WO2017029410A1 - Procédé de conversion de biomasse lignocellulosique avec addition de jus de sucre brut - Google Patents

Procédé de conversion de biomasse lignocellulosique avec addition de jus de sucre brut Download PDF

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Publication number
WO2017029410A1
WO2017029410A1 PCT/EP2016/069775 EP2016069775W WO2017029410A1 WO 2017029410 A1 WO2017029410 A1 WO 2017029410A1 EP 2016069775 W EP2016069775 W EP 2016069775W WO 2017029410 A1 WO2017029410 A1 WO 2017029410A1
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Prior art keywords
raw juice
sugar
juice
biomass
derived
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PCT/EP2016/069775
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English (en)
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Martin Dan JEPPESEN
Karl Björn RECHINGER
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Inbicon A/S
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Publication of WO2017029410A1 publication Critical patent/WO2017029410A1/fr

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    • 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
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/02—Monosaccharides
    • 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
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K11/00—Fructose
    • 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

Definitions

  • the present inventions relates to biotechnology, in particular to methods pertaining to the production of bioproducts - such as alcohols, fermentable sugars and/or fermentation products in general - from plant biomass, including plant primary sugars, such as fructose and sucrose, as well as from monomeric sugars derived from cellulose and other polysaccharides, such as glucose and xylan.
  • the current invention concerns a method and products related to the production of bioproducts such as alcohol from biomass, said method comprising the integrated conversion of primary and secondary lignocellulosic sugars.
  • Sugar cane and sweet sorghum processing to produce ethanol is typically conducted in a similar manner: Fresh canes are pressed to produce a sugar- rich juice, also called "raw juice", which is typically concentrated and effectively sterilized by evaporative processes, then directly fermented to ethanol.
  • Sorghum further comprises starch-rich seeds, which are typically subject to hydrolysis using amylase and glucoamylase enzymes for instance to produce a fermentable solution. Residual lignocellulosic materials in both cases such as bagasse, straw and leaves have been used typically as a fuel for steam (heat and power) generation. In recent years, there was considerable interest for the integrated processing schemes, whereby whole-crop sugar cane and sweet sorghum can be utilized in ethanol production.
  • Lignocellulosic 2G sugars are typically obtained through a process whereby bagasse, straw and/or leaves are first pretreated and then subject to enzymatic hydrolysis using a cellulase based enzyme preparation. Because of limitations of its physical structure, lignocellulosic biomass cannot be effectively converted to fermentable sugars by enzymatic hydrolysis without some pretreatment process. A wide variety of different pretreatment schemes have been reported, each offering different advantages and disadvantages. For review see Agbor et al. (201 1 ); Girio et al. (2010) ; Alvira et al. (2010) ;
  • hydrothermal pretreatments are especially attractive. These processes utilize pressurized steam/liquid hot water at temperatures in the order of 1 60 - 230°C to gently melt hydrophobic lignin that is intricately associated with cellulose strands, to solubilize a major part of the hemicellulose, rich in five carbon (C5) sugars, and to disrupt cellulose strands so as to improve accessibility to productive enzyme bindings. Hydrothermal pretreatments can be conveniently integrated with existing coal- and biomass-combustion electrical power generation plants to efficiently utilize turbine steam and power production capacity.
  • WO2015/120859 concerns methods and products related to the production of alcohol from sugar cane or sweet sorghum with integration of 1 st and 2nd generation (1 G/2G) biorefining, thus comprising the integrated conversion of primary and secondary soft lignocellulosic biomass.
  • 1 G/2G 1 st and 2nd generation
  • a number of schemes and process arrangements have been reported for optimizing ethanol production from sugar cane by integration of 1 G and 2G processes. See e.g. (for sugar cane) Dias et al. (2013) ; Palacios-Bereche et al. (2013); Macrelli et al. (2012) ; Dias et al. (201 2); Dias et al. (201 1 ); Walter et al. (2010) and (for sorghum) Kim et al.
  • the current invention concerns methods and products related to the integration of bioproducts-production, such as 2G bioethanol production with e.g. sugar production, fruit- or vegetable juice production, and/or 1 G bioethanol production.
  • bioproducts-production such as 2G bioethanol production with e.g. sugar production, fruit- or vegetable juice production, and/or 1 G bioethanol production.
  • a carbohydrate comprising aqueous fraction can be added to pretreated lignocellulosic biomass prior to enzymatic hydrolysis without negative impact on the hydrolysis yields.
  • the current invention concerns a method or process for the production of a bioproduct, comprising the steps of: (a) Pretreating a lignocellulosic biomass;
  • step (c) Diluting the pretreated biomass from step (a) with some quantity of the raw juice from step (b);
  • step (d) Hydrolysing the diluted biomass from step (c) by enzymatic hydrolysis using a cellulase and/or xylanase comprising enzyme preparation.
  • the first aspect relates to methods/processes, wherein the lignocellulosic biomass and/or the raw juice is not from sugar cane or sweet sorghum ; and/or wherein the lignocellulosic biomass and the raw juice are from a different plant.
  • the lignocellulosic biomass can e.g. be derived from sugar cane, while the raw juice is derived from sweet sorghum, and vice versa.
