FIELD

This disclosure relates to processes for recovery of derivatives of native lignin from lignocellulosic feedstocks, recovered derivatives of native Hgnins, and industrial applications thereof. More particularly, this disclosure relates to processes for recovery of derivatives of native lignin having certain chemical properties as well as uses, processes, methods, and compositions thereof.

BACKGROUND

Native lignin is a naturally occurring amorphous complex cross-linked organic macromolecule that comprises an integral structural component of all plant biomass. The chemical structure of lignin is irregular in the sense that different structural units (e.g., phenylpropane units) are not linked to each other in any systematic order. It is known that native Hgnin comprises pluralities of two monolignol monomers that are methoxylated to various degrees (trans-coniferyl alcohol and trans-sinapyl alcohol) and a third non-methoxylated monolignol (trans-p-coumaryl alcohol). Various combinations of these monolignols comprise three building blocks of phenylpropanoid structures i.e. guaiacyl monolignol, syringyl monolignol and p-hydroxyphenyl monolignol, respectively, that are polymerized via specific linkages to form the native lignin macromolecule.

Extracting native Hgnin from lignocellulosic biomass during pulping generally results in lignin fragmentation into numerous mixtures of irregular components. Furthermore, the lignin fragments may react with any chemicals employed in the pulping process. Consequentiy, the generated Ugnin fractions can be referred to as lignin derivatives and/ or technical Hgnins. As it is difficult to elucidate and characterize such complex mixture of molecules, Hgnin derivatives are usuaUy described in terms of the HgnoceUulosic plant material used, and the methods by which they are generated and recovered from HgnoceUulosic plant material, i.e. hardwood Hgnins, softwood Hgnins, and annual fiber Hgnins.

Native Hgnins are partially depolymerized during chemical pulping processes into Hgnin fragments which are soluble in the pulping Hquors and subsequendy separated from the ceUulosic pulps. Post-pulping Hquors containing Hgnin and polysaccharide fragments, and other extractives, are commonly referred to as "black Hquors" or "spent Hquors", depending on the chemical pulping process. Such liquors are generally considered a by-product, and it is common practice to combust them to recover some energy value in addition to recovering the cooking chemicals. However, it is also possible to precipitate and/ or recover lignin derivatives from these liquors. Each type of chemical pulping process used to separate cellulosic pulps from other lignocellulosic components produces lignin derivatives that are very different in their physico- chemical, biochemical, and structural properties.

Given that lignin derivatives are available from renewable biomass sources there is an interest in using these derivatives in certain industrial processes. For example, lignin derivatives obtained via organosolv extraction, such as the Alcell® process (Alcell is a registered trademark of Lignol Innovations Ltd., Burnaby, BC, CA), have been used in rubber products, friction materials, adhesives, resins, plastics, asphalt, cement, casting resins, agricultural products, and oilfield products. However, large-scale commercial application of the extracted lignin derivatives, particularly those isolated in traditional pulping processes employed in the manufacture of pulp and paper, has been limited due to, for example, the inconsistency of their chemical and functional properties. This inconsistency may, for example, be due to changes in feedstock supplies and the particular extraction/generation/recovery conditions. These issues are further complicated by the complexity of the molecular structures of lignin derivatives produced by the various extraction methods and the difficulty in performing reliable routine analyses of the structural conformity and integrity of recovered lignin derivatives. For instance, lignin derivatives are known to have antioxidant properties (e.g. Catignani G.L., Carter M.E., Antioxidant Properties of Lignin, Journal of Food Science, Volume 47, Issue 5, 1982, p. 1745; Pan X. et al. J. Agric. Food Chem., Vol. 54, No. 16, 2006, pp. 5806-5813) but, to date, these properties have been highly variable making the industrial application of lignin derivatives as an antioxidant problematic.

Thermoplastics and thermosets are used extensively for a wide variety of purposes. Examples of thermoplastics include classes of polyesters, polycarbonates, polylactates, polyvinyls, polystyrenes, polyamides, polyacetates, polyacrylates, polypropylene, and the like. Polyolefins such as polyethylene and polypropylene represent a large market, amounting to more than 100 million metric tons annually worldwide. During manufacturing, processing and use the physical and chemical properties of certain thermoplastics can be adversely affected by various factors such as exposure to heat, UV radiation, light, oxygen, mechanical stress or the presence of impurities. Clearly it is advantageous to mitigate or avoid these problems. In addition, the increase in recycling of material has led to an increased need to address these issues. Degradation caused by free radicals, exposure to UV radiation, heat, light, and environmental pollutants are frequent causes of the adverse effects. A stabilizer such as an antioxidant, anti-ozonant, or UV block is often included in thermoplastic resins for the purpose of aiding in the production process and extending the useful life of the product. Common examples of stabilizers and antioxidants include amine types, phenolic types, phenol alkanes, phosphites, and the like. These additives often have undesirable or even unacceptable environmental, health and safety, economic, and/or disposal issues associated with their use. Furthermore, certain of these stabilizers/antioxidants can reduce the biodegradability of the product.

It has been suggested that lignin may provide a suitable polymeric natural antioxidant which has a low level of toxicity toxicity, efficacy, and environmental profile. See, for example, A. Gregorova et al., Radical scavenging capacity of lignin and its effect on processing stabilization of virgin and recycled polypropylene, Journal of Applied Polymer Science 06-3 (2007) pp. 1626- 1631; C. Pouteau et al. Antioxidant Properties of Lignin in Polypropylene, Polymer Degradation and Stability 81 (2003) 9-18. For a variety of reasons, despite the advantages, lignin has not been adopted for widespread use as an antioxidant. For instance, it is often problematic to provide lignins that perform consistently in terms of antioxidant activity. Also, the processing of the lignin may introduce substances that are incompatible for use with chemicals such as polyolefins. Additionally, the cost of producing and/or purifying the lignin may make it uneconomic for certain uses.

SUMMARY

Some embodiments of the present disclosure relate to derivatives of native lignin having certain aliphatic hydroxyl contents. Surprisingly, it has been found that stable and predictable antioxidant activity is provided by selecting for derivatives of native lignin having certain aliphatic hydroxyl contents. Some embodiments of the present disclosure relate to processes for organosolv pulping of lignocellulosic biomass feedstocks wherein certain operating parameters are selectively manipulated to recover lignin derivatives having certain aliphatic hydroxyl contents.

This summary does not necessarily describe all features of the invention. Other aspects, features and advantages of the invention will be apparent to those of ordinary skill in the art upon review of the following description of specific embodiments of the invention. BRIEF DESCRIPTION OF THE DRAWINGS

The present disclosure will be described in conjunction with reference to the following drawings, in which:

Fig. 1 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from aspen as a function of organic solvent concentration [Ethanol] and pulping temperature [Temperature] at constant pH of 2.47 and pulping time of 68 min;

Fig. 2 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from acacia as a function of pulping time [time] and acidification of the organic solvent [pH] at constant organic solvent concentration of 60.0% (w/w) and pulping temperature of 185.5°C;

Fig. 3 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from eucalyptus as a function of acidification of the organic solvent [pH] and pulping temperature pTemperature] at constant organic solvent concentration of 60.0% (w/ w) and pulping time of 68 min;

Fig. 4 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from hybrid spruce as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 60.5% (w/w) and pulping temperature of 183°C;

Fig. 5 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from radiata pine as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 60.5% (w/w) and pulping temperature of 183°C;

Fig. 6 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from loblolly pine as a function of pulping time [Time] and pulping temperature pTemperature, °C] at constant pH of the pulping liquor of 2.43 and organic solvent concentration of 62% w/w ethanol;

Fig. 7 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from wheat straw as a function of organic solvent concentration [Ethanol] and pulping time [Time] at constant pulping temperature of 185.5°C and organic solvent acidified to a pH of 2.2; Fig. 8 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from bagasse as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 55% (w/w) and pulping temperature of 179°C; and

Fig. 9 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from corn cobs as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 53.5% (w/w) and pulping temperature of 177°C.

DETAILED DESCRIPTION

The present disclosure relates to derivatives of native lignin having certain aliphatic hydroxyl contents, and to organosolv pulping processes tailored for recovery of the lignin derivatives from lignocellulosic biomass feedstocks.

Lignin derivative having lower aliphatic hydroxyl contents have been found to score more highly on the Radical Scavenging Index (RSI), a measure of antioxidant activity. Thus, selecting for derivatives of native lignin having a lower aliphatic hydroxyl content results in a product having a higher and more predictable antioxidant activity. It has been found that derivatives of native lignin having an aliphatic hydroxyl content of about 2.35 mmol/ g or less result in a good level of antioxidant activity. For example, about 2.25 mmol/ g or less, about 2.00 mmol/g or less, or about 1.75 mmol/g or less.

