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    公开号:BR112013010725B1
    申请号:R112013010725-1
    申请日:2011-11-03
    公开日:2018-12-04
    发明作者:Robert Lawrence Blackbourn；Paul Richard Weider
    申请人:Shell Internationale Research Maatschappij B.V.；
    IPC主号:
    专利说明:

    (54) Title: METHOD FOR TREATING BIOMASS FOR THE PRODUCTION OF SUGARS FROM MATERIALS CONTAINING POLYESACARIDES, FOR USE IN BIOFUELS OR OTHER PRODUCTS OF HIGH VALUE, AND, COMPOSITION (73) Holder: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ. Address: CAREL VAN BYLANDTLAAN 30, NL-2596 HR THE HAGUE, NETHERLANDS (NL) (72) Inventor: ROBERT LAWRENCE BLACKBOURN; PAUL RICHARD WEIDER.
    Validity Term: 20 (twenty) years from 11/03/2011, subject to legal conditions
    Issued on: 12/04/2018
    Digitally signed by:
    Liane Elizabeth Caldeira Lage
    Director of Patents, Computer Programs and Topographies of Integrated Circuits
    1/49 “METHOD FOR TREATING BIOMASS FOR THE PRODUCTION OF SUGARS FROM MATERIALS CONTAINING POLYESACARIDES, FOR USE IN BIOFUELS OR OTHER PRODUCTS OF HIGH VALUE, AND, COMPOSITION” FIELD OF THE INVENTION [0001] The invention refers to a process for the treatment of biomass and, more specifically, a pre-treatment of biomass for the production of sugars from materials containing polysaccharides, for use in biofuels or other high-value products.
    BACKGROUND OF THE INVENTION [0002] Lignocellulosic biomass is seen as an abundant renewable resource for fuels and chemicals, due to the presence of sugars in the cell walls of plants. More than 50% of the organic carbon on the earth's surface is contained in plants. This lignocellulosic biomass is composed of hemicellulose, cellulose and smaller portions of lignin and protein. Cellulose is a polymer formed mainly by condensation of glucose and polymerized hemicellulose is a precursor to pentose, mainly xylose. These sugars can be easily converted into valuable fuels and components, as long as they can be released from the cell walls and polymers that contain them. However, the cell walls of plants have developed considerable resistance to microbial, mechanical or chemical disruption to give the component sugars. A number of approaches have been taken to overcome this resistance and the breakdown of these polymers into sugars, saccharification, has a long history. The general methods are described schematically in Figure 1.
    [0003] Original approaches dating from the early 19th century involve complete chemical hydrolysis using concentrated mineral acids, such as hydrochloric acid, nitric or sulfuric acid. Numerous improvements
    Petition 870180073787, of 08/22/2018, p. 10/62
    2/49 in these processes were carried out to earn higher sugar yields from the biomass feed load. These higher acid concentration approaches provide higher sugar yields, but due to economic and environmental reasons, acids must be recovered. The main obstacle to practicing this form of saccharification has been the challenges associated with acid recovery (M. Galbe and G. Zacchi, A review of the production of ethanol from softwood, Appl. Microbiol. Biotechnol. 59 (2002), pp. 618-628). Recent efforts to separate sulfuric acid and sugars using separation by ionic resin or hydrochloric acid and sugars via amine extraction and subsequent thermal regeneration of the acid have been described in US patent 5,820,687 and WO2010026572. Both approaches are complicated and expensive.
    [0004] Diluted acid processes have also been tried to perform chemical saccharification and one such example is the Scholler Tomesch process. However, the use of diluted acid requires higher temperatures and this generally results in low yields of the desired sugars due to the thermal degradation of the monosaccharides. Several such approaches have been made in the past, and all have failed to address economic obstacles. See Lim Koon Ong, Conversion of lignocellulosic biomass to fuel ethanol- A brief review, The Planter, Vol. 80, No. 941, August 2004 and Cell Wall Saccharification, Ralf Moller, Outputs from the EPOBIO project, 2006; published by CPL Press, Tall Gables, The Sydings, Speen, Newbury, Berks RG14 1RZ, UK.
    [0005] Cellulose saccharification enzymatically holds a promise of higher sugar yields under milder conditions and is therefore considered by many to be more economically attractive. The severe resistance of crude biomass to enzymatic hydrolysis requires a pretreatment to improve the susceptibility of cellulose to hydrolytic enzymes. Various pre-treatment methods, such as those described in
    Petition 870180073787, of 08/22/2018, p. 11/62
    3/49
    Nathan Mosier, Charles Wyman, Bruce Dale, Richard Elander, YY Lee, Mark Holtzapple, Michael Ladisch Features of promising technologies for pretreatment of lignocellulosic biomass Bioresource Technology 96 (2005) pp.673-686, were developed to modify the chemical and structural composition of biomass to improve enzymatic conversion. Such methods include the diluted acid vapor explosion treatment described in US Patent No. 4,461,648, hydrothermal pretreatment without the addition of chemicals described in WO 2007/009463 A2, ammonia freeze explosion, described in AFEX ; Holtzapple, Μ. T., Jun, J., Ashok, G., Patibandla, S.L., Dale, B.E., 1991, The ammonia freeze explosion (AFEX) process— a practical ligno cellulose pretreatment, Applied Biochemistry and Biotechnology 28/29, pp. 59-74, and organosolv extraction described in US patent 4,409,032. Despite this, pretreatment was cited as the most expensive process for converting biomass into fuels (Methods for Pretreatment of Lignocellulosic Biomass for Efficient Hydrolysis and Biofuel Production Ind. Eng. Chem. Res., 2009,48 (8), 3713 -3729).
    [0006] A pretreatment that has been extensively explored is a process of sulfuric acid (H2SO4) diluted at high temperature, which effectively hydrolyzes the hemicellulosic portion of the biomass into soluble sugars and exposes cellulose so that enzymatic saccharification is successful. The parameters that can be used to control the pretreatment conditions are time, temperature and acid charge. These are often combined in a mathematical equation called the combined severity factor. In general, the greater the acid load used, the lower the temperature that can be used, which is accompanied by the cost of acid and its recycling. Conversely, the lower the temperature, the longer the pre-treatment process takes, which is accompanied by the cost of volumetric productivity. It is desirable to reduce the temperature because the pentose sugars readily decompose to
    Petition 870180073787, of 08/22/2018, p. 12/62
    4/49 form furfuraldehydes and other species that represent a loss of yield and these compounds are poisons for downstream fermentation. However, the use of higher concentrations of acid requires reducing pretreatment temperatures below those where furfural formation becomes easy (BP Lavarack, GJ Griffin, D. Rodman The acid hydrolysis of sugarcane bagasse hemicelluloses to product xylose, arabinose, glucose and other products.Biomass and Bioenergy 23 (2002) pp.367-380) and once again requires the recovery of strong acid. If diluted acid streams and higher temperatures are used, the pretreatment reaction produces increased amounts of furfural and the acid passing downstream must be neutralized, resulting in inorganic salts which complicates downstream processing and requires treatment systems. more expensive wastewater.
    [0007] W02010 / 046051 describes a process for the production of lipids from biomass including at least one polysaccharide comprising: subjecting said biomass to acid hydrolysis in the presence of an aqueous solution of at least one organic acid selected from alkyl acids - or aryl sulfonic compounds having from C7 to C20 carbon atoms, preferably from C9 to C15 carbon atoms, or halogenated carboxylic acids, at a temperature ranging from 80 ° C to 160 ° C, preferably 100 ° At 150 ° C, obtaining a first mixture comprising a first solid phase and a first aqueous phase; subjecting said first mixture to enzymatic hydrolysis, obtaining a second mixture comprising a second solid phase and a second aqueous phase; subjecting said second aqueous phase to fermentation in the presence of at least one oleaginous yeast obtaining an oleaginous cell biomass comprising bipids. In order to recover the sulfonic acids used in W02010 / 046051, extraction is required, requiring significant amounts of organic solvents.
    Petition 870180073787, of 08/22/2018, p. 13/62
    5/49
    SUMMARY OF THE INVENTION [0008] Based on the above information, it is desirable to use a strong acid, which is easily reversed into recoverable and recyclable, preferably neutral, components. Such a system would benefit from both concentrated acid hydrolysis and diluted acid biomass pretreatment methods.
    [0009] In one embodiment the present invention comprises a method comprising: (a) providing a biomass containing polysaccharides and (b) contacting the biomass with a solution containing at least one alpha-hydroxysulfonic acid thus hydrolyzing the biomass to produce at least a fermentable sugar containing the product, and (c) optionally removing an alpha-hydroxysulfonic acid in its component form from the product by heating and / or reducing the pressure to produce a product with the removed acid containing at least one substantially fermentable sugar free of alpha-hydroxysulfonic acid.
    [00010] In another embodiment, a method comprises recycling the removed alpha-hydroxysulfonic acid as components for step (b) as components or in its recombined form.
    [00011] In yet another embodiment, a method further comprises hydrolysis more of the product with the acid removed.
    [00012] In yet another embodiment, a method comprises fermenting a stream containing the sugars produced by the above methods.
    [00013] In yet another embodiment, a composition comprises (a) biomass containing polysaccharides, (b) at least one alpha-hydroxysulfonic acid, and (c) water.
    [00014] In yet another embodiment, a composition comprises (a) biomass containing polysaccharides, (b) at least one alpha-hydroxysulfonic acid (c) water, and (d) at least one fermentable sugar.
    Petition 870180073787, of 08/22/2018, p. 14/62
    6/49 [00015] The characteristic features and advantages of the invention will be evident to those skilled in the art. While numerous changes can be made by those skilled in the art, such changes are within the spirit of the invention. BRIEF DESCRIPTION OF THE DRAWINGS [00016] This drawing illustrates certain aspects of some of the embodiments of the invention, and should not be used to limit or define the present invention.
    [00017] Figure 1 schematically illustrates a block flowchart of lignocellulose treatments.
    [00018] Figure 2 schematically illustrates a block flowchart of an embodiment of the present invention of the biomass treatment process.
    [00019] Figure 3 schematically illustrates a block flow chart of another embodiment of the invention's biomass treatment process. [00020] Figure 4 shows the xylose recovered with time, in the presence of 10% by weight alpha-hydroxyethanesulfonic acid and 10.7% of biomass in comparison with the comparative example with only water, biomass and SO2. [00021] Figure 5 shows the grams of Furfural / grams of xylose produced over time, in the presence of an alpha-hydroxysulfonic acid and 10% by weight of bagasse.
    [00022] Figure 6 shows a three-dimensional IR graph, plotting individual IR spectra over time from the treatment of bagasse with 20% by weight of alpha-hydroxyethane-sulfonic acid, at 100 ° C, followed by acid reversal.