  • the lignocellulosic biomass is from another plant, such as derived from sugar beet.
  • the raw juice is from another plant, such as derive from sugar beet.
  • the bioproduct is an alcohol, such as EtOH
  • the bioproduct is not EtOH, and can e.g. be one or more of primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • the bioproduct is a fermentation product, and the above method comprises a fermentation step (e), wherein the diluted and hydrolysed biomass from step (d) is fermented to provide a fermentation product, such as e.g. EtOH.
  • the raw juice provided in step (b) is a liquid stream from sugar production, fruit juice production or 1 st generation bioethanol production.
  • a second aspect pertains to one or more bioproducts, including fermentation product(s), hydrolysates, dissolved solids, mixtures or dissolved solids and raw juice, as well as intermediary products, said product(s) being obtained or obtainable by a method or process according to the first aspect of the invention.
  • bioproducts may include fuel or fuel additives for generation of power, heat and/or steam.
  • the bioproduct is an alcohol, such as EtOH.
  • a further product comprising 0.1 -99.9% weight/weight or volume/volume one or more of the bio- or fermentationproduct according to the second aspect of the present invention.
  • Figure 1 Glucan conversion as function of time for the six shake flasks.
  • Figure 3 Increase in glucose concentration in pre-treated wheat straw fiber fractions after 20 h hydrolysis. Conditions: 50 °C with 0.075 g CTec3/g glucan, 10 % TS, pH 4.7-5.2 adjusted with NaOH.
  • Figure 4 Increase in xylose concentration in pre-treated wheat straw fiber fractions after 20 h hydrolysis. Conditions: 50 °C with 0,075 g CTec3/g glucan, 10 % TS, pH 4.7-5.2 adjusted with NaOH.
  • dry matter (D %) refers to total solids (dissolved and undissolved) expressed as weight %, unless indicated otherwise.
  • Autohydrolysis refers to a pretreatment process wherein it is believed that acetic acid liberated by hemicellulose hydrolysis during pretreatment further catalyzes hemicellulose hydrolysis. This may apply to any hydrothermal pretreatment of lignocellulosic biomass, usually conducted at pH between 3.5 and 9.0.
  • bioproduct is meant to comprise one or more of: alcohol, EtOH, sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combinations thereof.
  • Plant refers mainly multicellular eukaryotes of the kingdom Plantae, in particular to plant families or species. Expressions like “lignocellulosic biomass and/or raw juice being from a different plant” are meant to be interpreted as not only being from a different individual plant, but lignocellulosic biomass and/or raw juice being derived from different plant taxons, such as different plant families or species, e.g. sugar beets, sugar cane, or sweet sorghum. In another context, "plant” may also refer to a production facility, such as an electrical power generation plant.
  • raw juice is meant not to be limited to raw juice from sugar production, such as from sugar cane, where fresh canes are pressed to produce a sugar rich juice, and the residual lignocellulosic material is called "bagasse".
  • bagasse residual lignocellulosic material
  • raw juice is to be interpreted broader, comprising in its broadest definition any fermentable sugar comprising aqueous fluid, wherein said fermentable sugar is directly or indirectly derived from plant biomass. This includes any liquid/pumpable streams from e.g. sugar production from e.g. sugar beet, sugar cane, or sweet sorghum; fruit or vegetable juice production; or 1 G ethanol production.
  • the "raw juice” according to the present invention may comprise insoluble components, such as fibres.
  • whole slurry refers to an enzymatic hydrolysis reaction mixture in which the ratio by weight of undissolved to dissolved solids at the start of enzymatic hydrolysis is less than 2.2:1 .
  • cellulase is meant to comprise enzyme compositions that hydrolyse cellulose (beta-1 , 4-D-glucan linkages) and/or derivatives thereof.
  • Cellulases include the classification of exo- cellobiohydrolases (CBH), endoglucanases (EG) and beta-glucosidases (BG) (EC3.2.1 91 , EC3.2.1 .4 and EC3.2.1 .21 ).
  • Examples of cellulases include cellulases from e.g. Penicillium, Trichoderma, Humicola, Fusarium,
  • cellulases are commercially available and known in the art. Commercial cellulase preparations may comprise one or more further enzymatic activities.
  • “cellulase” can also be used interchangeably with “cell-wall modifying enzyme”, referring to any enzyme capable of hydrolysing or modifying the complex matrix polysaccharides of the plant cell wall, such as any enzyme that will have activity in the "cell wall solubilisation assay” as e.g. described in W0101 1 5754, which is herewith included by reference. Included within this definition of "cell-wall modifying enzyme” are cellulases, such as
  • cellobiohydrolase I and cellobiohydrolase II endo-glucanases and beta- glucosidases, xyloglucanases and hemicellulolytic enzymes, such as xylanases.
  • Commercially available cellulase preparation(s) suitable in the present context are often optimized for lignocellulosic biomass conversion and may comprise a mixture of enzyme activities that is sufficient to provide enzymatic hydrolysis of pretreated lignocellulosic biomass, often comprising endocellulase
  • glucan is meant to comprise cellulose as well as other gluco-oligomers and other gluco- polymers. Such oligo- or polysaccharides consist of glucose monomers, linked by glycosidic bonds.
