une composition contenant de la biomasse et un fluide de travail, (b) à injecter dans la composition par une buse communiquant avec le passage de l'appareil de traitement fluidique, un fluide de transport qui applique à la composition une force de cisaillement servant à atomiser le fluide de travail et à former un courant de vapeur et de gouttelettes en aval de la buse, (c) à soumettre à condensation le régime d'écoulement de vapeur et des gouttelettes, (d) à transférer la composition vers une première cuve d'attente, et (e) à maintenir la composition dans la première cuve d'attente à une première température prédéterminée pendant une première période de temps prédéterminée, une enzyme de liquéfaction étant ajoutée à la composition avant ou pendant le traitement. Cette composition peut alors subir un traitement ultérieur visant à la réalisation d'un biocombustible tel que, par exemple, du bioéthanol.
EP09796432A 2008-10-30 2009-10-28 Procédé et système de traitement de biomasse Withdrawn EP2340313A2 (fr)

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US12/290,700 US8193395B2 (en) 2007-05-02 2008-10-30 Biomass treatment process and system
PCT/IB2009/007443 WO2010049815A2 (fr) 2008-10-30 2009-10-28 Procédé et système de traitement de biomasse

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US9010663B2 (en) 2004-02-26 2015-04-21 Tyco Fire & Security Gmbh Method and apparatus for generating a mist
US20080103217A1 (en) 2006-10-31 2008-05-01 Hari Babu Sunkara Polyether ester elastomer composition
CA2556649C (fr) 2004-02-26 2012-07-10 Pursuit Dynamics Plc Ameliorations concernant un procede et un dispositif de vaporisation
US8419378B2 (en) 2004-07-29 2013-04-16 Pursuit Dynamics Plc Jet pump
GB0618196D0 (en) 2006-09-15 2006-10-25 Pursuit Dynamics Plc An improved mist generating apparatus and method
CA2808227A1 (fr) * 2010-08-24 2012-03-01 Delaval Holding Ab Methode antibacterienne pour les procedes de fermentation d'ethanol comprenant du peroxyde d'hydrogene et de l'acide peracetique
GB201119007D0 (en) * 2011-11-03 2011-12-14 Pdx Technologies Ag An improved fluid processing pparatus and method
DE102012025027A1 (de) * 2012-12-20 2014-06-26 Reiflock Abwassertechnik Gmbh Vorrichtung und Verfahren zur Behandlung von Biomasse
GB201705768D0 (en) 2017-04-10 2017-05-24 Kanu Ifeyinwa Rita Anaerobic digester

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WO2010049815A2 (fr) 2010-05-06
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CN102333879A (zh) 2012-01-25
BRPI0921727A2 (pt) 2018-01-30
JP2012507276A (ja) 2012-03-29

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