    DETAILED DESCRIPTION OF THE INVENTION [00023] It has been found that the present invention provides an improved method for treatment with biomass acid in a process for the production of sugars and biofuels. Alpha-hydroxysulfonic acid is effective for the treatment of biomass by hydrolyzing biomass into sugars
    Petition 870180073787, of 08/22/2018, p. 15/62
    7/49 fermentable as pentose, as xylose, at a lower temperature, for example, 100 ° C, to an alpha-hydroxymethane-sulfonic acid or alpha-hydroxyethane acid, producing little or no furfural in the process. A portion of the cellulose has also been shown to hydrolyze under these relatively mild conditions. It has been found that other polysaccharides, such as starch, are also readily hydrolyzed to component sugars by alpha hydroxy sulfonic acids. In addition, alpha-hydroxysulfonic acid is reversible for readily removable and recyclable materials other than mineral acids, such as sulfuric, phosphoric or hydrochloric acid. The lower temperatures and pressures used to treat biomass lead to lower equipment costs. Biomass pretreated in this way has been shown to be highly susceptible to additional saccharification especially enzyme-mediated saccharification.
    [00024] Alpha-hydroxysulfonic acids of the general formula OH
    R, RASOU I where Ri and R 2 are individually hydrogen or hydrocarbyl with up to 9 carbon atoms, which may or may not contain oxygen can be used in the treatment of the present invention. Alpha-hydroxysulfonic acid can be a mixture of the aforementioned acids. The acid can generally be prepared by reacting at least one carbonyl compound or a precursor of the carbonyl compound (for example, trioxane and paraformaldehyde) with sulfur dioxide or a sulfur dioxide precursor (for example, sulfur and oxidizer, or sulfur and reducing agent) and water according to general equation 1 below:
    O
    THE
    Rj R 2
    HO SO 3 H
    Ri r 2
    110
    Ri so / r 2 + ΙΓ where Ri and R 2 are individually hydrogen or
    Petition 870180073787, of 08/22/2018, p. 16/62 hydrocarbyl with up to 9 carbon atoms or a mixture of them. [00025] Illustrative examples of carbonyl compounds usable to prepare the alpha-hydroxysulfonic acids used in this invention are found in which
    R, = R 2 = H (formaldehyde)
    Ri = H, R 2 = CH 3 (acetaldehyde)
    Ri = H, R2 = CH 2 CH 3 (propionaldehyde)
    Ri = H, R 2 = CH 2 CH 2 CH 3 (n-butyraldehyde) Ri = H, R 2 = CH (CH 3 ) 2 (i-butyraldehyde)
    Ri = H, R 2 = CH 2 OH (glycolaldehyde)
    Ri = H, R 2 = CHOHCH 2 OH (glyceraldehyde)
    Ri = H, R 2 = C (= O) H (glyoxal)
    CCI1CI1CIIO
    Ri = H, R 2 = I-1 (furfural)
    C (CII) 4 C (OII)
    Ri = H, R 2 = I-1 (salicylaldehyde)
    C (CH) 4 CH
    Ri = H, R 2 = I-1 (benzaldehyde)
    Ri = R 2 = CH 3 (acetone)
    Ri = CH 2 0H, R 2 = CH 3 (acetol)
    Ri = CH 3 , R 2 = CH 2 CH 3 (methyl ethyl ketone)
    Ri = CH 3 , R 2 = CHC (CH 3 ) 2 (mesityl oxide)
    Ri = CH 3 , R 2 = CH 2 CH (CH 3 ) 2 (methyl i-butyl ketone)
    Laughs; R 2 = (CH 2 ) 5 (cyclohexanone) or Ri = CH 3 , R 2 = CH 2 C1 (chloroacetone).
    [00026] Carbonyl compounds and their precursors can be a mixture of compounds described above. For example, the mixture can be a carbonyl compound or a precursor, such as, for example, trioxane, which is known to thermally revert to formaldehyde, at elevated temperatures, or to an alcohol that can be converted to the aldehyde
    Petition 870180073787, of 08/22/2018, p. 17/62
    9/49 dehydrogenation of alcohol to an aldehyde, by any of the known methods. An example of such a conversion to aldehyde from alcohol is described below. An example of a source of carbonyl compounds may be a mixture of hydroxyacetaldehyde and other aldehydes and ketones produced from rapid pyrolysis oil, as described in Fast Pyrolysis and Bio-oil Upgrading, Biomass-to-Diesel Workshop, Pacific Northwest National Laboratory , Richland, Washington, September 5-6, 2006. Carbonyl compounds and their precursors can also be a mixture of ketones and / or aldehydes, with or without alcohols that can be converted to ketones and / or aldehydes, preferably in range of 1 to 7 carbon atoms.
    [00027] The preparation of alpha-hydroxysulfonic acids by combining an organic carbonyl compound, SO 2 and water is a general reaction and is illustrated in equation 2 for acetone.
    bbO + S0 5 +
    O
    X
    [00028] Alpha-hydroxysulfonic acids appear to be as strong as, if not stronger than HC1, since an aqueous solution of the adduct product has been evaluated to react with NaCl to release the weakest acid, HC1 (see US 3,549 .319). The reaction in equation 1 is a true equilibrium, which results in the easy reversibility of the acid. That is, when heated, the balance shifts to the starting carbonyl, sulfur dioxide and water (form of components). If volatile components (for example, sulfur dioxide) are allowed to leave the reaction mixture via vaporization, or other methods, the acid reaction completely reverses and the solution becomes effectively neutral. Thus, by increasing the temperature and / or decreasing the pressure, the sulfur dioxide can be expelled and the reaction completely reverses due to the Le principle
    Petition 870180073787, of 08/22/2018, p. 18/62
    10/49
    Châtelier, the destination of the carbonyl compound depends on the nature of the material used. If carbonyl is also volatile (for example, acetaldehyde), the material is also easily removed in the vapor phase. Carbonyl compounds such as benzaldehyde, which are poorly soluble in water, can form a second organic phase and be separated by mechanical means. Thus, the carbonyl can be removed by conventional means, for example, continuous application of heat and / or vacuum, steam and nitrogen extraction, solvent washing, centrifugation, etc. Therefore, the formation of these acids is reversible, in that as the temperature is high, sulfur dioxide and / or aldehyde and / or ketone can be instantly distilled from the mixture and condensed or absorbed in another location, in order to to be recycled. These reversible acids, which are approximately as strong as strong mineral acids, have been found to be effective in biomass treatment reactions. Applicants have found that these treatment reactions produce very few of the undesirable furfural by-products produced by other conventional mineral acids. In addition, since acids are effectively removed from the reaction mixture after treatment, neutralization with base and formation of salts to complicate downstream processing is substantially avoided. The ability to reverse and recycle these acids also allows for the use of higher concentrations than would otherwise be economically or environmentally practical. As a direct result, the temperature used in the treatment of biomass can be reduced to decrease the formation of by-products such as furfural or hydroxymethylfurfural.
    [00029] It was found that the position of the equilibrium given in equation 1 at any temperature and pressure is highly influenced by the nature of the carbonyl compound employed, electronic stereochemical effects having a strong influence on the thermal stability of the acid. A more stereochemical volume around carbonyl tends to favor a lower
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    11/49 thermal stability of the acid form. Thus, it is possible to adjust the potency of the acid and the temperature of easy decomposition by selecting the appropriate carbonyl compound.
    [00030] In one embodiment, the acetaldehyde starting material to produce alpha-hydroxysulfonic acids can be supplied by converting ethanol, produced from the fermentation of treated biomass from the process of the invention, to acetaldehyde by dehydrogenation or oxidation . Dehydrogenation can typically be performed in the presence of copper catalysts activated with zinc, cobalt or chromium. At reaction temperatures of 260-290 ° C, the conversion of ethanol per pass is 30-50% and the selectivity for acetaldehyde is between 90 and 95% by mol. By-products include crotonaldehyde, ethyl acetate, and higher alcohols. The acetaldehyde and unconverted ethanol are separated from the hydrogen-rich exhaust gas by washing with ethanol and water. Pure acetaldehyde is recovered by distillation, and an additional column is used to separate ethanol for recycling from higher boiling point products. It may not be necessary to supply pure aldehyde for the above alpha-hydroxysulfonic acid process and the crude current may be sufficient. Hydrogen-rich effluent gas is suitable for hydrogenation reactions, or it can be used as a fuel to provide a portion of the endothermic heat of the ethanol dehydrogenation reaction. The copper-based catalyst has a useful life of several years, but requires periodic regeneration. In an oxidation process, ethanol can be converted to acetaldehyde in the presence of air or oxygen, and using a silver catalyst, in the form of wire gauze or raw crystals. Typically, the reaction is carried out at temperatures between 500 ° and 600 ° C, depending on the ratio of ethanol to air. Part of the acetaldehyde is also formed by dehydrogenation, with subsequent combustion of hydrogen to produce water. At a given reaction temperature, the endothermic heat of dehydrogenation partially compensates for the
    Petition 870180073787, of 08/22/2018, p. 20/62
    12/49 exothermic oxidation heat. Conversion of ethanol per pass is typically between 50 and 70%, and selectivity for acetaldehyde is in the range of 95 to 97 mol%. By-products include acetic acid, CO and CO 2 . The separation phases are similar to those of the dehydrogenation process, except that the steam is generated by heat recovery from the reactor effluent stream. Residual gas vapor consists of nitrogen containing some methane, hydrogen, carbon monoxide and carbon dioxide, it can be used as a poor fuel with a low calorific value. An alternative method to produce acetaldehyde by air oxidation of ethanol in the presence of a Fe-Mo catalyst. The reaction can be carried out at 180-240 ° C and at atmospheric pressure using a multitubular reactor. According to patent examples, selectivities for acetaldehyde between 95 and 99 mole% can be obtained with ethanol conversion levels above 80%.
    [00031] As used herein, the term biomass refers to materials produced by plants (for example, leaves, roots, seeds and stems). Common sources of biomass include: agricultural waste (eg, corn stalks, straw, seed husks, sugar cane remains, bagasse, nut shells, and livestock manure, poultry and pigs), wood materials (for example, eg wood or bark, sawdust, wood cutting and factory scrap); solid urban waste (for example, waste paper and yard shavings); and energy crops (for example, poplars, willows, panic grass, alfalfa, blue pasture, corn, soybeans, seaweed and seaweed). The term biomass also refers to the primary building blocks of all of the above, including, but not limited to, saccharides, lignins, celluloses, hemicelluloses and starches. The term polysaccharides refers to structures of polymeric carbohydrates, of repeating units (or mono- or di-saccharides), joined together by glycosidic bonds. These structures are usually linear, but can contain varying degrees of branching. Examples include storage polysaccharides such as starch and glycogen and structural polysaccharides
    Petition 870180073787, of 08/22/2018, p. 21/62
    13/49 such as cellulose and chitin. Biomass is typically pre-processed for particles of appropriate size, which can include milling. Without the intention of restricting the scope of the invention, it is typically found that it is easier to process smaller particles of biomass. Biomass which is reduced in size to facilitate handling (for example, less than 1.3 cm) are particularly susceptible materials.