  • “Hydrothermal pretreatment” commonly refers to the use of water, either as hot liquid, vapor steam or pressurized steam comprising high temperature liquid or steam or both, to “cook” biomass, at temperatures of 120 degrees centigrade or higher, either with or without addition of acids or other chemicals.
  • Solid/liquid separation -related terms refer to an active mechanical process, whereby liquid is separated from solid by application of force through pressing, centrifugal or other force, whereby “solid” and “liquid” fractions are provided. The separated liquid is collectively referred to as “liquid fraction.” The residual fraction comprising considerable insoluble solid content is referred to as “solid fraction.” A “solid fraction” will have a dry matter content and will typically also comprise some residual of "liquid fraction.”
  • lignocellulosic biomass is meant to comprise any biomass obtained, obtainable or derived from a lignin comprising plant, such as annual or a perennial plants, such as one or more of: cereal, wheat, wheat straw, rice, rice straw, corn, corn fiber, corn cobs, corn stover, hardwood bulk, softwood bulk, sugar cane, sweet sorghum, bagasse, nut shells, empty fruit bunches, grass, straw, cotton seed hairs, barley, rye, oats, sorghum, brewer's spent grains, palm waste material, wood, soft lignocellulosic biomass, algae, and any combination thereof.
  • a lignin comprising plant such as annual or a perennial plants, such as one or more of: cereal, wheat, wheat straw, rice, rice straw, corn, corn fiber, corn cobs, corn stover, hardwood bulk, softwood bulk, sugar cane, sweet sorghum, bagasse, nut shells, empty fruit bunches, grass, straw, cotton seed
  • the term "soft lignocellulosic biomass” indicates non-wood biomass.
  • the terms “about”, “around”, “approximately”, or “ ⁇ ” indicate e.g. the measuring uncertainty commonly experienced in the art, which can be in the order of magnitude of e.g. +/- 1 , 2, 5, 10, 20, or even 50 percent (%), usually +/- 10%.
  • composition comprising a chemical compound may thus comprise additional chemical compounds. Further definitions may be found elsewhere in this document.
  • Table 1 shows an accounting of expected final ethanol concentration in fermentation of hydrolysate, where sugar cane bagasse has been subject to hydrothermal pretreatment and hydrolysed at various different levels of dry matter (total solids) % to equivalent conversion. Shown are values of expected ethanol in weight % where the hydrolysate is dilute using a mixture comprising 90% water, 1 0% cane juice, or 70% water and 30% cane juice, or 50% water and 50% cane juice. Also shown are expected ratios of enzyme consumption at the various levels of dry matter, in the absence of cane juice
  • the precise amount of raw juice supplementation to be used is a variable to be optimized, in light of the degree of inhibition experienced in a raw juice environment by each given cellulase enzyme preparation, as well as the sugar/carbohydrate of the raw juice added, including economical concerns.
  • this invention is seen to be relevant, when balancing the increased costs for extracting the remaining percentages of sugars, and/or fruit juice in sugar or fruit juice production versus the increased bioproduct yields, such as EtOH in 2G bioethanol production obtained according to the present invention. This provides a hitherto unprecedented flexibilities and alternatives.
  • the current invention concerns a method for the production of a bioproduct, said method comprising the steps of:
  • step (c) Diluting the pretreated biomass from step (a) with some quantity of the raw juice from step (b); (d) Hydrolysing the diluted biomass from step (c) by enzymatic hydrolysis using a cellulase and/or xylanase comprising enzyme preparation.
  • the lignocellulosic biomass is soft lignocellulosic biomass. In other embodiments, the lignocellulosic biomass is not soft lignocellulosic biomass, such as wood.
  • the raw juice comprises undissolved components or constituents, such as fibers and/or lignocellulosic plant materials. In some embodiments, the raw juice does not comprise undissolved components or constituents.
  • the bioproduct is a fermentation product
  • the above method comprises a fermentation step (e), wherein the diluted and hydrolysed biomass from step (d) is fermented to provide a fermentation product, such as an alcohol, e.g. EtOH.
  • the aqueous liquid phase of the hydrolysis mixture in step (d) comprises at least 5 g/L sucrose derived from the added raw juice, such as at least 1 0 g/L or more; such as 1 5 g/L or more; such as 20 g/L or more; such as, 25 g/L or more; such as 30 g/L or more; such as 40 g/L or more; such as 50 g/L or more; such as 60 g/L or more sucrose derived from the added raw juice.
  • the initial dissolved sucrose from the added raw juice is between 5 and 60 g/L, and/or around 5, 1 0, 15, 20, 25, 30, 40, 50, 60, 70, 80, 90, 100, 1 10, 120, or more than 120 g/L. g/L. In some embodiments, the initial dissolved sucrose from the added raw juice is in the range of 1 -120, 2.5-100, or 5-60 g/L.
  • a pretreated biomass and/or a fiber fraction is
  • the pretreated biomass and/or fiber fraction is hydrolysed under conditions where initial dissolved sucrose from the added raw juice is between 5 and 60 g/L, 10 and 60 g/L, 15 and 60 g/L, 20 and 60 g/L, 25 and 60 g/L, 30 and 60 g/L, 40 and 60 g/L, or 50 and 60 g/L.