Radical Scavenging Index (RSI) is a measure of radical scavenging capacity. The assay uses 2,2-diphenyl-l-picrylhydrazyl (DPPH), a stable free radical which absorbs light strongly at 515 nm to measure a compound's radical scavenging index (RSI). In its radical form, DPPH* absorbs strongly at 515 nm and has a deep purple colour. As DPPH gives up its free electron to radical scavengers, it loses its purple colour and its absorbance shifts to 520 nm. The greater the drop in DPPH absorbance at 515 nm after a test compound has been added to the DPPH solution, the higher the compound's free RSI and also, its antioxidant activity. In the present disclosure, Vitamin E (Vit. E) and butylated hydroxytoluene (BHT) are used as positive controls. The lignin derivative samples (1.0 - 2.0 mg), Vit. E control samples (1.0-2.0 mg), and BHT control samples (6.0 - 8.0 mg) are prepared for testing by being placed into rnicrocentrifuge tubes after which, each was diluted with 1.0 mL of 90% (v/v) aqueous dioxane, vortexed, transferred to new rnicrocentrifuge tubes and further diluted 50/50 with 90% aqueous dioxane to give stock concentrations of 0.5-1.0 mg/mL for the samples and Vitamin E and 3.0-4.0 mg/mL for BHT. An indicating (purple) DPPH stable free radical solution is made by dissolving 3.78 mg DPPH in 100 mL 90% dioxane (95.9 μΜ). Samples and standards are serially diluted to fill columns of a quartz 96-well plate (8 dilutions). The assays were performed by placing aliquots of the sample stock solutions into two rows of wells in a 96-well plate. The first row served as the reference row while the second row received DPPH aliquots. 165 μΧ, of 90% dioxane was added to each well and mixed. Aliquots of the mixed samples in each row are transferred to the adjacent row which is further diluted with 65 of 90% dioxane in each well. The mixing, transferring and dilution are repeated until the last row of wells is prepared. The same volume of aliquots is removed from the last row. The 96-well plate also contains a row of wells that received only the 90% dioxane. In the final step of the preparation procedure, 165 kL of the DPPH solution is added to all the control and analytical columns by using an 8-channel auto- pipette and an Eppendorf reagent reservoir as quickly as possible. As soon as all reagents are added, the plate is placed into a plate-reading spectrophotometer (Molecular Devices, Sunnyvale, CA, USA, Spectra Max Plus), and absorbance measurements are carried out. The program for the spectrophotometer (SOFTmax software) consists of a timing sequence of 16 min and a reading of the entire plate at 515 nm. RSI is defined as the inverse of the concentration which produces 50% inhibition in DPPH absorbance at 515 nm. The results are then 'normalized' by dividing sample RSI by the RSI value for the BHT control. The normalized RSI is represented by this acronym "NRSI".

The present disclosure provides processes for recovery of derivatives of native lignin during or after organosolv pulping of lignocellulosic feedstocks. The pulp may be from any suitable lignocellulosic feedstock including hardwoods, softwoods, annual fibres, and combinations thereof.

Hardwood feedstocks include Acacia; Afzelia; Synsepalum duloificum; Albizia; Alder (e.g. Alnus glutinosa, Alnus rubra); Applewood; Arbutus; Ash (e.g. F. nigra, F. quadrangulata, F. excelsior, F. pennsylvanica lanceolata, F. latifolia, F. profunda, F. americana); Aspen (e.g. P. grandidentata, P. tremula, P. tremuloides); Australian Red Cedar (Toona ciliatd); Ayna (Distemonanthus benthamianus); Balsa [Ochroma pyramidale); Basswood (e.g. T. americana, T. heterophylla); Beech (e.g. F. sylvatica, F. grandifolid); Birch; (e.g. Betula populifolia, B. nigra, B. papyrifera, B. lenta, B. alkghaniensis/B. lutea, B. pendula, B. pubescens); Blackbean; Blackwood; Bocote; Boxelder; Boxwood; Brazilwood; Bubinga; Buckeye (e.g. Aesculus hippocastanum, Aesculus glabra, Aesculus flava I Aesculus octandra); Butternut; Catalpa; Cherry (e.g. Prunus serotina, Prunus pennsylvanica, Prunus avium); Crabwood; Chestnut; Coachwood; Cocobolo; Corkwood; Cottonwood (e.g. Vopulus balsamifera, Vopulus deltoides, Vopulus sargentii, Vopulus heterophylla); Cucumbertree; Dogwood (e.g. Cornus florida, Cornus nuttallii); Ebony (e.g. Diospyros kur^ii, Diospyros melanida, Diospyros crassiflord); Elm (e.g. Ulmus americana, Ulmus procera, Ulmus thomasii, Ulmus rubra, Ulmus glabra); Eucalyptus; Greenheart; Grenadilla; Gum (e.g. Nyssa sylvatica, Eucaylptus globulus, Uquidambar syt raciflua, Nyssa aquatica); Hickory (e.g. Gary a alba, Carya glabra, Carya ovata, Carya laciniosd); Hornbeam; Hophornbeam; Ipe; Iroko; Ironwood (e.g. Bangkirai, Carpinus caroliniana, Casuarina equisetifolia, Choricbangarpia subargentea, Copaifera spp., Eusideroxylon Guajacum officinale, Guajacum sanctum, Hopea odorata, Ipe, Krugiodendron ferreum, Lyonothamnus y l onii L flonbundus), Mesua ferrea, Olea spp., Olneya tesota, Ostrya virginiana, Varrotia persica, Tabebuia serratifolid); Jacaranda; Jotoba; Lacewood; Laurel; Limba; Lignum vitae; Locust (e.g. Robinia pseudacacia, Gleditsia triacanthos); Mahogany; Maple (e.g. Acer saccharum, Acer nigrum, Acer negundo, Acer rubrum, Acer saccharinum, Acer pseudoplatanus); Meranti; Mpingo; Oak (e.g. Quercus macrocarpa, Quercus alba, Quercus stellata, Quercus bicolor, Quercus virginiana, Quercus michauxii, Quercus prinus, Quercus muhlenbergii, Quercus chrysolepis, Quercus lyrata, Quercus robur, Quercus petraea, Quercus rubra, Quercus velutina, Quercus laurifolia, Quercus falcata, Quercus nigra, Quercus phellos, Quercus texand); Obeche; Okoume; Oregon Myrde; California Bay Laurel; Pear; Poplar (e.g. P. balsamifera, P. nigra, Hybrid Poplar (Vopulus x canadensis)); Ramin; Red cedar; Rosewood; Sal; Sandalwood; Sassafras; Satinwood; Silky Oak; Silver Wattle; Snakewood; Sourwood; Spanish- cedar; American sycamore; Teak; Walnut (e.g. Juglans nigra, Juglans regid); Willow (e.g. Salix nigra, Salix alba); Yellow-poplar (Liriodendron tulipifera); Bamboo; Palmwood; and combinations/hybrids thereof.

For example, hardwood feedstocks for the present disclosure may be selected from Acacia, Aspen, Beech, Eucalyptus, Maple, Birch, Gum, Oak, Poplar, and combinations /hybrids thereof. The hardwood feedstocks for the present disclosure may be selected from Vopulus spp. (e.g. V. grandidentata, V. tremula, V. tremuloides, V. balsamifera, V. deltoides, V. sargentii, V. heterophylla, V. balsamifera, V. nigra, Vopulus canadensis), Eucaylptus spp. (e.g. E. astrigens, e. clivicola, E. dielsii, E. forrestiana, E. gardneri, E. globulus, E. nitans, E. occidentalis, E.ornata, E. salubris, E. spathulata), Acacia spp. (e.g. A. albida, A. cavenia, A. dealbata, A. decutrens, A. famesiana, A. meamsii, A. melanoxylon, A. nilotica, A. penninervis, A. pycnatha, A. saligna, and combinations thereof.

It has been found that derivatives of native lignin from hardwood feedstocks having an aliphatic hydroxyl content of about 2.35 mmol/g or less have a good level of antioxidant activity. For example, about 2.25 mmol/g or less, about 2mmol/g or less, or about 1.75 mmol/g or less. In the present disclosure, "aliphatic hydroxyl content" refers to the quantity of aliphatic hydroxyl groups in the lignin derivative and is the arithmetic sum of the quantity of Primary and Secondary Hydroxyl Groups (al-OH = pr-OH + sec-OH). The aliphatic hydroxyl content can be measured using quantitative ¹³ C high resolution NMR spectroscopy of acetylated lignin (using 1,3,5-trioxane as internal reference).

For the data analysis "BASEOPT" (DIGMOD set to baseopt) routine in TopSpin 2.1.4 was used to predict the first FID data point back at the mid-point of ^!3 C r.f. pulse in the digitally filtered data was used. For the NMR spectra recording a Bruker AVANCE II digital NMR spectrometer running TopSpin 2.1 was used. The spectrometer used a Bruker 54 mm bore Ultrashield magnet operating at 14.1 Tesla (600.13 MHz for Ή, 150.90 MHz for ¹³ C). The spectrometer was coupled with a Bruker QNP cryoprobe (5 mm NMR samples, ¹³ C direct observe on inner coil, 1H outer coil) that had both coils cooled by helium gas to 20K and all preamplifiers cooled to 77K for maximum sensitivity. Sample temperature was maintained at 300 K ±0.1 K using a Bruker BVT 3000 temperature unit and a Bruker BCU05 cooler with ca. 95% nitrogen gas flowing over the sample tube at a rate of 800 L/h.