    [00032] In some embodiments, the reactions described below are carried out in any appropriate design system, including systems comprising continuous flow (CSTR, such as buffer flow reactors), in batch, semi-batch vessels or multiple compacted bed systems and reactors and flow reactors. For reasons of economic feasibility only, it is preferable that the invention be practiced using a steady-state steady-state flow system. In an advantage of the process in contrast to the pretreatment reactions of diluted acids in which residual acid is left in the reaction mixture (<1% by weight of sulfuric acid), the lower temperatures using these acids (10 to 20% by weight) result in substantially lower pressures in the reactor, resulting in potentially less expensive processing systems, such as plastic-lined reactors, duplex stainless steel reactors, and type 2205 reactors. [00033] Figure 2 shows a form of rehabilitation of the present invention for the conversion of biomass to sugars. In this form of rewiring, a biomass sludge charge 112 is introduced to a hydrolysis reaction 114, along with the recycle stream 118. The hydrophobic reaction 114 may comprise a number of components, including alpha-hydroxysulfonic acid generated in situ. The term in situ as used herein refers to a component that is produced within the overall process, which is not limited to a particular reactor, for production or use and, therefore, is synonymous with a component generated in process. The current of
    Petition 870180073787, of 08/22/2018, p. 22/62
    14/49 reacted product 116 from 114 is introduced into the acid removal system 120, where the acid is removed in its component form and then 122 (and, optionally, purified 124) is recovered and recycled via the recycle 118 to 114 and product stream 126 containing at least one fermentable sugar (e.g., pentose and optionally hexose) substantially free of alpha-hydroxysulfonic acids is produced for further processing. The acid removed as components is recycled into 114 as components and / or in its recombined form.
    [00034] Figure 3 shows another embodiment of the present invention for converting biomass to sugars. In this embodiment, a biomass feed charge 112 is introduced into a hydrolysis reaction 114, along with a recycle stream of 118. The hydrolysis reaction 114 can comprise a number of components, including alpha hydroxysulfonic acid generated in situ. . The reaction product stream 116 from 114 is introduced into the acid removal system 120, where the acid is removed in its component form, then 122 is recovered (and, optionally, rinsed 124) and recycled through the flow stream. recycle from 118 to 114 and product stream 126 containing at least one fermentable sugar (eg, pentose and optionally hexose) without alpha-hydroxysulfonic acid being produced. The acid is removed as components recycled to 114 as components and / or in its recombined form. The product stream 126 is filtered off 200 to produce a liquid stream 210 containing fermentable sugars (e.g., pentose and hexose optionally) and a wet solid stream 220 containing cellulose and lignin. [00035] Several factors affect the conversion of the biomass feed load in the hydrolysis reaction. The carbonyl compound or incipient carbonyl compound (such as trioxane) with sulfur dioxide and water should be added in an amount and under conditions that are effective to form alpha-hydroxysulfonic acids. The temperature and pressure of the hydrolysis reaction
    Petition 870180073787, of 08/22/2018, p. 23/62
    15/49 must be in the range to form alpha-hydroxysulfonic acids and to hydrolyze biomass into fermentable sugars. The amount of carbonyl compound or its precursor and sulfur dioxide must be to produce alpha-hydroxysulfonic acids in the range of 1% by weight, preferably 5% by weight, more preferably 10% by weight, to 55% by weight, preferably at 50% by weight, more preferably up to 40% by weight, based on the total solution. For the reaction, excess sulfur dioxide is not necessary, but excess sulfur dioxide can be used to conduct the equilibrium in equivalent 1 to favor the acid form at elevated temperatures. The contact conditions of the hydrolysis reaction can be conducted at temperatures preferably at least 50 ° C, depending on the alpha-hydroxysulfonic acids used, although such a temperature can be as low as the ambient temperature, depending on the acid and pressure used. The contact condition of the hydrolysis reaction can preferably vary up to and including 150 ° C, depending on the alpha-hydroxysulfonic acid used. In a more preferred condition the temperature is at least 80 ° C, more preferably at least 100 ° C. In a more preferred condition the temperature range goes up to and includes 90 ° C to 120 ° C The reaction is preferably conducted at as low a pressure as possible, taking into account the requirement to contain excess sulfur dioxide. The reaction can also be conducted at a pressure as low as 1 bar, preferably 4 bar, at a monometric pressure as high as up to 10 bar. The optimum temperature and pressure to be used will depend on the particular alpha-hydroxysulfonic acid chosen and optimized based on economical considerations of metallurgy and container vessels as practiced by those skilled in the art.
    [00036] The amount of acid solution for the dry weight biomass determines the final concentration of fermentable sugar obtained. Thus, a concentration of biomass as high as possible is desirable. This is
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    16/49 balanced by the biomass absorption nature, with mixing, transport and heat transfer becoming more and more difficult as the relative amount of solid to liquid in the biomass is increased. Numerous methods have been used by those skilled in the art to circumvent these obstacles to mixing, transport and heat transfer. Thus, the weight percentage of biomass solids for total liquids (consistency) can be as low as 1% or as high as 33%, depending on the chosen device and the nature of the biomass.
    [00037] The temperature of the hydrolysis reaction can be chosen so that the maximum amount of extractable carbohydrates is hydrolyzed and extracted as fermentable sugar (more preferably pentose and / or hexose) from the biomass feed load while limiting the formation of degradation products.
    [00038] In some embodiments, a plurality of reactor vessels can be used to carry out the hydrolysis reaction. These vessels can have any design capable of carrying out a hydrolysis reaction. Suitable reactor vessel models may include, but are not limited to, batch, drip bed, concurrent, counter-current, agitated tank, or fluidized bed reactors. Reactor scaling can be employed to arrive at the most economical solution. The solids in the remaining biomass feed charge can then optionally be separated from the liquid stream, to allow more severe processing of the resistant solids or to pass directly into the liquid stream for further processing, which may include enzymatic hydrolysis, fermentation, extraction, distillation and / or hydrogenation. In another embodiment, a series of reactor vessels can be used with an increasing temperature profile, so that a desired sugar fraction is extracted in each vessel. The outlet of each vessel can then be cooled before the currents are combined, or the currents can be fed individually to the next reaction for conversion.
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    17/49 [00039] Appropriate reactor models may include, but are not limited to, a re-mixed reactor (for example, a stirred tank, a bubbling column, and / or a mixed jet reactor) may be employed, if the viscosity and characteristics of the partially digested biobased feed charge and liquid reaction media is sufficient to operate in a regime where the solids from the biobased feed charge are suspended in an excess liquid phase (as opposed to a stacked pile digester ). It is also conceivable that a drip bed reactor can be used with the biomass present as a stationary phase and a solution of alpha-hydroxysulfonic acid passing over the material.
    [00040] The treatment reaction product contains fermentable sugar or monosaccharides, such as pentose and / or hexose, which is suitable for further processing. Residual alpha-hydroxysulfonic acid can be removed by applying heat and / or vacuum from the product stream containing fermentable sugar to reverse the formation of alpha-hydroxysulfonic acid to its starting material to produce a stream containing fermentable sugar substantially free of alpha-hydroxysulfonic acid. In particular, the product stream is substantially free of alpha-hydroxysulfonic acid, meaning that no more than 2% by weight is present in the product stream, preferably no more than 1% by weight, more preferably no more than 0 , 2 wt%, more preferably not more than 0.1 wt present in the product stream. The temperature and pressure will depend on the particular alpha-hydroxysulfonic acid used and minimizing the temperatures employed are desirable to preserve the sugars obtained in treatment reactions. Typically, removal can be carried out at temperatures in the range of 50 ° C, preferably between 80 ° C and more preferably from 90 ° C to 110 ° C, up to 150 ° C. The monometric pressure can be in the range of 0.5 bar (gauge), to 2 bar (gauge), more preferably 0.1
    Petition 870180073787, of 08/22/2018, p. 26/62
    18/49 bar (absolute) to 1 bar (gauge). It can be appreciated by a person skilled in the art that the treatment 114 and acid 120 removal reaction can take place in the same container or in a different vessel or in a number of different types of vessels, depending on the reactor configuration and scaling provided that the system is designed so that the reaction is conducted under favorable conditions for the formation and maintenance of alpha-hydroxysulfonic acid and favorable removal for the reverse reaction (as components). As an example, the reaction in reactor vessel 114 can be operated at about 100 ° C and a pressure of 4 bar, in the presence of alpha-hydroxyethanesulfonic acid and the removal vessel 120 can be operated at approximately 110 ° C and a pressure of 0 , 5 bar (gauge). It is also contemplated that the reversal can be favored by the reactive distillation of the formed alpha-hydroxysulfonic acid. In recycling the removed acid, optionally additional carbonyl compounds, SO 2 , and water can be added as needed. The removed starting material and / or alpha-hydroxysulfonic acid can be condensed and / or purified by contact with water and recycled for reaction 114.
    [00041] Thus, a typical reaction mixture contains (a) a biomass containing polysaccharides, (b) at least one alpha-hydroxysulfonic acid, and (c) water. Since some of the biomass is hydrolyzed, the reaction mixture contains (a) a biomass containing polysaccharides, (b) at least one alpha-hydroxysulfonic acid (c) water and (d) at least one fermentable sugar. [00042] In one embodiment, the cellulose-containing product stream can be further hydrolyzed by other methods, for example, enzymes to further hydrolyze biomass into sugar products containing hexose and pentose (eg, glucose) and fermented to produce alcohols as described in US publication 2009/0061490 and US patent 7781191.
    [00043] In yet another embodiment, fermentable sugar can be converted to furfural or hydroxymethylfurfural (HMF) or even
    Petition 870180073787, of 08/22/2018, p. 27/62
    19/49 fermented in alcohols. Although, in some embodiments, it may be desirable to minimize furfural formation, if furfural formation is desired, the acid-containing solution from step (b) can still be heated to a temperature in the range of 110 to 160 ° C, preferably in the range of 120 to 150 ° C, to form at least one product stream containing furfural. In one embodiment, the temperature of step (b) is maintained at a temperature of 100 ° C or less, if it is desirable to obtain minimal furfural in the product stream.
    [00044] In yet another embodiment, fermentable sugars can be converted to higher hydrocarbons as a biofuel component using catalytic hydrogenation and condensation techniques, rather than another enzyme hydrolysis and fermentation. Typically, the product containing fermentable sugar is contacted with hydrogen in the presence of a hydrogenolysis catalyst to form a plurality of oxygenated intermediates, and then further processing the oxygenated intermediates to produce a fuel mixture in one or more processing reactions. In one embodiment, the condensation reaction can be used together with other reactions to generate a fuel mixture and can be catalyzed by a catalyst comprising acidic or basic functional sites, or both, to produce a liquid fuel. As used here, the term higher hydrocarbons refers to hydrocarbons having a lower oxygen-to-carbon ratio than at least one component of the biomass feed load. As used herein, the term hydrocarbon refers to an organic compound comprising primarily hydrogen and carbon atoms, which is also an unsubstituted hydrocarbon. In certain embodiments, the hydrocarbons of the invention also comprise heteroatoms (for example, oxygen or sulfur), and thus the term hydrocarbon can also include substituted hydrocarbons.
    Petition 870180073787, of 08/22/2018, p. 28/62
    20/49 [00045] In such an example, the product stream containing fermentable sugar can be further processed to produce mixtures of C4 + compounds usable for biofuels, as described in US publication No. US2011 / 0154721 and US patent application serial number 13/106509 deposited on May 12, 2011. As such another example, the product stream containing fermentable sugar can be processed to produce mixtures of C4 + compounds usable for biofuels, as described in US publication No. 20080216391. The feeding of sods it may also be suitable for use in reactions that have rapid pyrobase leading to fuels and chemicals.