  • the ratio of added raw juice to pretreated biomass in weight/weight (w/w) or volume/volume (v/v) in step (c) and/or (d) is in the range of 0.01 to 4, 0.1 to 3, or 0.5 to 2; and/or in the range of 0.01 -0.1 ; 0.1 -0.25; 0.25- 0.5; 0.5-1 .0; 1 .0-1 .5; 1 .5-2.0; 2.0-2.5; 2.5-3.0; 3.0-3.5; 3.5-4.0.
  • the ratio of added raw juice to pretreated biomass in weight/weight (w/w) or volume/volume (v/v) in step (c) and/or (d) is at least 0.10:1 0 or more; such as 0.25:10 or more; such as 0.5 :1 0 or more; such as
  • 0.75:1 0 or more such as 1 :10 or more; such as 1 .5:10 or more; such as 2:10 or more; such as 2.5:10 or more; such as 3:10 or more; such as 3.5:10 or more; such as 4:1 0 or more; such as 4.5:1 0 or more; such as 5:10 or more; such as 5.5:10 or more; such as 6 :10 or more; such as 6.5:1 0 or more; such as 7:1 0 or more; such as 7.5:10 or more; such as 8:10 or more; such as 8.5:10 or more; such as 9:1 0 or more; such as 9.5:1 0 or more; such as 10:10 or more, such as such as 1 1 :10 or more, such as 12:1 0 or more, such as 1 3:10 or more, such as 14:1 0 or more, such as 1 5:10 or more, such as 1 6:1 0 or more, such as 1 7:10 or more, such as 1
  • the raw juice provided in step (b) is a liquid stream from sugar production, such as sugar production from sugar beet, sugar cane or sweet sorghum.
  • sugar production such as sugar production from sugar beet, sugar cane or sweet sorghum.
  • "Liquid stream” is meant to comprise a pumpable, fluid, thus said liquid stream may comprise non-soluble components/precipitates.
  • the raw juice is usually an aqueous liquid.
  • said non- soluble components may be biomass, nutrients or other factors that contribute positively in the final yield of the provision of the bioproduct according to the invention.
  • the non-soluble components may also be or comprise undissolved lignocellulosic plant material such as fibers.
  • the raw juice provided in step (b) is a liquid stream from fruit juice production.
  • the raw juice provided in step (b) is a liquid stream from a 1 st generation bioethanol production, such as a 1 st generation bioethanol production based on starch comprising plant material such as tubers including e.g. potatoes and cassava), cereals (e.g. maize, barley, wheat, sorghum, rye, oat), sugar cane, sweet sorghum and/or sugar beet.
  • a 1 st generation bioethanol production such as a 1 st generation bioethanol production based on starch comprising plant material such as tubers including e.g. potatoes and cassava), cereals (e.g. maize, barley, wheat, sorghum, rye, oat), sugar cane, sweet sorghum and/or sugar beet.
  • the lignocellulosic biomass may be subjected to different forms of
  • the pretreatment in step (a) can e.g. be a hydrothermal pretreatment and/or a autohydrolysis pretreatment.
  • the pretreatment in step (a) may comprise: (i) addition of a base such as ammonia (NH 4 OH) or NaOH ; and/or (ii) addition of an acid such as H2SO. .
  • said pretreatment in step (a) does not comprise (i) addition of a base such as NH 4 OH or NaOH ; and/or (ii) addition of an acid such as H2SO4.
  • the pretreatment according to the invention may, or may not comprise a processing step known as steam explosion.
  • the pretreated biomass is subjected to at least one solid/liquid separation step to provide a fiber fraction and a liquid fraction ; and optionally washing the fiber fraction as to remove dissolved solids, such as conducting said washing by a series of pressing and dilution steps, or other washing steps known in the art.
  • the pretreated biomass and/or the fiber fraction is hydrolysed under conditions where initial undissolved solids are between 1 0% and 25%, 1 0% and 20%, or around 15% (w/w). In some embodiments, the pretreated biomass and/or fiber fraction is hydrolysed under conditions where pH is maintained at or around pH 7.0, 6.5, 6.0, 5.5, 5.0, 4.5 or 4.0 or lower. In some embodiments, the pretreated biomass and/or fiber fraction is hydrolysed under conditions where pH is maintained at +/- 0.1 -0.25 pH units around pH 7.0, 6.5, 6.0, 5.5, 5.0, 4.5 or 4.0.
  • the pretreated biomass and/or fiber fraction is hydrolysed under conditions where pH is maintained in the range of pH 7-4, 7-5, 7-6, 6-4, 6-5, 5- 4; and/or wherein the pH is maintained lower than pH 7.0, 6.5, 6.0, 5.5, 5.0, 4.5 or 4.0.
  • hydrolysis is conducted at a constant or approximately constant pH.
  • the pretreated biomass and/or fiber fraction is hydrolysed using a cellulase preparation optimized for lignocellulosic biomass conversion, such as a commercially available cellulase preparation.