Derivatives of native lignin according to the present disclosure, coming from hardwood feedstocks tend to have a normalized RSI of 30 or greater, 40 or greater, 50 or greater, 60 or greater, 70 or greater.

Softwood feedstocks include Araucaria (e.g. A. cunninghamii, A. angustifolia, A. araucana); softwood Cedar (e.g. Juniperus virginiana, Thuja plicata, Thuja ocddentalis, Chamaecyparis thyoides Callitropsis nootkatensis); Cypress (e.g. Chamaecyparis, Cupressus Taxodium, Cupressus Taxodium distichum, Chamaecyparis obtusa, Chamaecyparis lawsoniana, Cupressus semperviren); Rocky Mountain Douglas-fir; European Yew; Fir (e.g. Abies balsamea, Abies alba, Abies procera, Abies amabilis); Hemlock (e.g. Tsuga canadensis, Tsuga mertensiana, Tsuga heterophylld); Kauri; Kaya; Larch (e.g. L rix decidua, Larix kaempferi, L rix laricina, Larix occidentalis); Pine (e.g. Pinus nigra, Pinus banksiana, Pinus contorta, Pinus radiata, Pinus ponderosa, Pinus resinosa, Pinus sylvestris, Pinus strobus, Pinus monticola, Pinus lambertiana, Pinus taeda, Pinus palustris, Pinus rigida, Pinus echinatd); Redwood; Rimu; Spruce (e.g. Picea abies, Picea mariana, Picea rubens, Picea sitchensis, Picea glaucd); Sugi; and combinations /hybrids thereof.

For example, softwood feedstocks which may be used herein include cedar; fir; pine; spruce; and combinations thereof. The softwood feedstocks for the present disclosure may be selected from loblolly pine (P. taedd), radiata pine, jack pine, spruce (e.g., white, interior, black), Douglas fir, black spruce, and combinations/hybrids thereof. The softwood feedstocks for the present disclosure may be selected from pine (e.g. Pirns radiata, Pinus taeda); spruce; and combinations/hybrids thereof.

It has been found that derivatives of native lignin from softwood feedstocks having an aliphatic hydroxyl content of about 2.35 mmol/g or less have a good level of antioxidant activity. For example, about 2.25 mmol/g or less, about 2mmol/g or less, or about 1.75 mmol/g or less.

Derivatives of native lignin according to the present disclosure, coming from softwood feedstocks tend to have a normalized RSI of 15 or greater, 25 or greater, 30 or greater, 35 or greater, 40 or greater.

Annual fibre feedstocks include, for example, flax; cereal straw (wheat, barley, oats, rye); bagasse; corn; hemp, fruit pulp, alfa grass, switchgrass, miscanthus, kenaf, and combinations/hybrids thereof. For example, the annual fibre feedstock may be selected from wheat straw, com stover, corn cobs, sugar cane bagasse, and combinations/hybrids thereof.

Derivatives of native lignin according to the present disclosure, coming from annual fibre feedstocks tend to have a normalized RSI of 15 or greater, 20 or greater, 25 or greater, 30 or greater, 35 or greater.

In an embodiment of the present disclosure, derivatives of native lignin from annual fibre feedstocks have an aliphatic hydroxyl content of about 3.75 mmol/g or less; 3.5 mmol/g or less; 3.25 mmol/g or less; 3 mmol/g or less; 2.75 mmol/g or less; 2.5 mmol/g or less; 2.35 mmol/g or less; 2.25 mmol/ g or less.

The derivatives of native lignin will vary with the type of process used to separate native lignins from cellulose and other biomass constituents. Examples of extractive technologies include (1) solvent extraction of finely ground wood; (2) acidic dioxane extraction (acidolysis) of wood; (3) steam explosion; or (4) acid hydrolysis methods. Furthermore, derivatives of native lignin can be recovered after pulping of lignocellulosic biomass including industrially operated kraft and soda pulping (and their modifications) and sulphite pulping. It should be noted that kraft pulping, sulphite pulping, and ASAM organosolv pulping will generate derivatives of native lignin containing significant amounts of organically-bound sulphur which may make them unsuitable for certain uses. Four major "organosolv" pulping methods have been proposed. Organosolv extraction tends to produce highly-purified lignin mixtures. The first organosolv method uses ethanol/ solvent pulping (aka the Alcell ^® process); the second organosolv method uses alkaline sulphite anthraquinone methanol pulping (aka the "ASAM" process); the third organosolv process uses methanol pulping followed by methanol, NaOH, and anthraquinone pulping (aka the "Organocell" process); the fourth organosolv process uses acetic acid/hydrochloric acid pulping (aka the "Acetosolv" process).

Organosolv extraction processes, particularly the Alcell ^® process, tend to be less aggressive and can be used to separate highly purified lignin and other useful materials from biomass without excessively altering or damaging the lignin. Such processes can therefore be used to maximize the value from all the components making up the biomass. Organosolv extraction processes however typically involve extraction at higher temperatures and pressures with a flammable solvent than other industrial methods and thus are generally more complex and expensive.

A description of the Alcell ^® process can be found in US Patent 4,764,596 (herein incorporated by reference). The process generally comprises pulping a fibrous biomass feedstock with primarily an ethanol/water solvent solution under conditions that included: (a) 60% ethanol/40% water, (b) temperature of about 180° C to about 210° C, (c) pressure of about 20 atm to about 35 atm, and (d) a processing time ranging from 30 to 120 minutes. Derivatives of native lignin are fractionated from the native lignins into the pulping liquor which also receives solubilised hemicelluloses, other saccharides and other extractive such as resins, organic acids, phenols, and tannins. Organosolv pulping liquors comprising the fractionated derivatives of native lignin and other extractives from the fibrous biomass feedstocks, are often called "black liquors". The organic acid extractives released by organosolv pulping significantly acidify of the black liquors to pH levels of about 5.5 and lower. After separation from the cellulosic pulps produced during the pulping process, the derivatives of native lignin are recovered from the black liquors by depressurization/ flashing followed by dilution with cold water which will cause the fractionated derivatives of native lignin to precipitate thereby enabling their recovery by standard solids/liquids separation processes. Various disclosures exemplified by US Patent No. 7,465,791 and PCT Patent Application Publication No. WO 2007/129921, describe modifications to the Alcell ^® organosolv process for the purposes of increasing the yields of fractionated derivatives of native lignin recovered from fibrous biomass feedstocks during biorefining. Modifications to the Alcell ^® organosolv process conditions included adjusting: (a) ethanol concentration in the pulping solution to a value selected from a range of 60% - 80% ethanol, (b) temperature to a value selected from a range of 120° C to 350° C, (c) pressure to a value selected from a range of 15 aim to 35 atm, and (d) processing time to a duration from a range of 20 minutes to about 2 hours. Some modifications to the Alcell ^® organosolv process also include the addition of an acid catalyst to the pulping solution to lower its pH to a value from the range of about 1.5-5.5.

The present disclosure provides a process for producing derivatives of native lignin from lignocellulosic biomass feedstocks wherein the lignin derivatives have certain aliphatic hydroxyl contents selected before pulping is commenced, said process comprising:

(a) pulping a fibrous biomass feedstock with an organic solvent/water solvent solution using a combination of the following operating conditions or parameters: (1) a selected organic solvent concentration, (-2) a selected degree of acidification of the organic solvent, (3) a selected temperature at which the pulping is conducted, and (4) a selected time period during which pulping is conducted,

(b) separating the cellulosic pulps from the black liquor produced during pulping, and

(c) recovering derivatives of native lignin from the black liquor.

The organic solvent may be selected from short-chain aliphatic alcohols such as methanol, ethanol, propanol, and combinations thereof. For example, the solvent may be ethanol. The liquor solution may comprise about 20%, by weight, or greater, about 30% or greater, about 50% or greater, about 60% or greater, about 70% or greater, of ethanol.

The pH of the organic solvent may be adjusted to, for example, from about 1 to about 6, or from about 1.5 to about 5.5.

Step (a) of the process may be carried out at a temperature of from about 100°C and greater, or about 120°C and greater, or about 140°C and greater, or about 160°C and greater, or about 170°C and greater, or about 180°C and greater. The process may be carried out at a temperature of from to about 300°C and less, or about 280°C and less, or about 260°C and less, or about 240°C and less, or about 220°C and less, or about 210°C and less, or about 205°C and less, or about 200°C and less.

Step (a) of the process may be carried out at a pressure of about 5 atm and greater, or about 10 atm and greater, or about 15 atm and greater, or about 20 atm and greater, or about 25 atm and greater, or about 30 atm and greater. The process may be carried out at a pressure of about 150 atm and less, or about 125 atm and less, or about 115 atm and less, or about 100 atm and less, or about 90 atm and less, or about 80 atm and less.