    [00046] The term fermentable sugar refers to obgosaccharides and monosaccharides that can be used as a carbon source (for example, pentoses and hexoses) by a microorganism in a fermentation process. It is contemplated that fermentable sugar can be fermented, as described above, but it can also be processed by other methods, without fermentation to produce fuels, as described above. The term pentose refers to monosaccharides, with five carbon atoms. The term hexose refers to monosaccharides, with six carbon atoms.
    [00047] In an enzymatic hydrolysis - fermentation process the pH of the pre-treated abmentation load for the enzymatic hydrobe is typically adjusted to be within a range that is optimal for the cellulase enzymes used. Generally, the pH of the pretreated ablation load is adjusted within a range of 3.0 to 7.0, or any pH between this range. [00048] The temperature of the treated ablation load is adjusted so that it is within the optimum range for cellulase enzyme activity. Generally, a temperature of 15 ° C to 100 ° C, 20 ° C to 85 ° C, 30 ° C to 70 ° C, preferably or at any temperature in between, is appropriate for most cellulase enzymes. The cellulase enzymes and the β-gbcosidase enzyme are added to the pre-treated feed,
    Petition 870180073787, of 08/22/2018, p. 29/62
    21/49 before, during, or after adjusting the temperature and pH of the aqueous suspension after pretreatment. Preferably, the cellulase enzymes and the β-glycosidase enzyme are added to the pre-treated lignocellulosic feed load after adjusting the temperature and pH of the suspension.
    [00049] The term cellulase enzymes or cellulases means a mixture of enzymes that hydrolyze cellulose. The mixture can include cellobiohydrolases (CBH), glucobiohydrolases (PAP), endoglucanoses (EG), and β-glycosidase. By the term β-glycosidase, we mean any enzyme that hydrolyzes the glucose dimer, cellobiose, to glucose. In a non-limiting example, a cellulase mixture can include, EG, CBH, and β-glycosidase enzymes.
    [00050] Enzymatic hydrolysis can also be carried out in the presence of one or more xylanose enzymes. Examples of xylanose enzymes that can also be used for this purpose and include, for example, xylanose, 2 (Xynl and Xyn2) and β-xylosidase, which are typically present in cellulase mixtures.
    [00051] The process can be carried out with any type of cellulase enzymes, regardless of their origin. Non-limiting examples of cellulases that can be used include those obtained from fungi of the genera Aspergillus, Humicola, and Trichoderma, Myceliophthora, Chrysosporium and bacteria of the genus Bacillus, Thermobifida and Thermotoga. In some embodiments, the filamentous fungal host cell is an Acremonium, Aspergillus, Aureobasidium, Bjerkandera, Ceriporiopsis, Chrysosporium, Coprinus, Coriolus, Cryptococcus, Filibasidium, Fusarium, Humicola, Magnaporthe, Mucor, Neocore, Mycora, Neutral, Mycelor , Penicillium, Phanerochaete, Phlebia, Piromyces, Pleurotus, Schizophyllum, Talaromyces, Thermoascus, Thielavia, Tolypocladium, Trametes or Trichoderma.
    [00052] The cellulase enzyme dosage is chosen to convert the
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    22/49 cellulose of the pre-treated glucose feed. For example, an appropriate cellulase dosage can be 0.1-40.0 unit (s) of filter paper (FPU or IU) per gram of cellulose, or any amount present between them. The term filter paper unit (s) refers to the amount of enzyme required to release 2 mg reducing sugar (eg gbcose), from a 50 mg piece of Whatman No. 1 filter paper in 1 hour at 50 ° C at approximately pH 4.8.
    [00053] In practice, hydrophobic can be replenished in a hydrophobic system, which can include a series of hydrophobic reactors. The number of hydrophobic reactors in the system depends on the cost of the reactors, the volume of the aqueous suspension, and other factors. Enzymatic hydrobse with cellulase enzymes produces an aqueous stream of sugar (hydrated), comprising glucose, unconverted cellulose, bignin and other sugar components. Hydrobes can be re-made in two steps (see US patent No. 5,536,325), or can be re-made in a single step.
    [00054] In the fermentation system, the aqueous sugar stream is then fermented by one or more of a fermentation microorganism to produce a fermentation broth, comprising the alcohol fermentation product usable as biofuels. In the fermentation system, any one of a number of known microorganisms (for example, yeast or bacteria) can be used to convert sugar into ethanol or other alcohol fermentation products. Microorganisms convert sugars, including, but not limited to, glucose, mannose and galactose present in the clarified sugar solution in a fermentation product. [00055] Many known microorganisms can be used in the present process to produce the desired alcohol for use in biofuels. Clostridium, Escherichia coli (E. coli) and recombinant strains of E. coli, genetically modified strain of Zymomonas mobilis, as described in US2003 / 0162271, 60/847, 813 and 60/847. 856 are
    Petition 870180073787, of 08/22/2018, p. 31/62
    23/49 some examples of such bacteria. The microorganisms can also be a yeast or a filamentous fungus of the genus Saccharomyces, Kluyveromyces, Candida, Pichia, Schizosaccharomyces, Hansenula, Kloeckera, Schwanniomyces, Yarrowia, Aspergillus, Trichoderma, Humicola, Acremonium, Fusarium and Penicillium. Fermentation can also be carried out with recombinant yeast designed to ferment both pentose and hexose sugars in ethanol. Recombinant yeasts that can ferment one or both sugars pentose xylose and arabinose in ethanol are described in US patents. No. 5,789,210, US patent No. 6,475,768, European patent EP 1,727,890, European patent EP 1 863,901 and WO 2006/096130. Use of xylose can be mediated by the xylose reductase / xylitol dehydrogenase pathway (for example, WO9742307 and W09513362 Al 19971113 19950518 Al) or the xylose isomerase pathway (for example, W02007028811 and W02009109631). It is also contemplated that the fermentation organism can also produce fatty alcohols, for example, as described in WO 2008/119082 and PCT / US 07/011923. In another embodiment, fermentation can be carried out by yeasts capable of fermenting predominantly C6 sugars, for example, using commercially available strains, such as Thermosacc and Superstart.
    [00056] Preferably, fermentation is carried out at or near the optimum temperature and pH of the fermentation microorganism. For example, the temperature can be 25 ° to 55 ° C, or any amount between them. The dose of the fermentation microorganism will depend on other factors, such as the activity of the fermentation microorganism, the desired fermentation time, the reactor volume and other parameters. It will be appreciated that these parameters can be adjusted as desired by one skilled in the art to achieve optimal fermentation conditions.
    [00057] Fermentation can be carried out in batch modes,
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    24/49 continuous or batch fed, with or without agitation. The fermentation system can employ a series of fermentation reactors.
    [00058] In some embodiments, the hydrolysis system and the fermentation system can be carried out in the same vessel. In one embodiment, the hydrolysis can be partially completed and the partially hydrolyzed stream can be fermented. In one embodiment, a simultaneous saccharification and fermentation (SSF) process, where the hydrolysis system can be performed until the final target of percentage solids is reached and then the hydrolyzed biomass can be transferred to a fermentation.
    [00059] The fermentation system produces an alcohol stream preferably containing at least one alcohol with 2 to 18 carbon atoms. In the recovery system, when the product to be recovered in the alcohol stream is a distillable alcohol, such as ethanol, the alcohol can be recovered by distillation in a manner known to separate this alcohol from an aqueous stream. If the product to be recovered in the alcohol stream is a non-distillable alcohol, such as fatty alcohols, the alcohol can be recovered by removing alcohols as solids or oils from the fermentation vessel, thereby separating it from the effluent stream aqueous. [00060] Although the invention is susceptible to various modifications and alternative forms, specific embodiments of it are shown by means of examples described in detail here. It should be understood that its detailed description is not intended to limit the invention to the particular form described, but, on the contrary, the intention is to cover all modifications, equivalents and alternatives that are within the spirit and scope of the present invention, such as defined by the appended claims. The present invention will be illustrated by the following illustrative embodiment, which is given by way of illustration only and should not be construed as limiting the claimed invention in any way.
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    25/49
    ILLUSTRATIVE ACHIEVEMENTS
    General Methods and Materials [00061] In the examples, aldehyde or aldehyde precursors were obtained from Sigma-Aldrich.
    [00062] Complete bagasse having the following components analyzed using standard TAPPI methods (T-249, T-222, T-211) and the following average composition, on a dry basis:
    Glucan 44.5% by weight Xylan 24.6% by weight Lignin 23.25% by weight Gray 2.79% by weight Others 4.86%
    Analytical methods
    Determination of oxygenated components in the aqueous layer.
    [00063] A sample or standard is analyzed by injection into a current of a mobile phase, which flows through a Bio-Rad column (Aminex HPX-87H, 300 mm x 7.8 mm). Reverse phase HPLC system (Shimadzu) equipped with IR and UV detectors and the signals are recorded as peaks in a data acquisition and data processing system. The components are quantified using external calibration through calibration curves based on injection of known concentrations of the target components. Some of the components were calculated using a single pattern point. The reference samples contained 0.5% by weight of glucose, xylose and sorbitol in water
    HPLC instrument conditions:
    Column: Bio-Rad Aminex HPX-87H (300 mm x 7.8 mm) Flow rate: 0.6 ml / minute
    Column oven: 30 ° C Injection volume: 10 μΐ
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    26/49
    UV detector: @ 320 NM
    IR detector: Mode - A; track - 100
    Run time: 70 minutes
    Mobile Phase: 5 mM Sulfuric acid in water
    Sample is injected directly or diluted with water first, but ensuring that there is no indication. It passes through the 0.2 pm syringe filter, if there is precipitation in the sample or in the diluted sample. The samples were analyzed for glucose, xylose, cellobiose, sorbitol, formic acid, acetic acid, arabinose, hydroxymethyl furfural, and furfural. EXAMPLES
    General procedure for the formation of alpha-hydroxysulfonic acids.
    [00064] Aldehydes and ketones will react quickly with sulfur dioxide in water to form alpha-hydroxysulfonic acids, according to equation 1 above. These reactions are generally quick and somewhat exothermic. The order of addition (SO 2 for carbonyl or carbonyl for SO 2 ) does not appear to affect the reaction result. If carbonyl is capable of aldol reactions, the preparation of concentrated mixtures (> 30% by weight) is best conducted at temperatures below room temperature to minimize side reactions. Applicants have found that it is beneficial to control the course of the reaction using infrared spectroscopy (ISIR) in situ using probes capable of being inserted into vessels or pressure reaction systems. There are several manufacturers of such systems, such as Mettler Toledo AutoChem Sentinal probe. In addition to being able to see the starting materials: water (1640 cm 1 , carbonyl (approximately 1.750 cm ' 1 to 1650 cm 1 , depending on the organic carbonyl structure) and SO2 (1331 cm 1 ), the formation of alpha acid -hydroxysulfonic is accompanied by the formation of characteristic bands of the SO3 group (broad band of approximately 1,200 cm 1 ) and extensions of the alpha-hydroxy group (single bands for multiples around 1,125 cm 1 ). In addition to monitoring the formation of a alpha hydroxy acid
    Petition 870180073787, of 08/22/2018, p. 35/62
    27/49 sulfonic, the relative position of the equilibrium at any temperature and pressure can be easily assessed by the relative heights of the peaks of the starting components and the acid complex. The definitive presence of alpha-hydroxy sulfonic acid under conditions of biomass hydrolysis can also be confirmed with ISIR and it is possible to monitor the growth of sugars in the reaction mixture by monitoring the appropriate IR bands.