  • the pretreated biomass and/or fiber fraction is hydrolysed using a cellulase preparation that is not inhibited more than 20% after 145 hours hydrolysis at an enzyme loading of at least 8 FPU/g DM under conditions appropriate for the tested enzyme preparation by added raw juice where sucrose derived from the added juice is at least 5 g/L.
  • the pretreated biomass and/or fiber fraction is hydrolysed using a cellulase preparation that is not inhibited more than 10, 15, 20, 25, 30, 35, 40, 45, or 50%, after 24, 48, 72, 96, 120, or 145 hours hydrolysis at an enzyme loading of at least 8 FPU/g DM under conditions appropriate for the tested enzyme preparation by added raw juice where sucrose derived from the added juice or raw juice is at least 5, 1 0, 15 or 20 g/L.
  • the hydrolysate obtained after hydrolysis of pretreated biomass and/or fiber fraction is subject to at least one solid/liquid separation step to provide insoluble solids separated from dissolved solids, such as by using a filter press with internal wash, optionally comprising a further step such as a drying step.
  • the insoluble solids provided according to the first aspect are suitable as a fuel and/or fuel additive, such as fuel and/or fuel additive for generation of power, heat and/or steam.
  • a fuel and/or fuel additive such as fuel and/or fuel additive for generation of power, heat and/or steam.
  • This may require one or more conventional processing steps known in the art, such as pressing, drying, and/or pelleting.
  • the dissolved solids comprising cellulosic sugars and sugars derived from the raw juice are mixed with a further quantity of raw juice, optionally followed by a concentration step, such as evaporative concentration and/or reverse osmosis concentration. Other conventional concentration steps or procedures may be used as well.
  • the further quantity of raw juice added can e.g. be in the range of around 1 , 2, 5, 10, 1 5, 20, 30, 40, or 50% by weight or volume; and/or at least 1 , 2, 5, 1 0, 1 5, 20, 30, 40, or 50% by weight or volume.
  • a method is provided, wherein (i) the hydrolysate obtained according to any one of the preceding embodiments; (ii) the dissolved solids obtained according to any one of the preceding embodiments; (iii) the mixture of dissolved solids and raw juice obtained according to any one of the preceding embodiments; (iv) the concentrated solution provided through the concentration step according to any one of the preceding embodiments; and/or any combination of (i), (ii), (iii) and/or (iv) is subsequently fermented to provide one or more product(s), optionally after concentration, purification or any other step(s), such as unit operations known in the art.
  • the hydrolysate obtained according to the first aspect of the invention is subsequently fermented to provide one or more product(s), optionally followed and/or preceded by a concentration, purification or any other processing step(s).
  • the dissolved solids are subsequently fermented to provide one or more product(s), optionally followed and/or preceded by a concentration, purification or any other step(s).
  • a mixture of dissolved solids and raw juice is
  • the bioproduct is a fermentation product, such as one or more chemical, alcohol, ethanol and/or any combination thereof.
  • the bio- and/or fermentation product is one or more of: EtOH, primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • hydrolysis in particular enzymatic hydrolysis can be performed in different ways, and many different methods are known in the art.
  • hydrolysis is performed as whole slurry.
  • the hydrolysis in step (d) is either performed as whole slurry, or a solid/liquid separation step is performed prior to hydrolysis so as to provide a fiber fraction and a liquid fraction.
  • said fiber fraction is separately subject to enzymatic hydrolysis.
  • the raw juice is not derived from sugar cane and/or sweet sorghum.
  • the lignocellulosic biomass is not derived from sugar cane and/or sweet sorghum.
  • the fermentation product is not EtOH.
  • the raw juice is not derived from sugar cane or sweet sorghum;
  • the lignocellulosic biomass is not derived from sugar cane or sweet sorghum, and/or
  • the fermentation product is not EtOH, including any combination of (i), (ii) and/or (iii).
  • the lignocellulosic biomass is not from sugar cane or sweet sorghum.
  • the raw juice is not from sugar cane or sweet sorghum.
  • the bio- and/or fermentation product is not an alcohol, such as EtOH.
  • the flexibility of the current invention allows for a wide range of lignocellulosic biomasses and/or raw juices to be processed.
  • the lignocellulosic biomass and the raw juice are or are derived from a different plant.
  • the lignocellulosic biomass is derived from sugar cane, and the raw juice is derived from sweet sorghum or from another plant than sugar cane, such as e.g. sugar beet, a fruit plant, etc.
  • the lignocellulosic biomass is derived from sweet sorghum, and the raw juice is derived from sugar cane or from another plant than sugarcane, such as e.g. sugar beet, a fruit plant, etc.
  • fermentation especially fermentation in the field of ethanol production is performed using yeast, often Saccharomyces, such as
  • Saccharomyces cerevisiae Alternatives are known in the art, especially when aiming at provision of other fermentation products than ethanol.
  • the second aspect of the current invention relates, in the broadest sense, to any products obtained, or being obtainable according to any one of the preceding embodiments of the first aspect of the invention, including any combination thereof.