The fibrous biomass may be treated with the solvent solution of step (a) for about 1 minute or more, about 5 minutes or more, about 10 minutes or more, about 15 minutes or more, about 30 minutes or more. The fibrous biomass may be treated with the solvent solution of step (a) for about 360 minutes or less, about 300 minutes or less, about 240 minutes or less, about 180 minutes or less, about 120 minutes or less.

The present disclosure provides a process for producing a lignin derivative having an aliphatic hydroxyl content of about 2.35 mmol/g or less, about 2.25 mmol/g or less, about 2mmol/g or less, or about 1.75 mmol/g or less. Said process comprises: a) commingling a fibrous biomass feedstock in a vessel with a selected organic solvent/ water solvent solution having a selectively adjusted pH, wherein: i. the solution comprises about 30% or greater, by weight, of organic solvent; and ii. the pH of the organic solvent is adjusted from about 1 to about 5.5; b) heating the commingled fibrous biomass and pH-adjusted organic solvent to a temperature selected from the range of about 100°C to about 300°C; c) raising the pressure in the vessel to about 10 atm or greater; d) mamtaining the elevated temperature and pressure for a period of time selected from the range of about 1 minute to about 360 minutes while continuously commingling fibrous biomass and pH-adjusted organic solvent thereby producing cellulosic pulps and a black liquor, and; e) separating the cellulosic pulps from the pulp liquor f) recovering derivatives of native lignin. g) Liquor-to-biomass ratios can be varied from 2:1 to 15:1 wt:wt The present disclosure provides a process for producing a hardwood lignin derivative having an aliphatic hydroxyl content of about 2.35 mmol/ g or less, about 2.25 mmol/ g or less, about 2 mmol/g or less, or about 1.75 mmol/g or less, said process comprises: a) pulping a fibrous biomass feedstock in a vessel with a pH-adjusted organic solvent/water solvent solution to form a liquor, wherein: i. the solution comprises a selected concentration of organic solvent of about 30% or greater; and ii. the pH of the organic solvent is selectively adjusted from about 1 to about 5.5; b) heating the liquor to a selected temperature of about 100°C or greater; c) raising the pressure in the vessel to about 10 atm or greater; d) maintaining the elevated temperature and pressure for a selected period of time of 1 minute or longer; e) separating the cellulosic pulps from the pulp liquor f) recovering derivatives of native lignin.

The present disclosure provides a process for producing a softwood lignin derivative having an aliphatic hydroxyl content of about 2.35 mmol/g or less, about 2.25 mmol/g or less, about 2 mmol/g or less, or about 1.75 mmol/g or less, said process comprises: a) corruTiingling a fibrous biomass feedstock in a vessel with a selected organic solvent/water solvent solution having a selectively adjusted pH, wherein: i. the solution comprises about 30% or greater, by weight, of organic solvent; and ii. the pH of the organic solvent is adjusted from about 1 to about 5.5; b) heating the commingled fibrous biomass and pH-adjusted organic solvent to a temperature selected from the range of about 100°C to about 300°C; c) raising the pressure in the vessel to about 10 atm or greater; d) mamtaining the elevated temperature and pressure for a period of time selected from the range of about 1 minute to about 360 minutes while continuously commingling fibrous biomass and pH-adjusted organic solvent thereby producing cellulosic pulps and a black liquor, and; e) separating the cellulosic pulps from the pulp liquor

The present disclosure provides a process for producing an annual fibre lignin derivative having an aliphatic hydroxyl content of about 3.75 mmol/g or less; 3.5 mmol/g or less; 3.25 mmol/g or less; 3 mmol/g or less; 2.75 mmol/g or less; 2.5 mmol/g or less; 2.35 mmol/g or less; 2.25 mmol/g or less, said process comprises: a) commingling a fibrous biomass feedstock in a vessel with a selected organic solvent/water solvent solution having a selectively adjusted pH, wherein: i. the solution comprises about 30% or greater, by weight, of organic solvent; and ii. the pH of the organic solvent is adjusted from about 1 to about 5.5; b) heating the commingled fibrous biomass and pH-adjusted organic solvent to a temperature selected from the range of about 100°C to about 300°C; c) raising the pressure in the vessel to about 10 atm or greater; d) mamtaining the elevated temperature and pressure for a period of time selected from the range of about 1 minute to about 360 minutes while continuously con mingling fibrous biomass and pH-adjusted organic solvent thereby producing cellulosic pulps and a black liquor, and; e) separating the cellulosic pulps from the pulp liquor

The present disclosure relates to methods for determining suitable operating conditions for organosolv pulping of lignocellulosic biomass feedstocks for production of derivatives of native lignin having certain desirable aliphatic hydroxyl contents. Such operating conditions may be determined, for example, by selecting a target operating value for each of at least two process parameters while keeping other process parameters constant. Suitable process parameters that can be manipulated by selection of target operating values include: (a) concentration of organic solvent in the pulping liquor, (b) degree of acidification of the organic solvent prior to commencing pulping, (c) temperature at which pulping is conducted, (d) duration of the pulping period, and (e) liquor- to-biomass ratios among others. Suitable target operating values can be determined by empirically modelling the performance results collected from a series of preliminary otganosolv pulping runs with subsamples of a selected lignocellulosic feedstock wherein at least one process parameter has been adjusted between each of the runs. Exemplary performance results are the aliphatic hydroxyl contents of lignin derivatives recovered from each preliminary organosolv pulping run. A suitable number of preliminary pulping runs is about 10, or about 15, or about 20 about 25 or about 30. The performance results in combination with the manipulated process parameters can be used for equations for identification of suitable target operating values for one or more organosolv processing conditions for lignocellulosic biomass feedstocks from which lignin derivatives have desirable chemical or structural or functional attributes can be recovered. Such equations can be derived from performance results by mathematical tools and software exemplified by Madab ^® Version 7.7.0.471 R2008b (Madab is a registered trademark of The Mathworks Inc., Natick, MA, USA) with a Model-Based Calibration Toolbox Version 3.5 supplied by The Mathworks Inc.

In reference to use of the Matlab software tools for generating the predictive equations for selected organosolv process conditions, suitable model characteristics include:

Model Class: Linear Models

Linear Model Subclass: polynomial

Interaction order: 2

Suitable model terms include:

Constant terms: 1

Linear terms: 4

Second Order Terms: 10

Total Number Terms: 15

Stepwise: Minimize PRESS with 50 maximum iterations Suitable experimental designs include: Experimental Design Type: Sobol Sequence

Number of Points: all available points in Tables 1, 3, and 4

Input factors: 4 (the process parameters Cooking time [Time], cooking temperature [Temperature], cooking pH [pH], solvent concentration [SOLVENT]

The maximum and niinimum values used in each model should be those maximum and minimum values observed in the actual performance data points collected for both the input and output variables ("responses").

This modelling approach can be used to select and manipulate organosolv process conditions to recover lignin derivatives that have certain targeted ranges of chemical and/or structural attributes, for example, one or more of: non-conjugated carbonyl groups/g lignin derivative in the range of about 0.09 to about 1.62 CO-nc mmol/g; conjugated carbonyl groups/g lignin derivative in the range of about 0.31 to about 1.36 CO-conj mmol/g; total carbonyl groups/g lignin derivative in the range of about 0.51 to about 2.72 CO tot mmol/g;

primary hydroxyl groups/g lignin derivative in the range of about 0.48 to about 3.62 pr-OH mmol/g;

secondary hydroxyl groups/g lignin derivative in the range of about 0 to about 3.19 sec-OH sec mmol/ g; aliphatic hydroxyl groups/g lignin derivative in the range of about 0.53 to about 6.62 al-OH mmol/g;

phenolic hydroxyl groups/g of Hgnin derivative in the range of about 2.00 mmol to about 7.12 ph-OH mmol/g;

total hydroxyl groups/g lignin derivative in the range of about 4.73 to about 10.28 tot-OH mmol/g;

0 to about 2.46 mmol/g of aliphatic carboxylic and/ or aliphatic ester groups (COOR al mmol/g); conjugated carboxylic and/ or conjugated ester groups/ g lignin derivative in the range of about 0 to about 2.20 COOR con mmol/g;

carboxylic or ester group/g lignin derivative in the range of about 0 to about 4.46 COOR tot mmol/g; methoxyl groups/g lignin derivative in the range of about 3.61 to about 8.46 O-me mmol/g; ethoxyl or other alkoxy groups/g lignin derivative in the range of about 0.28 to about 1.34 O-et mmol/g; syringyl groups/g lignin derivative in the range of about 0 to about 3.60 S mmol/ g; guaiacyl groups /g Hgnin derivative in the range of about 1.33 to about 7.78 G

S/ G ratio in the range of about 0.41 to about 41.87;

0 to about 1.91 p-hydroxyphenyl units (or H-units)/g Hgnin derivative mmol/g; β-5 structural moitie/g Hgnin derivative in the range of about 0 to about 0.68 mmol/g; β-β structural moitiey/ g Hgnin derivative in the range of about 0 to about 0.46 β-β mmol/g; β-Ο-4 structural moitiey/ g Hgnin derivative in the range of about 0 to about 2.66 β- 0-4 mmol/g;

degree of condensation (DC) in the range of about 0.78 to about 85.0 %; number-average molecular weight (Mn, g/mol) in the range of about 536.50 Daltons to about 1464.00 Daltons;

weight-average molecular weight (Mw, g/mol) in the range of about 965.00 Daltons to about 3366.50 Daltons;

Z average molecular weight (Mz, g/mol) in the range of about 1378.50 Daltons to about 5625.00 Daltons; polydispersity (D) in the range of about 1.46 to about 3.04 (Mw/Mn); carbon content (% dry weight) in the range of about 60.54% to about 72.50%; hydrogen content (% dry weight) in the range of about 4.52% to about 7.24%; and oxygen content (% dry weight) in the range of about 21.90% to about 35.38%;

nitrogen content (% dry weight) in the range of about 0.08% to about 2.82%; sulphur content (% dry weight) in the range of about 0.50% to about 1.25%.