    Example 1
    Formation of 40% by weight alpha-hydroxyethane sulfonic acid from acetaldehyde.
    [00065] In a pressure reaction vessel of 340.19 g Lab-Crest (Fischer-Porter bottle) 260 grams of degassed water with nitrogen were placed. To this was added 56.4 g of acetaldehyde through a syringe, with stirring. The acetaldehyde / water mixture showed no apparent vapor pressure. The contents of the Fischer-Porter flask were transferred to a cooled 600 ml C276 steel reactor equipped with an IR SICOMP optical device. A single-ended Hoke vessel was loaded with 81.9 grams of sulfur dioxide that was inverted and connected to the top of the reactor. SO 2 was added to the reaction system in a single portion. The pressure in the reactor rose to about 3 bar and then quickly dropped to atmospheric pressure as ISIR indicated the onset and then the rapid consumption of SO 2 . The temperature of the reaction mixture rose approximately 31 ° C during the formation of the acid (from 14 ° C to 45 ° C). ISIR and reaction pressure indicated that the reaction was complete in approximately 10 minutes. The final solution presented an infrared spectrum with the following characteristics: a wide band centered at 1,175 cm 1 and two high bands at 1038 cm ' 1 and 1015 cm 1 The reactor was purged twice by pressurization with nitrogen at 3 bar and then , ventilation. This produced 397 grams of a stable alpha acid solution Petition 870180073787, of 22/08/2018, p. 36/62
    28/49 40% by weight sulfonic hydroxyethane without any residual acetaldehyde or SO2. A sample of this material was dissolved in C-DMSO and analyzed by 13 C NMR, revealing two absorbances of carbon at 81.4 and 18.9 ppm corresponding to the two carbons of sulfonic alpha-hydroxyethane acid, without other organic impurities until the limit detection (800: 1).
    Example 2
    Formation of 41% by weight alpha-hydroxyethane sulfonic acid from trioxane.
    [00066] In a 600 ml C276 steel reactor equipped with SICOMP IR optical device, 280.29 grams of nitrogen degassed water and 46.88 grams of trioxane were added. The reactor was sealed and purged with nitrogen and a one-way Hoke vessel, loaded with 101.26 grams of sulfur dioxide, was inverted and connected to the top of the reactor. SO2 was added to the reaction system in a single portion. There was no apparent reaction and ISIR revealed IR bands consistent only with the starting components. This is consistent with the fact that trioxane must be heated to generate carbonyl formaldehyde. The reaction mixture was heated to 105 ° C, with stirring, the pressure of the mixture rising to 8.3 bar. Upon approaching the target temperature an exothermic reaction occurred, the pressure in the reactor dropped to 4.1 bar due to the consumption of SO2 and the temperature rose from 105 ° C to 124 ° C. ISIR and reaction pressure indicated that the reaction was complete in approximately 10 minutes, once started. The final solution presented an infrared spectrum with the following characteristics: a broad band centered at 1,185 cm 1 and a single acute band at 1034 cm ' 1 (a small peak due to the excess of SO2 at 1331 cm 1 was observed). Once the reactor was cooled to room temperature and purged twice by pressurizing with nitrogen at 3 bar and then venting, this produced 423.92 grams of a stable 41% by weight solution of alpha-hydroxymethane sulfonic acid without formaldehyde or residual SO2.
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    29/49
    Example 3
    Formation of 40% by weight alpha-hydroxyethane sulfonic acid from paraformaldehyde.
    [00067] In a 600 ml sealed and sparged nitrogen autoclave equipped with an IR SICOMP probe 285.02 grams (ml) of deionized water sprinkled with nitrogen and 49.31 grams of paraformaldehyde (Aldrich 158127, batch MKAA1858, 95) were loaded %). The autoclave was sealed, sparged with nitrogen and stirred. ISIR showed water and dissolved paraformaldehyde. A Hoke vessel containing 100.01 g of sulfur dioxide is inverted, connected to the reactor as a blow box injector and the sulfur dioxide injected into the reactor through a ball valve. ISIR immediately showed a rising SO2 band of 1,331 cm 1 . The pressure in the reactor rose to 3.31 bar (gauge). A slow reaction starts with bands indicative of alpha-hydroxyethane sulfonic acid growing inside.l The reaction accelerates as an exothermic reaction occurs, the reactor temperature rises from 25 ° C to 39 ° C, as the pressure of the reactor drops to 0.5 bar (gauge). ISIR shows the rapid growth of alpha-hydroxyethane sulfonic acid and SO2 disappears from the reaction mixture. The reactor is allowed to cool to room temperature and purged twice by pressurizing with nitrogen to 3 bar and then ventilated, producing 430 grams of a 40% by weight solution of alpha-hydroxyethane sulfonic acid. Example 4
    Formation of 10% by weight alpha-hydroxysulfonic acid from 2furaldehyde.
    [00068] In a 600 ml autoclave, sealed and sparged with nitrogen, equipped with an IR SICOMP probe and heating band, 374.92 grams of deionized water sprinkled with nitrogen and 22.59 g of furfural (Aldrich batch MKBC2892 ). A vase of
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    30/49
    Hoke containing 15.25 grams of sulfur dioxide (234 mmol) is reversed and connected to the reactor like a blow box injector. The reactor is closed and purged three times with nitrogen gas. The agitator is turned on and ISIR acquisition initiated. Sulfur dioxide is injected into the reactor through a ball valve, the pressure in the reactor briefly peaks at 2.25 bar (gauge) and SO 2 in the reaction mixture is observed in the ISIR spectrum. The formation of alpha-hydroxymethanesulfonic acid was immediately observed at ISIR by the growth of a wide band of 1,198 cm ' 1 with a peak peak at 1154 cm 1 and two sharp bands at 1034 cm' 1 and 1,015 cm 1 . The reactor temperature rises from 26 to 29 ° C. This produces approximately 410 grams of a 10% by weight alpha-hydroxysulfonic acid solution.
    Example 5
    Formation of 20% by weight bis-alpha-hydroxyethane sulfonic acid.
    [00069] In a 600 ml C276 reactor equipped with an IR optical system, 366.36 grams of water sprayed with nitrogen and 63.45 grams of 40% by weight glyoxal solution were loaded. The reactor was sealed, stirring started and purged twice with nitrogen. A Hoke vessel containing 58.56 grams of sulfur dioxide is inverted, connected to the reactor as a blow box injector and the sulfur dioxide injected into the reactor through a ball valve. ISIR immediately showed an SO 2 band growing at 1,331 cm ' 1 . The pressure in the reactor increased. A slow reaction begins with bands indicative of bis-hydroxyethane sulfonic acid growing (broad peak at 1202 cm 1 and acute peak at 1,030 cm 1 ). The reaction accelerates as an exothermic reaction occurs, the reactor temperature rises from 23 ° C to 29 ° C, as the reactor pressure drops. ISIR shows the slow growth of alpha-hydroxyethane sulfonic acid and SO 2 gradually disappears from the reaction mixture. The reactor was heated to 50 ° C and held there for 30 minutes to complete the reaction. The reactor is left
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    31/49 cool to room temperature and the pressure in the reactor dropped to atmospheric. There is only one trace of SO 2 in the ISIR spectrum (slight excess used). This was purged twice by pressurizing with nitrogen to 3 bar and then venting to remove excess SO 2 , the procedure produced 485 grams of a 20% by weight solution of bis-alpha-hydroxyethane sulfonic acid. Note that commercial glyoxal solutions contain very little free carbonyl, most of the material bound as hydrates and oligomers, this shows that the formation of alpha-hydroxysulfonic acid effectively shifts this balance to low temperatures to completely reverse all the incipient carbonyl in complexed bisacid.
    Examples 6-27
    Hydrolysis of biomass with alpha sulfonic acid hydroxyethane solutions, Examples 6 to 27.
    [00070] This is the general procedure for Examples 6 to 27, the conditions used and the results are in Table 1, the type of acid used is listed in column B, the concentration in column C, the target temperature in column D, and the time at reaction temperature in column E. In a 300 ml autoclave equipped with a DiComp IR probe, place approximately 12 grams of chopped dry bagasse. To do this, add 100 grams of a solution of alpha-hydroxyethane sulfonic acid, carefully pouring this material over the bagasse in the reactor. Seal the reactor equipped with heating bands and stir the mixture for 5 minutes, then the system is purged lightly three times with nitrogen. The reactor now contains a mixture comprising approximately 10.7% by weight of biomass in contact with the alpha-hydroxy sulfonic acid solution (112 grams of total solution).
    [00071] The reaction mixture is stirred (1000-1500 rpm, as noted in column I, using a 45 ° downward step impeller) and
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    32/49 start the acquisition of the IR spectra. The reaction mixture is then heated to the target temperature and maintained for the specified period of time. Heating is stopped and the reactor cooled to room temperature, using a compressed air flow. The reactor was vented and then purged with a slow flow of nitrogen for a few minutes to eliminate any sulfur dioxide in the gas cover. The reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner. The reactor was rinsed with three separate 25 ml portions of water (note the weight on all rinses), the rinses being used to complete the transfer of solids and rinse the solids in the funnel. In order to completely rinse the solids in the funnel, it was necessary to turn off the vacuum, add water, suspend the solids by hand stirring and then restore the vacuum to the filter. The cumulative weight of the filtrate and rinses was obtained. The filtrate was then analyzed by HPLC and the recovery of the materials from the biomass calculated by comparison with the amount of precursors present in the biomass. The solids were dried at a constant weight in air.
    [00072] Xylose recovered over time and grams of furfural / grams of xylose produced over time for Examples 10 to 20 are shown in Figures 4 and 5, respectively. For comparison, furfural made from a pretreatment with sulfuric acid diluted at a traditional elevated temperature as described in Patent Application Publication US2010 / 0184151 is shown as a circle in Figure 5.