  • This may include one or more bioproducts, including fermentation product(s), hydrolysates, dissolved solids, mixtures or dissolved solids and raw juice, as well as intermediary products, said product(s) being obtained or obtainable by a process according to the first aspect of the invention, including fuel or fuel additives for generation of power, heat and/or steam.
  • the bioproduct is EtOH.
  • a bioproduct such as a fermentation product, provided according to any one of the methods of the preceding embodiments.
  • the bioproduct is a bio- alcohol, such as bioethanol.
  • the bio- and/or fermentation product is one or more of: alcohol, EtOH, primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • Further embodiments relate to one or more products comprising or consisting essentially of the hydrolysate, the dissolved solids, the mixture of dissolved solids and raw juice, and any concentrate (s) and/or solid fraction(s) provided as described herein, such as in the first aspect.
  • a fuel or fuel additive such as fuel and/or fuel additive for generation of power, heat and/or steam.
  • fuel and/or fuel additive for generation of power, heat and/or steam.
  • These can be provided from the insoluble solids separated from dissolved solids, such as by using a filter press with internal wash, optionally comprising a further drying step, such as described herein.
  • Such fuel or fuel additives are believed to be very suitable for power, heat and/or steam generation.
  • the fuel is provided as solid fuel, such as in the form of pellets.
  • Some embodiments relate to further products according to the second aspect of the invention, said further products comprising 0.1 -99.9% weight/weight or volume/volume of any product according to the present invention.
  • a method for the production of a bioproduct comprising the steps of :
  • step (d) Hydrolysing the diluted biomass from step (c) by enzymatic hydrolysis using a cellulase and/or xylanase comprising enzyme preparation; wherein the lignocellulosic biomass and/or the raw juice is not from sugar cane or sweet sorghum.
  • a method for the production of a bioproduct comprising the steps of : (a) Pretreating a lignocellulosic biomass, such as soft lignocellulosic biomass;
  • step (d) Hydrolysing the diluted biomass from step (c) by enzymatic hydrolysis using a cellulase and/or xylanase comprising enzyme preparation; wherein the lignocellulosic biomass and the raw juice are from a different plant.
  • step (d) fermenting the hydrolysed and diluted biomass from step (d) to provide a fermentation product.
  • step (d) comprises at least
  • sucrose derived from the added raw juice such as at least 1 0 g/L or more; such as 15 g/L or more; such as 20 g/L or more; such as, 25 g/L or more; such as 30 g/L or more; such as 40 g/L or more; such as 50 g/L or more; such as 60 g/L or more sucrose derived from the added raw juice. 5.
  • the initial dissolved sucrose from the added raw juice is between 1 -1 20, 2.5-1 00, or 5-60 g/L; and/or around 5, 10, 1 5, 20, 25, 30, 40, 50, 60, 70, 80, 90, 100, 1 10, 1 20, or more than 120 g/L.
  • step (c) and/or (d) is in the range of 0.01 to 4, 0.1 to 3, or 0.5 to 2; and/or 0.01 -0.1 ; 0.1 -0.25; 0.25-0.5; 0.5-1 .0; 1 .0-1 .5; 1 .5-2.0; 2.0-2.5; 2.5-3.0; 3.0-3.5; 3.5-4.0.
  • the ratio of added raw juice to pretreated biomass in weight/weight (w/w) or volume/volume (v/v) in step (c) and/or (d) is at least 0.10:10 or more; such as 0.25:10 or more; such as 0.5:10 or more; such as 0.75:1 0 or more; such as 1 :10 or more; such as 1 .5:10 or more; such as 2:10 or more; such as 2.5:10 or more; such as 3 :10 or more; such as 3.5:10 or more; such as 4:10 or more; such as 4.5:1 0 or more; such as 5:1 0 or more; such as 5.5:10 or more; such as 6:1 0 or more; such as 6.5:1 0 or more; such as 7:10 or more; such as 7.5:1 0 or more; such as 8:1 0 or more; such as 8.5:1 0 or more; such as 9:10 or more; such as
  • step (b) is a liquid stream from sugar production, such as sugar production from sugar beet, sugar cane or sweet sorghum.
  • the raw juice provided in step (b) is a liquid stream from fruit juice production.
  • the raw juice provided in step (b) is a liquid stream from a 1 st generation bioethanol production, such as a 1 st generation bioethanol production based on starch comprising plant material such as tubers including e.g. potatoes and cassava), cereals (e.g. maize, barley, wheat, sorghum, rye, oat), sugar cane, sweet sorghum and/or sugar beet.
  • a 1 st generation bioethanol production such as a 1 st generation bioethanol production based on starch comprising plant material such as tubers including e.g. potatoes and cassava), cereals (e.g. maize, barley, wheat, sorghum, rye, oat), sugar cane, sweet sorghum and/or sugar beet.
  • a method according to any one of the preceding embodiments, wherein the pretreatment in step (a) is hydrothermal and/or autohydrolysis pretreatment.
  • a method according to any one of the preceding embodiments, wherein the pretreatment in step (a) comprises one or more of:
  • step (a) does not comprises one or more of:
  • a method wherein the pretreated biomass is subject to at least one solid/liquid separation step to provide a fiber fraction and a liquid fraction; and optionally washing the fiber fraction as to remove dissolved solids, such as conducting said washing by a series of pressing and dilution steps.