This modelling approach can be used to select and manipulate organosolv process conditions to recover lignin derivatives that have certain targeted ranges of functional attributes, for example, one or more of: radical scavaging index (RSI) in the range of about 5.44 to about 53.36;

glass transition temperature (Tg) in the range of about 51° C to about 127° C; melt flow index ( FI) in the range of about 0 g/10 min to about 878.00 g/10 sec; viscosity (V) of a phenol-formaldehyde resin containing these lignin derivatives at 40% phenol replacement level in the range of about 50 cP to about 20,000 cP; and normalized shear strength as measured by the automated bonding evaluation system (ABES) of a phenol-formaldehyde resin where 40% of the phenol has been replaced by the lignin derivative about 2,034 MPa*cm ² /g to about 3796 MPa*cm ² /g.

The derivatives of native lignin recovered with the processes described herein may be incorporated into polymer compositions. The compositions herein may comprise a lignin derivative according to the present disclosure and a polymer-forming component. As used herein, the term 'polymer-forming component' means a component that is capable of being polymerized into a polymer as well as a polymer that has already been formed. For example, in certain embodiments the polymer-forming component may comprise monomer units which are capable of being polymerized. In certain embodiments the polymer component may comprise oligomer units that are capable of being polymerized. In certain embodiments the polymer component may comprise a polymer that is already substantially polymerized.

Polymers forming components for use herein may result in thermoplastic polymers such as epoxy resins, urea-formaldehyde resins, polyimides and the like, and thermosets such as phenol- formaldehyde resins, and the like. For example, polyalkenes such as polyethylene or polypropylene.

Typically, the lignin derivative will comprise from about 0.1%, by weight, or greater, about 0.5% or greater, about 1% or greater, of the composition. Typically, the lignin derivative will comprise from about 80%, by weight, or less, about 60% or less, about 40% or less, about 20% or less, about 10% or less, about 5% or less, of the composition.

The compositions comprise lignin derivative and polymer-forming component but may comprise a variety of other optional ingredients such as adhesion promoters; biocides (antibacterials, fungicides, and moldicides), anti-fogging agents; anti-static agents; bonding, blowing and foaming agents; dispersants; fillers and extenders; fire and flame retardants and smoke suppressants; impact modifiers; initiators; lubricants; micas; pigments, colorants and dyes; plasticizers; processing aids; release agents; silanes, titanates and zirconates; slip and anti-blocking agents; stabilizers; stearates; ultraviolet light absorbers; foaming agents; defoamers; hardeners; odorants; deodorants; antifouling agents; viscosity regulators; waxes; and combinations thereof

The present disclosure provides the use of the present derivatives of native lignin as an antioxidant. For example, the present use may be as an antioxidant additive for use with thermoplastic polymers such as polyethylene, polypropylene, polyamides, and combinations thereof.

The present disclosure provides methods of producing derivatives of native lignin having an aliphatic hydroxyl content of about 2.35 mmol/g or less, about 2.25 mmol/g or less, about 2 mmol/g or less, or about 1.75 mmol/g or less.

The present disclosure provides methods of producing derivatives of native hardwood Kgnin having an aliphatic hydroxyl content of about 2.35 mmol/g or less result, about 2.25 mmol/g or less, about 2mmol/g or less, or about 1.75 mmol/g or less.

The present disclosure provides methods of producing derivatives of native softwood lignin having an aliphatic hydroxyl content of about 2.35 mmol/g or less, about 2.25 mmol/g or less, about 2mmol/g or less, or about 1.75 mmol/g or less.

The present disclosure provides methods of producing derivatives of native annual fibre lignin having an aliphatic hydroxyl content of about 3.75 mmol/g or less; 3.5 mmol/g or less; 3.25 mmol/g or less; 3 mmol/g or less; 2.75 mmol/g or less; 2.5 mmol/g or less; 2.35 mmol/g or less; 2.25 mmol/g or less.

The present disclosure provides methods of producing derivatives of native lignin having a normalized RSI of 15 or greater, 20 or greater, 25 or greater, 30 or greater, 35 or greater, 40 or greater, 50 or greater, 60 or greater, 70 or greater. The present disclosure provides methods of producing derivatives of native hardwood lignin having a normalized RSI of 15 or greater, 20 or greater, 25 or greater, 30 or greater, 35 or greater, 40 or greater, 50 or greater, 60 or greater, 70 or greater.

The present disclosure provides methods of producing derivatives of native softwood lignin having a normalized RSI of 15 or greater, 20 or greater, 25 or greater, 30 or greater, 35 or greater, 40 or greater.

The present disclosure provides methods of producing derivatives of native annual fibre lignin having a normalized RSI of 15 or greater, 20 or greater, 25 or greater, 30 or greater, 35 or greater.

All citations are herein incorporated by reference, as if each individual publication was specifically and individually indicated to be incorporated by reference herein and as though it were fully set forth herein. Citation of references herein is not to be construed nor considered as an admission that such references are prior art to the present invention.

One or more currently preferred embodiments of the invention have been described by way of example. The invention includes all embodiments, modifications and variations substantially as hereinbefore described and with reference to the examples and figures. It will be apparent to persons skilled in the art that a number of variations and modifications can be made without departing from the scope of the invention as defined in the claims. Examples of such modifications include the substitution of known equivalents for any aspect of the invention in order to achieve the same result in substantially the same way.

The following examples are intended to be exemplary of the invention and are not intended to be limiting.

EXAMPLES

EXAMPLE 1: Recovery of derivatives of native lignin from hardwood feedstocks, softwood feedstocks, and annual fibre feedstocks.

The three hardwood feedstocks chips were prepared from: (1) aspen trees grown in British Columbia, Canada, (2) acacia grown in Chile, and (3) eucalyptus grown in Chile. Subsamples of the three hardwood plant species were individually pulped using an autocatalysed ethanol pulping process organosolv process wherein a different set of pulping conditions was used for each subsample. The individual sets of pulping conditions applied to hardwood species are listed in Tables 1(a)— 1(c). Twenty seven different combinations of pulping conditions were tested with each of BC aspen (Table 1(a)), Chilean Acacia dealbata (Table 1(b)), and Chilean Eucalyptus nitens (Table 1(c)).

For each subsample, the ethanol pulping solvent was prepared as listed in its respective table. First, the ethanol was partially diluted with water after which, a suitable amount of sulphuric acid was added to achieve the target final acidity after which, the ethanol solution was further diluted with water to achieve the target ethanol concentration.

The raw ugnin content of each fibrous biomass subsample was determined using the Klason lignin determination method. Then, after adding the fibrous biomass subsample to a pressure vessel (100-700g odw chips), the tailored ethanol-based pulping solvent was added to the vessel (6:1 liquor:wood ratio), after which it was pressurized and brought up to the target temperature listed in the table. The biomass subsample was then "cooked" for the specified period of time after which, the pulping process was stopped. After pulping, the derivatives of native lignin were recovered by transferring the contents of the pressure vessel to a press. The solids were then squeezed in a press and filtered through a coarse silk screen which separated the chip residues from the fine particles and the liquids. Next, the fine particles were separated from the liquids by filtering the suspension separated from the chip residues, through fine filter paper. The fine particles represent derivatives of native lignin that were extracted and which precipitated from solution after cooling and is herein referred to as self-precipitated derivatives of native lignin designated in the tables as "SPL". Finally, the derivatives of native lignin still remaining in the filtered liquid were precipitated from solution by dilution with cold water. The derivatives of native lignin precipitated by cold-water dilution are referred to herein as precipitated lignin or "PL". After determination of the dry weights of SPL and PL derivatives of native lignin, the relative yield of each lignin derivative was determined in reference to the total lignin value determined for the biomass sample before pulping. The original lignin and carbohydrates content of each fibrous biomass subsample was determined using the methods described in National Renewable Energy Laboratory (NREL) Technical Report entitled 'Determination of Structural Carbohydrates and Lignin in Biomass" - Laboratory Analytical Procedure (TP-510-42618 (25 April 2008)). Ash and extractives content were evaluated according to the standard TAPPI procedures. The yields of SPL and PL derivatives of native lignin for each subsample are expressed on a weight % basis relative to the total lignin value in raw biomass, and listed in Tables l(a)-l(c) for the hardwood feedstocks, Tables 3(a)-3(c) for the softwood feedstocks, and Tables 4(a)-4(c) for the annual fibre feedstocks in columns next to the processing conditions used for each subsamples. Table 2 shows the chemical composition of the raw lignocellulosic biomass samples used in this disclosure. The chip residues remaining after the first filtering step were pressed, dried and weighed. The yield of de-lignified residues, "pulp", (referred to in Tables 1 , 3, 4 as "PBY") is expressed on a % basis relative to the dry weight of the pre-pulping biomass subsample.