    Petition 870180073787, of 08/22/2018, p. 41/62 σ
    ΓΌ
    Table 1
    - Agitator speed 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1500 rpm | 1500 rpm | 1500 rpm | 1500 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | 1000 rpm | K % furfural recovery in filtrate * 0.37 | V)σ 0.60 | * 0.073 | 0.47 | 0.27 | COONLY 3.33 | 0.54 | CO σr-> „ C0σ 0.67 | 9.37 | 0.82 | 0.88 | Ü % glucose recovery in filtrate ** σΐ 4.24 | 3.84 | THESAWσ Tfσ in 00 σΐ 4.32 | V)sd 7.79 | 3.77 | 5.65 | 5.50 | 6.20 | TtTf 12.58 | 12.43 | 4.66 | 0.48 | go %xylose recovery in filtrate * 55.43 | 55.26 | 55.97 | 15.09 | 2.56 | 54.89 | 46.17 | 66.16 | 65.02 | 75.60 | 82.7 | 66.12 | 72.9 | 70.68 | 73.46 | 44.46 | 55.48 | 15.33 | 67.12 | onlyoc 53.85 | 73.16 | ω Time in temperature (h) 22.5 | 24 | V) 26.5 | ***σ O,CO ***σ C0 C0 C0 22 | COCO 25.5 | ***σ ***σ CO CO Q Reaction temperature (° C) 1 os 1 1 08 | 1 80 | 1 08 | 1 80 | 1 08 1 8 1 90 | 8 8 8 1 90 | 1 06 1 1 06 1 8 1 08 | 8 1 08 | 1 80 | 1 08 1 1 08 1 1 08 1 u Acid concentration (% by weight) O O 1 op | V σι-H σ σ σι-H σ σ σ σ 1 0Z | σ 1 oz | σ 1 10.25 | Tf Tf σι-H σ σ « Acid Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Alpha-hydroxyethane sulfonic acid | Bis-alpha-dihydroxyethane sulfonic acid Bis-alpha-dihydroxyethane sulfonic acid < Example r- 00 THE σ C0 CO i — H Tf V) r- 00 THE 1 20 | C0 1 22 | COCO 1 24 | V)CO CO CO
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    34/49
    Examples 28 and 29
    Biomass treatment with a hydroxyethane sulfonic acid versus SO2 water.
    [00073] Reaction with SO2 and water (without carbonyl compound, thus without alpha-hydroxysulfonic acid):
    In a 300 ml autoclave equipped with an IR DiComp probe, 12 grams of chopped dry bagasse were placed. For this, 95 grams of water (5,277 mmoles) were added, gently pouring over the bagasse in the reactor. Seal the reactor equipped with heating bands and start the agitator (1500 rpm), then the system is lightly purged three times with nitrogen. Invert a single-ended Hoke vessel containing 5.44 grams of sulfur dioxide (84.9 mmol) and connect this to the reactor. The Hoke vessel was opened for the reactor and the SO2 added in a single portion. Their presence in the reaction mixture was confirmed or a strong acute band in the ISIR characteristic of SO 2 in 1331 cm 1 . The reactor now contains a mixture comprising approximately 10.71% by weight of the biomass in contact with a mixture of SCV water at 0.61 bar (gauge) and 25 ° C. The reaction mixture was heated to 90 ° C and held there for 4 hours. The pressure at 90 ° C was 3.13 bar (gauge). Heating is stopped and the reactor cooled to room temperature, using a compressed air flow. The reactor was vented and then purged with a slow flow of nitrogen for a few minutes to eliminate any sulfur dioxide in the gas cover. The reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner. The reactor was rinsed with three separate 25 ml portions of water to complete the transfer of solids and rinse the solids in the funnel. The accumulative weight of the filtrate and rinses was obtained. The filtrate was then analyzed by HPLC and the recovery of materials from biomass calculated by comparison
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    35/49 with the amount of precursors present in the biomass. The solids are dried to a constant weight in air. The results are shown in Table 2.
    [00074] Reaction with acetaldehyde, SO2 and water (alpha-hydroxyethanesulfonic acid):
    In a 300 ml autoclave equipped with an IR DiComp probe 12.03 grams of chopped dry bagasse were placed. For this, 100 grams of a 10% solution of alpha-hydroxyethane sulfonic acid (this is composed of about 91.26 grams of water, 5.07 grams of SO2 and 3.5 grams of acetaldehyde) were added, carefully pouring this material on bagasse in the reactor. The reaction mixture was heated to 90 ° C and held there for 4 hours. The pressure at 90 ° C was 1.36 bar (manometric) and ISIR confirmed the presence of alpha-hydroxyethane sulfonic acid during the reaction. Heating is stopped and the reactor cooled to room temperature, using a compressed air flow. The reactor was vented and then purged with a slow flow of nitrogen for a few minutes to eliminate any sulfur dioxide in the gas cover. The reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner. The reactor was rinsed with three separate 25 ml portions of water to complete the transfer of solids and rinse the solids in the funnel. The accumulative weight of the filtrate and rinses was obtained. The filtrate was then analyzed by HPLC and the recovery of the materials from the biomass calculated by comparison with the amount of precursors present in the biomass. The solids were dry to a constant weight in air. The results are shown in Table 2.
    [00075] From the substantial absence of conversion of xylan to xylose without the addition of acetaldehyde (since the formation of alpha-hydroxysulfonic acid requires a carbonyl, this represents an absence of
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    36/49 alpha-hydroxysulfonic acid, but all other components are present), which illustrates that alpha-hydroxysulfonic acid is responsible for the hydrolysis activity. The results of comparative example 28 and example 29 are shown in figure 4. Example 28 is shown as a circle in Figure 4.
    Table 2
    Ex. Acid % xylose recovery in filtrate % glucose recovery in filtrate % furfural recovery in filtrate 28 SO2 only - without aldehyde 14.71 0.55 ND 29 alpha hydroxyethane sulfonic acid 71.11 5.03 1.16
    Based on% by weight of xylan in the feed (x grams of xylan produces y grams of theoretical xylose) ** Based on% cellulose and% by weight cellubiosis in the feed *** Based on% by weight of xylan in the feed [00076] It can be seen from the results that the formation of alpha-hydroxyethane-sulfonic acid, with a carbonyl compound is necessary to obtain the excellent recovery of fermentable sugar in the process of the invention. Example 30
    Hydrolysis of biomass with alpha-hydroxyethane-sulfonic acid followed by acid reversion by means of depressurization and distillation of the components.
    [00077] In 20 grams of water degassed with nitrogen, 50 grams of a 40% by weight solution of alpha-hydroxyethane sulfonic acid were added to obtain 100 grams of a solution of 20% alpha-hydroxyethane sulfonic acid. This was gently poured over 12.03 grams of chopped dried bagasse in a 300 ml autoclave equipped with an IR DiComp probe. The reactor was sealed and the mixture stirred for 5 minutes, then it was pressurized to 6.8 bar (gauge) with nitrogen to test the integrity of the pressure. After ventilating the reactor to atmospheric pressure, the unit was closed and heated to 100 ° C in 18 minutes. The mixture of
    Petition 870180073787, of 08/22/2018, p. 45/62
    The reaction was maintained at 100 ° C for 1 hour. The pressure at 100 ° C was 4.3 bar (gauge). Spectral evidence shows the presence of alpha-hydroxyethane sulfonic acid, as well as SO2 and acetaldehyde. Approximately 75 mole% of the charged acid is in the form of acid measured by variable temperature NMR under these conditions, and that the acid level is stable. During the heating period a 75 ml tare Hoke vessel provided with a cold collector is connected to the reactor and cooled with crushed dry ice. At the end of the 1-hour heating period, the valve opening for the gas cover and leading to the cold collector is slowly opened and the pressure in the reactor decreases rapidly. A view of the ISIR spectra in a cascade graph with time is shown in figure 6, which reveals a corresponding drop in SO2 and acetaldehyde in solution. The IR bands for alpha-hydroxyethane-sulfonic acid fall off and are virtually non-existent within 15 minutes of ventilation, which is shown in figure 6. After 20 minutes of ventilation, both the reactor and the cold collector are sealed. The reactor is pressurized with 2.7 bar (gauge) of nitrogen and allowed to cool to room temperature. The reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner. The reactor was rinsed with three separate 25 ml portions of water to complete the transfer of solids and rinse the solids in the funnel. The accumulative weight of the filtrate and rinses was obtained. The filtrate was then analyzed by HPLC and the recovery of the materials from the biomass calculated by comparison with the amount of precursors present in the biomass. These results are shown as example 20 in table 1. The solids are dried to a constant weight in air.
    [00078] The steam collector is allowed to warm up to room temperature and 20.31 grams of material were captured in the collector. IR analysis revealed that the collector contained alpha-hydroxyethane-sulfonic acid, SO2 and acetaldehyde. There was not enough water in the collector for the acid to reform
    Petition 870180073787, of 08/22/2018, p. 46/62
    38/49 completely. This shows the reversible and recyclable nature of the acid, as well as the concurrent acid treatment of biomass. Examples 31-33
    Hydrolysis of biomass with alpha-hydroxyethane-sulfonic acid formed in situ with or without excess SO2.
    [00079] To approximately 84 grams of distilled water cooled in a cabled flask, 7.14 g of acetaldehyde was added, which was mixed to dissolve. The bottle was capped and allowed to warm to room temperature. The bottle was weighed to confirm accurate amounts of acetaldehyde dissolved in the water. Approximately 90 grams of this solution were poured over 12 grams of chopped dry bagasse in a 300 ml autoclave equipped with an IR DiComp probe. The reactor was sealed and pressurized with nitrogen at 6.8 bar (gauge) to guarantee the integrity of the pressure. A single-ended Hoke vessel with a closed ball valve containing the required amount of sulfur dioxide was inverted and connected to the reactor. After the mixture was stirred for ten minutes, the IR spectrum revealed the presence of water and acetaldehyde, but no alpha-hydroxysulfonic acid. Sulfur dioxide is injected into the reactor stirred at 24 ° C in a single portion. This was accompanied by an immediate exotherm and ISIR indicated a rapid formation of alpha-hydroxyethane sulfonic acid. Fourteen minutes after the addition of SO2, there was no observable change in the composition of the reaction mixture by ISIR and the temperature of the mixture had increased to 32 ° C. Heat was then applied to the reactor to raise the temperature to 100 ° C. The reaction was maintained at that temperature for one hour. During the temperature rise and while at the temperature, SO2 and acetaldehyde were observed to be present in the reaction mixture by ISIR, but a substantial part of the alpha-hydroxyethane-sulfonic acid remained. The IR spectra of the reaction mixture also show that the addition of excess SO2 to the reaction mixture
    Petition 870180073787, of 08/22/2018, p. 47/62
    39/49 results in an increased amount of alpha hydroxy sulfonic acid at elevated temperatures. The hydrolysis reaction is allowed to proceed for one hour at 100 ° C and then the acid is reversed when the gas cover is released into the compound collector 70 grams of water in a 250 ml three-necked round-bottom flask, which it is equipped with an acetone condenser with dry ice. The condenser outlet is routed to a caustic collector to prevent the passage of any SO2 into the atmosphere. The water in the bottle is shaken with a stir bar and the bottle is cooled in a wet ice bath. The reactor's ventilation is directed immediately above the ice-cooled water. This slows to a stop and a liquid can be seen condensing from the dry ice condenser, and when this ceases and the pressure in the reactor is <0.2 bar (gauge), the reactor temperature has been raised to 110 ° C and ventilation was continued for an additional 15 minutes. The reactor vent valve is closed and the reactor cooled to room temperature. The collector is allowed to warm up to room temperature. The collector was weighed to obtain the rest of the material on the vaporization and the liquid analyzed by analysis of IR and 13 C, ’H NMR, which is used to calculate the percentage acid recovery used. The cooled reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner to extract the liquid through the funnel. The reactor was rinsed with three separate 25 ml portions of water to complete the transfer of solids and rinse the solids in the funnel. The cumulative weight of the filtrate and rinses was obtained and the filtrate was analyzed by HPLC. The residual solid was dried to a constant weight in air.