  • hydrolysate obtained after hydrolysis of pretreated biomass and/or fiber fraction is subject to at least one solid/liquid separation step to provide insoluble solids separated from dissolved solids, such as by using a filter press with internal wash, optionally comprising a further step such as a drying step.
  • insoluble solids are suitable as a fuel and/or fuel additive, such as fuel and/or fuel additive for generation of power, heat and/or steam.
  • a method according to any one of the preceding embodiments wherein dissolved solids comprising cellulosic sugars and sugars derived from the raw juice are mixed with a further quantity of raw juice, optionally followed by a concentration step, such as evaporative concentration and/or reverse osmosis concentration.
  • bio- and/or fermentation product is one or more of: EtOH, primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • hydrolysis is either performed as whole slurry, or wherein a solid/liquid separation step is performed prior to hydrolysis so as to provide a fiber fraction and a liquid fraction, wherein the fiber fraction is separately subject to enzymatic hydrolysis.
  • the lignocellulosic biomass is derived from sugar cane, and the raw juice is derived from sweet sorghum, or another plant than sugar cane.
  • the lignocellulosic biomass is derived from sweet sorghum
  • the raw juice is derived from sugar cane, or another plant than sweet sorghum.
  • the fermentation product is one or more of: alcohol, EtOH, primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • a bioproduct such as a fermentation product, provided according to any one of the preceding embodiments.
  • bioproduct according to embodiment 37 said product being one or more of: alcohol, EtOH, primary sugar, glucose, fructose, xylan, sucrose, monomeric sugar derived from cellulose or other polysaccharides, including any combination thereof.
  • a product comprising or consisting essentially of (i) the hydrolysate
  • a fuel or fuel additive such as fuel and/or fuel additive for generation of power, heat and/or steam provided according to any one of the preceding embodiments.
  • a further product comprising 0.1 -99.9% weight/weight or volume/volume one or more of the product according to any one of embodiments 37-40.
  • Juice from sugar cane and sweet sorghum were analyzed to determine their sugar composition.
  • Cane juice was extracted by pressing to provide juice, then irradiated using X- ray irradiation to eliminate contaminating microorganisms, then stored at 4° C until use.
  • Composition of sugar cane juice soluble dry substance have also been published to be:
  • a cellulase preparation can be obtained from Trichoderma reesei RUT-C30 raised on C5- rich liquid fraction from pretreated sorghum bagasse as carbon source, as described by Korpos et al. (2012).
  • a cellulase preparation can be obtained from Penicillium echinulatum raised on pretreated sugar cane bagasse as carbon source, as described by Pereira et al. (2013).
  • a cellulase preparation can be obtained from Aspergillus sp. S4 B2 F raised on wheat bran as carbon source, as described by Soni et al. (2010)
  • a commercially available cellulase preparation optimized for conversion of lignocellulosic biomass and sold by NOVOZYMESTM under the tradename CELLIC CTEC3TM can be obtained commercially.
  • ACCELLERASE TRIOTM can be obtained commercially.
  • a commercially available cellulase preparation optimized for conversion of lignocellulosic biomass and sold by DSM Tm can be obtained commercially.
  • a commercially available cellulase preparation optimized for conversion of lignocellulosic biomass and sold by Dyadic Tm can be obtained commercially.
  • the cellulase activity of the cellulase preparations can be determined and expressed per unit volume or mass as "filter paper units” as determined by the method of Adney, B. and Baker, J., Laboratory Analytical Procedure #006, "Measurement of cellulase activity", August 12, 1996, the USA National Renewable Energy Laboratory (NREL), which is expressly incorporated by reference herein in entirety. It will be readily understood by those skilled in the art that FPU provides a measure of cellulase activity, but additional enzyme activities may be usefully included in an effective mixture of cellulytic enzymes, including but not limited to hemicellulase enzyme activities.
  • cellulase preparations can e.g. be found herein , e.g. in the section "Definitions", as well as e.g. in WO101 1 5754.
  • Example 3 Comparative performance of enzymatic activity of selected cellulase
  • the raw juice supplementation which will be advantageous will be that where the final ethanol concentration in fermentation broth with added juice is equivalent to "base case” conditions, but at which the
  • DM % of hydrolysis is sufficiently lowered so as to provide better conversion at a given enzyme dose overall, notwithstanding some inhibition of conversion imposed by the added juice.
  • FPU Filter Paper Units
  • a set of six shake flasks was set up with double determination of the three conditions: 100 wt-% 1 G sugar juice,50 wt-% 1 G sugar juice and 0 % sugar juice (pure water) as reference. Shake flasks were incubated with agitation at 250 rpm and 50 °C.
  • Bagasse obtained after extraction of cane juice as described in example 1 was pretreated in the Inbicon 100 kg/h pilot plant with a feed flow of 50 kg TS/h, as described by Petersen et al. (2009).
  • the fresh bagasse (SCB batch E) was soaked in water to achieve a dry matter content of 40 wt-% TSio5°c at ambient temperature without addition of any chemicals.