Table 1 (a): Organosolv processing conditions for hardwood feedstocks.

BC aspen

Time Temp. Ethanol PL OH-pr OH-sec

Run # pH OH-al

min NRSI

°C % % mmol/g mmol/g mmol/g

1 2.09 65 196 60 82.7 0.48 0.05 0.53 102.63

2 2.03 104 197 68 61.4 0.58 0.00 0.58 94.12

3 2.02 114 195 43 43.6 0.66 0.10 0.76 90.90

4 1.97 89 172 79 62.2 0.78 0.05 0.83 79.83

5 2.17 83 189 64 71.6 0.78 0.11 0.89 81.02

6 1.78 30 170 59 65.8 0.84 0.11 0.95 62.80

7 1.96 42 176 51 68.7 0.87 0.11 0.98 89.63

8 2.12 101 180 48 61.6 0.89 0.16 1.05 71.83

9 2.06 27 193 51 65.7 1.03 0.06 1.09 83.85

10 2.52 90 171 77 53.8 1.15 0.00 1.15 67.17

11 2.18 50 205 45 58.2 0.96 0.27 1.22 74.68

12 1.64 60 167 43 49.7 1.08 0.18 1.27 87.80

13 2.29 115 201 73 60.1 1.00 0.38 1.38 67.68

14 2.00 33 181 44 55.9 1.13 0.30 1.43 85.54

15 2.22 94 177 47 58.3 1.41 0.35 1.76 57.41

16 2.34 44 174 68 51.3 1.24 0.54 1.78 56.63

17 2.30 87 183 54 63.8 1.32 0.52 1.84 64.00

18 2.29 46 169 73 52.4 1.54 0.43 1.97 60.54

19 2.26 63 190 47 46.8 1.39 0.75 2.13 60.51

20 2.10 21 166 46 38.5 1.44 0.78 2.21 61.98

21 2.70 82 191 41 49.5 1.41 0.97 2.38 62.85

22 2.81 113 180 67 48.2 1.94 1.34 3.28 44.02

23 3.30 107 170 61 35.5 2.00 2.00 3.99 27.27

24 3.27 100 166 65 27.6 2.16 1.95 4.11 34.71

25 2.94 56 176 60 42.0 2.21 2.04 4.25 36.85

26 1.87 67 194 58 106.0 0.60 0.05 4.37 97.39

27 1.68 79 173 49 62.1 0.79 0.11 4.46 84.41 Table 1 (b): Chilean Acacia dealbata

Acid Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # PH RSI

% min °C % % mmol/g mmol/g mmol/g

1 2.01 1.61 104 197 68 67.88 0.76 0.00 0.76 121.76

2 2.11 1.00 114 195 43 46.56 1.24 0.00 1.24 130.15

3 2.20 1.28 65 196 60 65.67 0.69 0.75 1.44 93.15

4 2.00 1.51 67 194 58 66.21 1.08 0.38 1.46 94.90

5 1.90 2.47 42 176 51 63.39 1.25 0.30 1.55 86.39

6 2.03 1.31 89 172 79 47.77 0.91 0.73 1.64 90.37

7 1.96 1.40 33 181 44 51.05 1.32 0.75 2.07 75.59

8 2.35 0.60 50 205 45 51.25 1.48 0.83 2.31 80.44

9 2.22 0.90 83 189 64 54.92 1.20 1.33 2.53 85.22

10 2.16 1.01 27 193 51 54.00 1.44 1.11 2.54 72.39

11 2.40 0.81 90 171 77 36.50 1.82 0.79 2.60 71.61

12 2.04 1.60 79 173 49 61.53 1.20 1.58 2.78 63.46

13 1.79 2.41 30 170 59 59.10 1.29 1.53 2.82 74.95

14 1.82 2.20 60 167 43 53.70 1.45 1.57 3.02 68.76

15 2.58 0.51 115 201 73 49.61 2.03 1.33 3.36 92.49

16 2.27 0.81 101 180 48 56.26 1.77 2.01 3.78 57.24

17 2.44 0.61 94 177 47 50.46 2.24 1.64 3.88 82.07

18 2.34 0.90 46 169 73 38.40 1.85 2.08 3.93 54.83

19 2.42 0.61 87 183 54 54.44 2.34 1.65 3.99 73.34

20 2.38 0.70 44 174 68 35.32 2.59 1.45 4.04 69.02

21 2.75 0.20 82 191 41 38.49 2.42 1.76 4.18 59.07

22 2.18 1.09 21 166 46 42.54 2.43 1.78 4.21 61.29

23 2.40 0.51 63 190 47 50.98 2.38 1.88 4.26 61.15

24 3.19 0.11 100 166 65 14.07 3.21 2.45 5.66 54.54

25 2.80 0.30 113 180 67 36.52 3.13 2.55 5.68 49.80

26 2.93 0.20 56 176 60 27.88 2.98 2.98 5.95 47.02

27 3.20 0.10 107 170 61 25.97 3.43 3.19 6.62 57.85 Table 1 (c): Chilean Eucaylptus nitens

Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # pH N SI min °C % % mmol/g mmol/g mmol/g

1 1.88 104 197 68 81.7 0.57 0.13 0.70 109.66

2 1.96 67 194 58 77.4 0.58 0.19 0.78 108.27

3 2.01 65 196 60 81.8 0.62 0.25 0.86 119.66

4 1.93 114 195 43 43.9 0.88 0.20 1.08 112.88

5 2.53 115 201 73 61.8 0.72 0.50 1.22 101.95

6 2.10 83 189 64 69.4 0.76 0.69 1.46 91.17

7 2.05 89 172 79 53.0 0.91 0.56 1.47 92.24

8 1.87 79 173 49 63.6 0.88 0.61 1.49 67.29

9 2.17 27 193 51 66.8 0.86 0.73 1.60 87.59

10 2.17 101 180 48 63.4 0.91 0.70 1.61 85.93

11 2.25 90 171 77 48.9 1.01 0.68 1.69 94.66

12 1.90 33 181 44 59.5 1.09 0.61 1.70 87.78

13 1.74 42 176 51 66.9 1.17 0.55 1.73 81.93

14 1.77 30 170 59 61.6 1.11 0.72 1.83 77.44

15 1.65 60 167 43 57.3 1.13 0.71 1.84 83.29

16 2.26 46 169 73 48.5 1.07 1.19 2.27 75.61

17 2.30 87 183 54 65.6 1.20 1.07 2.27 75.59

18 2.30 44 174 68 49.0 1.37 1.18 2.55 69.83

19 2.30 50 205 45 66.7 1.87 0.73 2.60 83.34

20 2.34 63 190 47 61.9 2.07 0.55 2.63 78.71

21 2.66 82 191 41 43.4 1.58 1.23 2.81 68.29

22 2.49 113 180 67 55.1 2.04 1.22 3.26 60.61

23 2.00 21 166 46 50.5 1.47 1.96 3.43 69.66

24 2.33 94 177 47 63.3 1.20 2.41 3.61 75.05

25 2.82 56 176 60 42.7 2.74 2.02 4.76 45.98

26 3.22 107 170 61 43.6 2.70 2.70 5.40 55.27

27 3.13 100 166 65 25.6 3.07 2.45 5.52 36.93 Table 2: Chemical composition of lignocellulosic biomass samples (% dry weight)

Biomass Arabinan Galactan Glucan Xylan Mannan Lignin Ash Extractives

Sample

Alberta 2.39 0.67 41.10 22.41 0 20.94 4.96 1.40

Wheat Straw

Chilean 0.55 0.64 44.65 19.78 1.35 22.85 0.54 1.63

Acacia dealbata

Brazilian 1.87 0.51 38.15 21.79 0.21 24.10 5.39 1.36

Sugarcane

Bagasse

British 1.00 2.00 43.75 4.97 11.70 22.85 1.00 0.86

Columbia

Hybrid

Spruce (Picea

engelmannii x

Picea glaucd)

Chilean Pinus 1.52 2.73 46.04 6.12 11.36 24.15 0.67 0.37 radiata

European 3.07 1.02 35.79 30.85 0 18.41 1.43 1.63

Corn Cobs

Southeastern 1.40 2.61 41.64 6.87 10.10 30.84 0.54 2.06

US Pinus taeda

British 0.44 0.43 48.76 16.44 1.48 22.84 0.25 2.63

Columbia

Aspen

Populus

tremuloides)

Chilean 0.96 0.61 47.70 17.52 1.12 27.57 0.01 0.99

Eucalyptus

nitens Characterization of the aliphatic hydroxyl content of derivatives of native lignin recovered from three species of hardwoods.