    Example 34
    Formation of alpha-hydroxyethane-sulfonic acid from ethanol-acetaldehyde mixture [00080] The reaction in Example 34 was carried out in a similar way to
    Petition 870180073787, of 08/22/2018, p. 48/62
    40/49
    Example 31, except the source of acetaldehyde was a 1: 1 mixture of acetaldehyde and ethanol mixture. This simulates the intermediate current produced by oxidizing ethanol to acetaldehyde. The result is shown in Table 3. Table 3
    Example Acid Acid concentration (% by weight) %xylose recovery in filtrate %glucose recovery in filtrate % furfural recovery in filtrate Agitator speed 31 Alpha-hydroxyethane sulfonic acid (In situ 1: 1 S0 2 : AA) 20 72.78 6.47 0.68 1500 rpm 32 Alpha-hydroxyethane sulfonic acid (In situ 1.15: 1 S0 2 : AA) 20 76.07 7.15 0.75 1500 rpm 33 Alpha-hydroxyethane sulfonic acid (In situ 1: 1 S0 2 : AA) 20 75.90 7.55 0.61 1500 rpm 34 Alpha-hydroxyethane sulfonic acid(EthanoVAA / S02) 20 71.80 6.94 1500 rpm
    * based on% by weight of xylan in the diet (x grams of xylan produces y grams of theoretical xylose) ** based on% by weight of glucan in the diet
    Examples 35-41
    Enzymatic hydrolysis of biomass treated with alpha-hydroxysulfonic acids [00081] The enzyme hydrophobic reactions were re-filled in 10 ml flasks with a conical bottom and thick walls with magnetic stirring. Approximately 0.3 grams of biomass substrate, 7.7 grams of deionized water, 0.5 grams of a pH 5 sodium acetate buffer are added to these flasks. This was adjusted with normal hydrochloric acid 1 to pH approximately 5.0. The vials are placed in a stirring / heating block at 52 ° C configured at 800 rpm. The mixtures were allowed to stir for 30 minutes and then individually removed from the block and 500 µl of GC 220 enzyme obtained from Genencor was added. This was allowed to water for a total of 72 hours, with the aliquots removed for gbcose and sucrose analysis in the time elapsed.
    Petition 870180073787, of 08/22/2018, p. 49/62
    41/49 indicated in hours. This procedure was used to hydrolyze bagasse treated with alpha-hydroxyethane-sulfonic acid and an alpha-hydroxyethane sulfonic acid, examples 16, 17, 18, 19, 20, and 29 in Table 1 and Table 2. The exact amounts of materials used and the results are shown in Table 4. It can be seen that the material treated with alpha-sulfonic hydroxyethane provides improved access to the cellulose contained by the enzymes. As shown in Table 4, in comparison with untreated bagasse, bagasse treated with alpha-hydroxy sulfonic acid allows for substantially complete conversion to gbcose.
    Table 4
    Example 35 36 37 38 39 40 41 Biomass source (Ex. #) 16 17 18 19 20 29 untreated food Sample weight (g) * 0.3025 0.3034 0.3008 0.3050 0.3044 0.3050 0.3028 I gave water. Initial (ml) 7.7733 7.7470 7.7451 7.7700 7.7700 7.8056 7.7674 Acetate solution23.01 g / 250 g total 0.5165 0.5178 0.5204 0.5100 0.5100 0.5161 0.5098 I gave water. Final (ml) 1.0064 1.0106 1.0101 1.0100 1.0100 1.0078 1.0325 Enzyme package (ml) 0.5580 0.5140 0.5105 0.5371 0.5560 0.5518 0.5409 Total 10.1567 10.0928 10.0869 10,1321 10,1504 10.1863 10.1534 Glucose (g / L) 1 h 0.380 0.550 0.710 0.550 2 am 0.510 0.710 0.780 0.705 0.942 0.710 4 am 0.670 0.840 0.940 0.820 24 h 1,500 1,420 1,630 1.43 1.74 1,450 48 h 1,690 1,600 1,710 1.68 1,810 65 h 72 h 1,800 1,610 1,760 1.85 1.84 1,860 0.42 Glucose recovery (%) ** 1 h 2 am 38 52 4 am 24 h 78 95 48 h 91 65 h 72 h 100 101 23
    * moisture content considered for analysis ** Glucan / cellulose-based glucose recovery from abatement Examples 42-45
    Long-term stability tests of alpha-hydroxyethane-sulfonic acid followed by reversion and top-to-top recovery of alpha-hydroxyethane-sulfonic acid.
    [00082] In a 2-liter C276 Parr reactor equipped with a device
    Petition 870180073787, of 08/22/2018, p. 50/62
    42/49 IR optical in situ 1,000 grams of alpha-hydroxyethanesulfonic acid (HESA, 5 approximately 5 or 10% by weight) were prepared by diluting a 40% by weight loading solution of acid with deionized water. Target concentration was confirmed by proton NMR of the starting integration mixture over the peaks for water and acid. The pressure integrity of the reactor system and replacement of air atmosphere were achieved by pressurizing with nitrogen at 7.03 kg / cm 2 manometer (7.03 kg / cm 2 manometer (100 psig)), where the sealed reactor was kept for 15 minutes, without loss of pressure, followed by ventilation at atmospheric pressure, in which the reactor was sealed. The reactor was then heated to 90 to 120 ° C and maintained at a target temperature for four hours. During this time, IR in situ reveals the presence of HESA, SO 2 , and acetaldehyde in an equilibrium mixture. Higher temperature cycles have a shifted balance more towards starting components than lower temperature cycles, indicative of true balance. After four hours, the acid reversion was obtained by opening the reactor gas cover, to a top condensation system, for the recovery of acid and adjusting the reactor temperature to 100 ° C. This top system consisted of a 1 liter jacketed flask equipped with an in situ IR probe based on optical fiber, an acetone condenser with dry ice at the outlet and the gas inlet coming through a steel condenser of 45.72 cm long made from a 0.63 cm diameter pipe core C-276 mounted inside the 1.27 cm stainless steel tube with appropriate connections to obtain downward drainage of the tube wrap condenser in the recovery bottle. The recovery flask was loaded with 400 grams of Dl water and the condenser and jacketed flask cooled with a circulation fluid maintained at 1 ° C. The progress of acid reversion was monitored through the use of IR in situ, both in the Parr reactor and in the
    Petition 870180073787, of 08/22/2018, p. 51/62
    43/49 top condensation. During the reversal of the first component to leave the Parr reactor, SO 2 was followed quickly by a decrease in the bands for HESA. Correspondingly, the bands for SO 2 rise in the recovery bottle and then fall off quickly as HESA was formed from the combination of vaporized acetaldehyde with this component. The reversal was continued until the in situ IR of the Parr reactor showed no trace of an alpha-hydroxyethane-sulfonic acid. The IR of the tops revealed that the concentration of HESA at this point had reached a maximum and then started to decrease, due to the dilution with condensed water, free of components of alpha-hydroxyethane-sulfonic acid, accumulating in the recovery bottle. The reactor was then sealed and cooled to room temperature. The residual liquid in the Parr reactor and the acid recovered at the top were absorbed by means of proton NMR for the concentration of HESA. The results are shown in the table below, indicating acid recovery with virtually no residual HESA in the Parr reactor.
    Example [HESA] Starting% P. Reaction temperature ° C Timeinreversal(min) [HESA] at the top (% P.) Pastaat thetop (g) % of HESA recovered Total mass rest% 42 10.01 90 42 15.15 243.1 96.9 99.4 43 10.07 105 39 14.33 241.4 91.3 99.3 44 5.11 105 40 7.39 255.1 94.7 99.5 45 5.36 120 37 8.42 163.3 88.5 99.4
    Example 46
    Hydrolysis with wheat straw acid with 10% by weight of alpha-hydroxyethane sulfonic acid, at 120 ° C for one hour, followed by reversion and recovery on top of alpha-hydroxyethane sulfonic acid.
    [00083] In a 2-liter C276 Parr reactor equipped with a JR optical device in situ, 120.1 grams of characterized wheat straw composition were added [base in dry state: xylan 22.1% by weight; glucan 38.7% by weight] chopped for nominal 0.5 cm particles. To this were added 999.1 g of alpha-hydroxyethane-sulfonic acid (HESA) at 9.6% by weight prepared by diluting the loading solution to 40% by weight of acid with water
    Petition 870180073787, of 08/22/2018, p. 52/62
    Deionized 44/49. Target acid concentration was confirmed by proton NMR from the integration of the peaks starting mixture into water and acid. The reactor was sealed and the integrity of the pressure in the reactor system and replacement of air atmosphere were achieved by pressurizing with nitrogen at 7.03 kg / cm 2 (100 psig), where the sealed reactor was maintained for 15 minutes, without loss of pressure, followed by ventilation at atmospheric pressure, in which the reactor was sealed. The reactor was then heated to 120 ° C and maintained at the target temperature for one hour. During this time the IR in situ reveals the presence of HESA, SO2, and acetaldehyde in an equilibrium mixture. At the end of the reaction period, the acid reversion was achieved by opening the gas cover of the reactor to a top condensation system for the recovery of the acid and adjusting the reactor temperature to 100 ° C. This top recovery system was the same as that used in Examples 42-45 above. The progress of the acid reversal was monitored through the use of IR in situ, both from the Parr reactor and the top condensation flask. The reversal was continued for a total of 52 minutes until IR in situ from the Parr reactor did not show the remaining traces of alpha-hydroxyethane-sulfonic acid, or SO2 in the reaction mixture. The reactor was then sealed and cooled to room temperature. The top condensate added 182.6 grams of mass to the starting water and gave a 15.0% by weight HESA solution (proton NMR analysis) for a total acid recovery of 91% of the starting HESA employed . The cooled reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner to extract the liquid through a funnel. The reactor was rinsed with three separate portions of water (noting the weight in all rinses, totaling 754 grams), the rinses being used to complete the transfer of solids and rinse the solids in the funnel. The residual solid was dried to a constant weight in air and then analyzed for moisture content, revealing that approximately 40% of the biomass had dissolved during the acid treatment. The analysis
    Petition 870180073787, of 08/22/2018, p. 53/62
    45/49 by HPLC of the 1362 grams of the filtrate plus rinses revealed that a recovery of 87.6% of the starting xylan had been converted to monomeric xylose and 8.2% of the starting cellulose had been converted to glucose. The filtrate and the general tops contained negligible amounts of furfural (0.1 g total). The total material rest of materials recovered for starting materials was 98.2%.
    Example 47
    Hydrolysis with expelled sorghum acid, stored in humid silos, with 10% by weight of alpha-hydroxy-ethane-sulfonic acid at 100 ° C for one hour, followed by reversion and top recovery of sulfonic alpha-hydroxyethane acid.