  • Pretreatment conditions were 195° C, residence time 12minutes, log severity Ro 3.88.
  • the pretreated biomass slurry was pressed to a fiber fraction of approximately 55 % DM and a liquid fraction. An adjustment period of 3 h before steady state was kept and samples were taken.
  • the pretreated material, fiber fraction as well as liquid fraction, was collected and analysed. The dry matter and composition of the samples were determined.
  • the pretreated bagasse fiber fraction obtained as described herein was used in shake flask experiments at a dry matter content 12 % without any additives other than AcTRIO and pH adjustment chemicals.
  • the pH was adjusted with 20 % Ca(OH)2 to pH 5.
  • the sugar content was measured by HPLC.
  • the solution was diluted with sulphuric acid, whereby the sucrose is split into glucose and fructose.
  • samples were measured on HPLC after 6, 24, 50, 72, 145 and 170 hours. From the measured glucose and xylose
  • the glucan conversion over time was calculated based on the sugars from the fiber fractions, the sugar from 1 G juice having been subtracted.
  • Figure 1 shows glucan conversion for the six shake flasks. The obtained glucan conversions after 170 h for the shake flasks without use of 1 G sugar juice (0 % OAI sugar juice), with 50 % 1 G sugar juice and with 100 % 1 G sugar juice were
  • OAI sugar juice indicates sugar cane raw juice.
  • Figure 2 shows the average glucan conversion after 145 h hydrolysis over the percentage of 1 G sugar juice added to hydrolysis. This relation can be described by a linear function and shows a decrease by 8 % conversion
  • sucrose concentration in the hydrolysate at the start of enzymatic hydrolysis comprised at least 12 g/L, assuming a sucrose concentration of at least 70 g/L in the cane juice.
  • a set of shake flasks was set up with double or single determination of the seven conditions:
  • Negative control pre-treated wheat straw fiber fraction (ptwsff) without any additional chemicals and/or enzymes
  • Wheat straw was pretreated in the Inbicon 100 kg/h pilot plant with a feed flow of 50 kg TS/h, as described by Petersen et al. (2009).
  • wheat straw (Wheat straw batch PWS_F) was soaked in water to achieve a dry matter content of 40 wt-% TSios°c at ambient temperature without addition of any further chemicals.
  • Pretreatment conditions were 189 °C, residence time 12 minutes.
  • the pretreated biomass slurry was pressed to a fiber fraction of 49% dry matter (DM) and a liquid fraction. An adjustment period of 3 h was kept before reaching steady state, whereupon samples were taken.
  • the pretreated material, fiber fraction as well as liquid fraction were collected and analyzed. The dry matter and composition of the samples were determined.
  • the pretreated wheat straw fiber fraction was used in shake flask experiments at a dry matter content 10 %.
  • the pH was adjusted with 8 % NaOH and maintained in the range of pH 4.7 to 5.2, as the pH decreased during hydrolysis presumably due to release of acetic acid.
  • CTec3 dosage 0.075 g CTec3/g glucan, 10 % TS, pH 4.7-5.2
  • the sugar content was measured by HPLC.
  • the hydrolysates and controls were sampled and diluted 1 :10 before monomeric carbohydrate yield was quantified by HPLC with a Phenomenex Rezex H+ column (Kristensen et al. 2009). To follow the hydrolysis, samples were measured on HPLC after 20 hours.

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Abstract

La présente invention concerne des procédés et des produits associés à la production de bioproduits tels que de l'alcool à partir de biomasse lignocellulosique. En particulier, l'invention concerne des procédés comprenant l'addition de sucre et/ou de glucide comprenant des jus bruts avant hydrolyse enzymatique d'une biomasse lignocellulosique prétraitée.
PCT/EP2016/069775 2015-08-20 2016-08-22 Procédé de conversion de biomasse lignocellulosique avec addition de jus de sucre brut WO2017029410A1 (fr)

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CN109423502A (zh) * 2017-09-05 2019-03-05 中粮营养健康研究院有限公司 木薯渣的回收利用方法
CN112143761A (zh) * 2019-06-26 2020-12-29 印度石油有限公司 改进的二次产生乙醇的制备方法
WO2021155452A1 (fr) * 2020-02-03 2021-08-12 Petróleo Brasileiro S.A. - Petrobras Procédé optimisé pour la production de sucres de deuxième génération et produits de fermentation

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109423502A (zh) * 2017-09-05 2019-03-05 中粮营养健康研究院有限公司 木薯渣的回收利用方法
CN108374024A (zh) * 2018-02-12 2018-08-07 北海明世科技开发有限公司 用甜高粱秆和玉米联产乙醇、果糖及多种副产品的方法
CN108374024B (zh) * 2018-02-12 2021-10-26 北海明世科技开发有限公司 用甜高粱秆和玉米联产乙醇、果糖及多种副产品的方法
CN112143761A (zh) * 2019-06-26 2020-12-29 印度石油有限公司 改进的二次产生乙醇的制备方法
WO2021155452A1 (fr) * 2020-02-03 2021-08-12 Petróleo Brasileiro S.A. - Petrobras Procédé optimisé pour la production de sucres de deuxième génération et produits de fermentation

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