Derivatives of native lignin recovered from hardwood feedstocks were analyzed to determine mmol of primary hydroxyl groups/g sample (OH-pr mmol/g) and mmol of secondary hydroxyl groups/g sample (OH-sec mmol/g). These data were then used to calculate mmol aliphatic hydroxyl groups/g sample (OH-al mmol/g).

The hydroxyl contents were determined by analyses of NMR spectra recorded on a Bruker 700 MHz spectrometer equipped with Cryoprobe at 300 K using ca 30% solutions of sample in DMSO-^- Chemical shifts were referenced to TMS (0.0 ppm). To ensure more accurate baseline, especially in the carbonyl region (215-185 ppm), the spectra were recorded over the interval 240-(-40) ppm. The following conditions were provided for the quantitative ^,3 C-NMR:

1. Inverse gate detection;

2. a 90 ^° pulse;

3. Complete relaxation of all nuclei was achieved by addition of chromium (III) acetylacetonate (0.01 M) with a 1.2 s acquisition time and 1.7 s relaxation delay.

The NMR spectra were Fourier-transformed, phased, calibrated using TMS signals as a reference (0 ppm), and the baseline was corrected by using a polynomial function. The correction of baseline was done using the following interval references for adjustment to zero: (220-215ppm)-(l 85-182ppm)-(97-92ppm)-(5-(-20)ppm). No other regions were forced to 0. The signals in the quantitative ¹³ C NMR spectra were assigned on the base of 2D HSQC NMR and a known database. After the baseline correction the spectra were integrated using the area of internal standard (IS), trioxane, as the reference. Each spectrum was processed (as described) at least twice to ensure good reproducibility of the quantification. The calculation of the quantity of specific moieties was done as follows:

For non-acetylated lignins: X (mmol/g lignin) = I _x *m _IS / (30m _Lig *I _IS )*1000

For acetylated lignins: X (mmol/g lignin) = I _x *m _IS /(30m _Lig *I _ls - 42*I _OHtotal * m _IS )*1000

Where X was the amount of the specific moiety; I _x I _IS and Ι _ΟΗΚ)Β _ ^were the resonance values of the specific moiety (Table 3), the internal standard and total OH groups, correspondingly; m _Lig and m _IS are the masses of the lignin and internal standard. Table 3:

Symbol Calculation Equation Analytical Method

Resonance at 171.5-169.7 ppm in the

quantitative ¹³ C NMR spectra of acetylated Quantitative ¹³ C High Resolution NMR of

OH-pr

lignins minus resonance at 171.5-169.7 acetylated lignin using ,3,5-trioxane as internal mmol/ g

ppm in the quantitative 13C NMR spectra reference

of non-acetylated lignins

Resonance at 169.7-169.2 ppm in the

quantitative ¹³ C NMR spectra of acetylated Quantitative ¹³ C High Resolution NMR of

OH-sec

lignins minus resonance at 169.7-169.2 acetylated lignin using 1,3,5-trioxane as internal mmol/ g

ppm in the quantitative 13C NMR spectra reference

of non-acetylated lignins

OH-al

OH-al = OH-pr + OH-sec

mmol/g

The aliphatic hydroxyl content of the PL Ugnin derivatives from each of the twenty seven samples of aspen chips are shown in Table 1(a). The contents ranged from 0.70 mmol/g in run 1 to 5.52 mmol/g in run 27.

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty seven samples of acacia chips are shown in Table 1(b). The contents ranged from 0.76 mmol/g in run 1 to 6.62 mmol/g in run 27.

The aliphatic hydroxyl contents of the PL Ugnin derivatives from each of the twenty seven samples of eucalyptus chips are shown in Table 1(c). The contents ranged from 0.70 mmol/g in run 1 to 5.52 mmol/g in run 27.

Characterization of the NRSI of derivatives of native lignin recovered from three species of hardwoods.

Each of the lignin derivative subsamples produced above was assessed for its radical scavenging index (RSI). The potential antioxidant activity of each PL lignin derivative was determined by measuring its radical savaging capacity. The assay used 2,2-diphenyl-l- picrylhydrazyl (DPPH), a stabile free radical which absorbs light strongly at 515 nm to measure a compound's radical scavenging index (RSI). In its radical form, DPPH* absorbs strongly at 515 nm and has a deep purple colour. As DPPH gives up its free electron to radical scavengers, it loses its purple colour and its absorbance shifts to 520 nm. The greater the drop in DPPH absorbance at 515 nm after a test compound has been added to the DPPH solution, the higher the compound's free RSI and also, its antioxidant activity. In the present study, Vit. E and BHT were used as positive controls. PL lignin derivative subsamples (1.0 - 2.0 mg), Vit. E control samples (1.0 - 2.0 mg), and BHT control samples (6.0 - 8.0 mg) were prepared for testing by being placed into epitubes after which, each was diluted with 1.0 mL of 90% (v/v) aqueous dioxane, vortexed, transferred to new epitubes and then further diluted 50/50 with 90% aqueous dioxane to give stock concentrations of 0.5-1.0 mg/mL for samples and Vitamin E and 3.0-4.0 mg/ mL for BHT. An indicating (purple) DPPH stable free radical solution is made by dissolving 3.78 mg DPPH in 100 mL 90% dioxane (95.9 μΜ). Samples and standards are serial diluted to fill columns of a quartz 96-well plate (8 dilutions). The assays were performed by placing aliquots of the sample stock solutions into two rows of wells in a 96-well plate. The first row served as the reference row while the second row received DPPH aliquots. 165 of 90% dioxane was added to each well and mixed. Aliquots of the mixed samples in each row are transferred to the adjacent row with is further diluted with 165 L of 90% dioxane in each well. The mixing, transferring and dilution are repeated until the last row of wells was prepared. The same volume of aliquots was removed from the last row. The 96-well plate also contains a row of wells that received only the 90% dioxane. In the final step of the preparation procedure, 165 μί of the DPPH solution is added to all the control and analytical columns by using an 8-channel auto- pipette and an Eppendorf ^® reagent reservoir as quickly as possible. As soon as all reagents were added, the plate was placed into a plate-reading spectrophotometer, and absorbance measurements were performed. The program for the spectrophotometer (SOFTmax software) consists of a timing sequence of 16 rnin and a reading of the entire plate at 515 nm. RSI (radical scavenging index) is defined as the inverse of the concentration which produces 50% inhibition in DPPH absorbance at 515 nm. The results are then 'normalized' by dividing sample RSI by the RSI value for the BHT control.

The NRSI values for lignin derivatives recovered from BC aspen are shown in Table 1(a). The NRSI values for lignin derivatives recovered from Chilean acacia biomass are shown in Table 1(b). The NRSI values for lignin derivatives recovered from Chilean eucalyptus biomass are shown in Table 1(c).

EXAMPLE 2: Recovery of derivatives of native Iignin from softwood feedstocks.

Three softwood feedstocks chips were prepared from: (1) hybrid spruce (Picea engelmannii x Picea glauca) trees grown in British Columbia, (1) radiata pine grown in Chile, and (2) loblolly pine (Pinus taedd) grown in the southeast USA. Subsamples of the three plant species were individually pulped using an autocatalysed ethanol pulping process wherein a different set of pulping conditions was used for each subsample.

The individual sets of pulping conditions applied to softwood species are listed in Tables 3(a)-3(c). Twenty nine different combinations of pulping conditions were tested with each of BC hybrid spruce (Table 3(a)) and Chilean radiata pine (Table 3(b)), while 30 combinations of pulping combinations were tested with southeastern US loblolly pine (Table 3(c)).

For each subsample, the ethanol pulping solvent was prepared as listed in its respective table. First, the ethanol was partially diluted with water after which, a suitable amount of sulphuric acid was added to achieve the target final acidity after which, the ethanol solution was further diluted with water to achieve the target ethanol concentration.

The raw Hgnin content of each fibrous biomass subsample was determined using the methods described in National Renewable Energy Laboratory (NREL) Technical Report entitled "Determination of Structural Carbohydrates and Lignin in Biomass" - Laboratory Analytical Procedure (TP-510-42618 (25 April 2008)). Then, after adding the fibrous biomass subsample to a pressure vessel (100-700 g odw chips), the tailored ethanol-based pulping solvent was added to the vessel (6:1 liquor:wood ratio) after which it was brought up to the target temperature and pressure listed in the table. The biomass subsample was then "cooked" for the specified period of time, after which, the pulping process was stopped. After pulping, the derivatives of native lignin were recovered by transferring the contents of pressure vessel to a press. The solids were then squeezed in a press and filtered through a coarse silk screen which separated the chip residues from the fine particles and the liquids. Next, the fine particles were separated from the liquids by filtering the suspension separated from the chip residues, through fine filter paper. The fine particles represent derivatives of native lignin that were extracted and which precipitated from solution after cooling and is herein referred to as self-precipitated derivatives of native lignin designated in the tables as "SPL". Finally, the derivatives of native Hgnin still remaining in the filtered liquid were precipitated from solution by dilution with cold water. The derivatives of native lignin precipitated by cold-water dilution are referred to herein as precipitated lignin or "PL". After determination of the dry weights of SPL and PL derivatives of native lignin, the relative yield of each lignin derivative was determined in reference to the total lignin value determined for the biomass sample before pulping. The yields of SPL and PL derivatives of native lignin for each subsample are expressed on a weight % basis relative to its total lignin value, and listed in Tables 4(a) -4(c) for the softwood feedstocks in columns next to the processing conditions used for each subsamples. The chip residues remaining after the first filtering step were pressed, dried and weighed. The yield of de-lignified residues, "pulp" referred to in Tables 4(a)-4(c) as "PBY", are expressed on a % yield basis relative to the dry weight of the pre-pulping biomass subsample.