    [00084] In a Parr reactor of 300 ml C276 equipped with optical device JR in situ, 26.6 grams of uncharacterized sweet sorghum were added, stored in moist silos, with the free moisture having been expelled, the sorghum being peaked in particles of nominally <1 cm (ie 12.45 grams on a dry weight basis). To this was added 100 grams of alpha-hydroxyethane-sulfonic acid (HESA) at 19% by weight prepared by diluting the 40% by weight loading solution of acid with deionized water. Target acid concentration was confirmed by proton NMR of the integration of the starting mixture over the peaks for water and acid. The reactor was sealed and the integrity of the pressure in the reactor system and replacement of air atmosphere were achieved by pressurization with nitrogen at 7.03 kg / cm 2 (100 psig), where the sealed reactor was maintained for 15 minutes, without pressure loss, followed by ventilation at atmospheric pressure, in which the reactor was sealed. The reactor was then heated to 100 ° C and maintained at the target temperature for one hour. During this time, IR in situ reveals the presence of HESA, SO 2 , and acetaldehyde in an equilibrium mixture. An increase in the characteristic bands of glucose and xylose was noted during this time period. At the end of the reaction period, the acid reversal was obtained
    Petition 870180073787, of 08/22/2018, p. 54/62
    46/49 by opening the reactor gas cover to a top condensation system for acid recovery, while maintaining the reactor temperature at 100 ° C. This top recovery system was a 0.63 cm C-267 tube that extends downward into a 250 ml three-necked round-bottomed flask, loaded with 70 grams of Dl water, immersed in a bath wet ice and equipped with a dry ice / acetone condenser at the outlet. The progress of the acid reversal was monitored using IR in situ in the Parr reactor. The reversal was continued until the IR in situ of the Parr reactor did not show the remaining traces of alpha-hydroxyethanesulfonic acid, or SO2 in the reaction mixture. The reactor was then sealed and cooled to room temperature. The top condensate contained 90.45% of the HESA loaded into the system, as absorbed by proton NMR. The cooled reactor was opened and the contents filtered through a sintered glass funnel using a vacuum cleaner to extract the liquid through a funnel. The reactor was rinsed with three separate portions of water, noting the weight in all rinses, the rinses being used to complete the transfer of solids and the rinsing of solids in the funnel. The residual soap was dried at a constant weight in the air and then absorbed for moisture content which reveals that approximately 48% of the biomass had dissolved during the treatment with acid. The HPLC analysis of the filtrate plus the rinses revealed a cumulative recovery of 1.677 grams of monomeric xylose and 1.371 grams of monomeric gbcose. The filtrate and general tops contained insignificant amounts of furfural (0.015 grams total). The total material rest of the materials recovered for starting materials was 96.4%. The relatively high levels of glucose recovered during this hydrophobic were due to the easy starch hydrophobic (approximately 15% by weight) in the HESA starting biomass.
    Example 48
    Comparative example, hot water treatment of expelled sorghum,
    Petition 870180073787, of 08/22/2018, p. 55/62
    47/49 stored in humid silos, at 100 ° C for one hour.
    [00085] In a 300 ml Parr C276 reactor, equipped with an IR optical device in situ, 25.64 grams of uncharacterized sweet sorghum were added, stored in moist silos, with the free moisture having been expelled, the sorghum being peaked in particles nominally <1 cm (ie 12.00 grams on a dry weight basis). This was the same starting material as Example 47. To this was added 100 grams of deionized water. The reactor was sealed and the integrity of the pressure in the reactor system and the replacement of air atmosphere were achieved by pressurizing with nitrogen at 7.03 kg / cm 2 (100 psig), where the sealed reactor was maintained for 15 minutes, without loss of pressure, followed by ventilation at atmospheric pressure, in which the reactor was sealed. The reactor was then heated to 100 ° C and maintained at the target temperature for one hour. At the end of the reaction period, the sealed reactor was cooled to room temperature. The cooled reactor was opened and the contents filtered through a medium sintered glass funnel using a vacuum cleaner to extract the liquid through the funnel. The reactor was rinsed with three separate portions of water, observing the weight in all washes, the rinses being used to complete the transfer of solids and rinse the solids in the funnel. The residual solid was dried to a constant weight in air. HPLC analysis of the filtrate plus rinses revealed a cumulative recovery of 0.011 grams of monomeric xylose and 0.049 grams of monomeric glucose. Furfural was not detected in this cycle. The negligible sugars obtained in the absence of the acid demonstrate the relative effectiveness of alpha-hydroxysulfonic acid in the hydrolysis of sugars.
    Example 49
    Hydrolysis with corn forage acid, with 20% by weight alpha-hydroxyethanesulfonic acid, at 100 ° C, for one hour, followed by reversion and recovery on top of alpha-hydroxyethane sulfonic acid.
    Petition 870180073787, of 08/22/2018, p. 56/62
    48/49 [00086] In a 300 ml Parr C276 reactor, equipped with JR optical device in situ, 12.0 grams of uncharacterized corn forage cut into particles with nominally <1 cm (ie 10.96 grams) were added of biomass on a dry weight basis). To this was added 100 grams of alpha-hydroxyethane-sulfonic acid (HESA) at 20% by weight prepared by diluting the 40% by weight loading solution of the acid with deionized water. Target acid concentration was confirmed by proton NMR of the integration of the starting mixture over the peaks for water and acid. The reactor was sealed and the integrity of the pressure in the reactor system and replacement of air atmosphere were achieved by pressurizing with nitrogen at 7.03 kg / cm 2 (100 psig), where the sealed reactor was maintained for 15 minutes, without loss of pressure, followed by ventilation at atmospheric pressure, in which the reactor was sealed. The reactor was then heated to 100 ° C and maintained at the target temperature for one hour. During this time the IR in situ revealed the presence of HESA, SO 2 , and acetaldehyde in an equilibrium mixture. At the end of the reaction period, the acid reversion was achieved by opening the reactor gas cover to a top condensation system for acid recovery, while maintaining the reactor temperature at 100 ° C. This top recovery system was a 0.63 cm C-267 tube that extends downward into a 250 ml three-necked round-bottomed flask, loaded with 70 grams of Dl water, immersed in a bath wet ice and equipped with a dry ice / acetone condenser at the outlet. The progress of acid reversion was monitored using IR in situ in the Parr reactor. The reversal was continued until the in situ IR of the Parr reactor no longer shows any remaining traces of alpha-hydroxyethane-sulfonic acid, or SO 2 , in the reaction mixture. The reactor was then sealed and cooled to room temperature. The top condensate contained 90.00% of the HESA loaded into the system, as analyzed by proton NMR. The cooled reactor was opened and the contents filtered through a
    Petition 870180073787, of 08/22/2018, p. 57/62
    49/49 sintered glass funnel using a vacuum cleaner to extract the liquid through the funnel. The reactor was rinsed with three separate portions of water, observing the weight in all washes, the rinses being used to complete the transfer of solids and rinse the solids in the funnel. The residual solid was dried to a constant weight in the air and then absorbed for moisture content, revealing that approximately 58.2% of the biomass was recovered. HPLC analysis of the filtrate plus rinses revealed a cumulative recovery of 2.69 grams of monomeric xylose and 0.325 grams of monomeric gbcose. The filtrate and the tops contained 0.023 grams of furfural (total).
    Petition 870180073787, of 08/22/2018, p. 58/62
    1/3
    权利要求:
    Claims (16)
    [1]
    1. Method for treating biomass for the production of sugars from materials containing pobsaccharides, for use in biofuels or other products of high value, characterized by the fact that it comprises:
    (a) providing a biomass containing pobsaccharides;
    (b) contacting the biomass with a solution containing at least one alpha-hydroxysulfonic acid thus hydrobonding the biomass to produce at least one product containing fermentable sugar; and (c) optionally removing the alpha-hydroxysulfonic acid in its component form from the product by heating and / or reducing the pressure to produce a product with the removed acid containing at least one substantially free fermentable sugar of the alpha-hydroxysulfonic acid.
    [2]
    2. Method according to claim 1, characterized by the fact that alpha-hydroxysulfonic acid is present in an amount of 1% by weight to 55% by weight, based on the solution.
    [3]
    Method according to either of claims 1 or 2, characterized in that the alpha-hydroxysulfonic acid is produced from (a) a carbonyl compound or a precursor to a carbonyl compound with (b) sulfur dioxide or a precursor to sulfur dioxide and (c) water.
    [4]
    Method according to any one of claims 1 to
    3, characterized by the fact that alpha-hydroxysulfonic acid is generated in situ.
    [5]
    Method according to any one of claims 1 to
    4, characterized by the fact that step (b) is carried out at a temperature within the range of 50 ° C to 150 ° C and a pressure within the range of 1 bar (gauge) to 10 bar (gauge).
    Petition 870180073787, of 08/22/2018, p. 59/62
    2/3
    [6]
    Method according to any one of claims 1 to 5, characterized in that the fermentable sugar comprises at least one pentose or at least one hexose.
    [7]
    Method according to any one of claims 1 to 5, characterized in that in step (b) at least one pentose and at least one hexose are produced.
    [8]
    Method according to any one of claims 1 to 5, characterized in that it further comprises (d) separating a liquid stream containing said fermentable sugar and a wet solid stream containing the remaining biomass from the product with the acid removed.
    [9]
    Method according to claim 8, characterized in that it further comprises (e) the hydrolysis of the wet solid stream thus producing a sugar stream.
    [10]
    Method according to claim 9, characterized in that it additionally comprises (f) the fermentation of the sugar stream thus producing fermented products.
    [11]
    Method according to any one of claims 1 to 5, characterized in that it additionally comprises hydrolysis and fermentation of the stream containing fermentable sugar, thus producing fermented products.
    [12]
    Method according to any one of claims 1 to 11, characterized in that the alpha-hydroxysulfonic acid removed in step (c) as components is recycled to step (b) as components or in its recombined form.
    [13]
    Method according to any one of claims 1 to 12, characterized in that the biomass is contacted with alpha-hydroxysulfonic acid at a temperature of 120 ° C or less.
    [14]
    14. Method for treating biomass for the production of
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    3/3 sugars from materials containing polysaccharides, for use in biofuels or other high value products, characterized by the fact that it comprises:
    (a) providing a biomass containing polysaccharides;
    (b) contacting the biomass with a solution containing at least one alpha-hydroxysulfonic acid thus hydrolyzing the biomass to produce at least one product containing fermentable sugar;
    (c) heating the product containing fermentable sugar to a temperature of 110 ° C or more, thus producing the stream containing furfural; and (d) removing alpha-hydroxysulfonic acid in its component form from the stream containing furfural, by heating and / or reducing the pressure to produce a product after the acid is removed containing furfural substantially free of alpha-hydroxysulfonic acid; and (e) optionally, recycling the removed alpha-hydroxysulfonic acid as components or in recombinant form for step (b).
    [15]
    15. Composition, characterized by the fact that it comprises biomass containing polysaccharides, at least one alpha-hydroxysulfonic acid and water.
    [16]
    16. Composition according to claim 15, characterized in that it additionally comprises at least one fermentable sugar.
    Petition 870180073787, of 08/22/2018, p. 61/62
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    法律状态:
    2018-02-20| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2018-06-05| B06A| Notification to applicant to reply to the report for non-patentability or inadequacy of the application according art. 36 industrial patent law|
    2018-09-11| B09A| Decision: intention to grant|
    2018-12-04| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 03/11/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US41068910P| true| 2010-11-05|2010-11-05|
    US61/410689|2010-11-05|
    PCT/US2011/059140|WO2012061596A1|2010-11-05|2011-11-03|Treating biomass to produce materials useful for biofuels|
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