Characterization of the aliphatic hydroxyl content of derivatives of native lignin recovered from three species of softwoods.

Derivatives of native lignin recovered from softwood feedstocks were analyzed as discussed above to determine mmol primary hydroxyl groups/g sample (OH-pr mmol/g) and mmol secondary hydroxyl groups/g sample (OH-sec mmol/g). These data were then used to calculate mmol aliphatic hydroxyl groups/g sample (OH-al mmol/g).

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty nine samples of spruce woodchips are shown in Table 4(a). The contents ranged from 1.72 mmol/g in run 1 to 4.75 mmol/g in run 29.

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty nine samples of radiata pine woodchips are shown in Table 4(b). The contents ranged from 2.18 mmol/g in run 1 to 5.09 mmol/g in run 29.

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the thirty samples of loblolly pine chips are shown in Table 4(c). The contents ranged from 1.35 mmol/g in run 1 to 4.39 mmol/g in run 30. Table 4(a): Organosolv processing conditions for softwood feedstocks.

BC hybrid spruce

Acid Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # PH NRSI

% min °C % % mmol/g mmol/g mmol/g

1 2.02 1.20 58 191 46 44.84 1.57 0.14 1.72 61.61

2 1.96 1.80 46 187 49 43.57 1.47 0.32 1.79 58.80

3 2.08 1.40 43 189 61 67.77 1.67 0.29 1.96 46.83

4 2.09 1.60 50 183 77 72.10 1.74 0.28 2.02 40.66

5 1.80 2.60 32 182 50 44.49 1.82 0.42 2.24 35.37

6 2.26 1.10 54 185 76 75.89 1.94 0.55 2.49 31.90

7 1.95 1.90 33 179 57 63.89 2.05 0.55 2.60 27.44

8 2.18 0.90 55 184 47 40.42 2.19 0.48 2.66 28.15

9 1.81 2.50 36 175 78 71.84 2.18 0.56 2.75 26.22

10 2.49 0.35 79 198 42 26.78 2.23 0.58 2.81 22.29

11 1.72 2.90 34 168 43 40.04 2.44 0.49 2.93 23.98

12 2.16 0.98 38 178 44 26.24 2.51 0.43 2.94 22.22

13 2.12 1.20 41 181 68 70.59 2.35 0.69 3.04 30.63

14 2.14 1.30 46 175 68 66.06 2.44 0.61 3.05 23.39

15 2.11 1.30 34 172 79 56.41 1.94 1.20 3.14 15.76

16 1.82 2.10 39 170 46 33.37 2.61 0.58 3.19 17.63

17 2.69 0.23 110 191 44 30.37 2.39 0.91 3.30 24.17

18 2.52 0.47 57 194 61 59.02 2.88 0.60 3.48 21.88

19 2.08 1.00 59 171 42 24.55 2.94 0.59 3.53 18.93

20 2.65 0.38 73 189 54 52.60 2.89 0.67 3.55 18.78

21 2.60 0.31 84 184 76 36.43 2.95 0.69 3.64 16.71

22 1.89 2.10 31 167 52 44.49 2.18 1.58 3.76 15.88

23 2.37 0.52 77 178 46 35.16 2.24 1.56 3.79 14.90

24 2.43 0.43 49 179 45 28.34 3.07 0.84 3.91 13.98

25 2.66 0.36 61 188 67 54.42 3.23 0.70 3.93 18.54

26 2.42 0.64 51 176 65 64.03 2.38 1.66 4.04 15.15

27 3.15 0.13 53 199 73 24.55 2.85 1.19 4.04 16.90

28 3.02 0.12 86 186 47 30.28 3.14 1.39 4.53 22.32

29 2.88 0.17 60 182 62 29.21 3.34 1.40 4.75 13.27 Table 3 (b): Chilean radiata pine

Acid Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # PH NRSI

% min °C % % mmol/g mmol/g mmol/g

1 2.04 1.20 58 191 46 34.21 1.74 0.44 2.18 64.24

2 2.06 1.60 50 183 77 65.00 1.77 0.42 2.19 36.10

3 1.72 2.60 32 182 50 46.46 1.79 0.41 2.20 42.49

4 2.12 1.40 43 189 61 65.40 1.79 0.43 2.22 35.27

5 1.86 2.50 36 175 78 59.66 1.87 0.36 2.23 33.71

6 1.92 1.80 46 187 49 42.72 1.90 0.35 2.26 37.44

7 1.92 1.90 33 179 57 48.76 2.31 0.49 2.80 36.98

8 2.28 1.10 54 185 76 79.49 2.17 0.72 2.90 49.41

9 2.50 0.35 79 198 42 31.87 2.36 0.71 3.07 35.93

10 1.73 2.90 34 168 43 29.72 2.45 0.65 3.10 22.44

11 2.08 0.98 38 178 44 28.17 2.65 0.63 3.27 20.83

12 2.23 0.90 55 184 47 38.00 2.62 0.69 3.31 28.27

13 2.12 1.30 46 175 68 82.49 2.87 0.72 3.59 23.29

14 2.15 1.20 41 181 68 60.93 2.75 0.85 3.60 30.02

15 2.50 0.47 57 194 61 48.55 2.94 0.72 3.66 27.20

16 1.80 2.10 39 170 46 31.81 3.01 0.70 3.71 18.71

17 2.06 1.00 59 171 42 22.85 3.00 0.71 3.72 20.93

18 2.70 0.31 84 184 76 33.09 3.02 0.72 3.73 20.78

19 2.38 0.52 77 178 46 29.70 3.05 0.71 3.77 18.00

20 2.63 0.23 110 191 44 27.01 2.72 1.06 3.78 29.76

21 2.52 0.38 73 189 54 31.35 3.18 0.72 3.90 16.80

22 1.79 2.10 31 167 52 37.58 3.25 0.68 3.92 16.15

23 2.73 0.36 61 188 67 46.40 3.23 0.72 3.95 13.90

24 2.04 1.30 34 172 79 50.87 3.32 0.70 4.02 17.61

25 2.30 0.64 51 176 65 57.35 3.62 0.72 4.35 14.63

26 3.08 0.13 53 199 73 22.04 3.12 1.35 4.47 18.15

27 2.50 0.43 49 179 45 25.33 3.09 1.54 4.63 14.24

28 2.95 0.12 86 186 47 28.54 3.23 1.54 4.77 19.76

29 3.01 0.17 60 182 62 22.12 3.55 1.53 5.09 13.68 Table 3 (c): Southeastern US loblolly pine

Acid Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # pH NRSI

% min °C % % mmol/g mmol/g mmol/g

1 2.05 1.20 33 192 82 65.1 1.16 0.19 1.35 48.73

2 2.12 1.20 58 191 46 36.9 1.42 0.03 1.42 55.39

3 2.00 1.60 50 183 77 69.1 1.42 0.03 1.43 44.54

4 2.01 1.40 43 189 61 63.3 1.55 0.03 1.58 46.95

5 1.65 2.60 32 182 50 41.6 1.74 0.00 1.74 47.49

6 2.13 1.10 54 185 76 69.9 1.29 0.58 1.87 31.66

7 1.80 1.80 46 187 49 42.3 1.74 0.13 1.87 53.44

8 2.02 1.20 41 181 68 58.0 1.68 0.26 1.94 32.17

9 1.90 2.50 36 175 78 66.8 1.68 0.26 1.94 32.73

10 2.33 0.90 55 184 47 36.0 1.87 0.26 2.13 34.41

11 2.07 1.70 43 176 81 62.1 1.94 0.39 2.32 31.29

12 1.90 1.90 33 179 57 53.1 2.06 0.45 2.52 24.37

13 1.83 2.10 39 170 46 29.8 2.19 0.45 2.65 27.78

14 2.10 1.30 34 172 79 50.2 2.32 0.45 2.77 20.05

15 1.80 2.90 34 168 43 25.3 2.26 0.52 2.77 33.44

16 2.17 1.30 46 175 68 58.9 2.26 0.58 2.84 27.85

17 2.52 0.35 79 198 42 16.4 2.19 0.71 2.90 27.95

18 2.58 0.64 51 176 65 48.7 2.13 0.77 2.90 13.78

19 2.15 1.00 59 171 42 20.5 2.32 0.58 2.90 23.61

20 2.25 0.98 38 178 44 38.5 2.45 0.52 2.97 23.34

21 1.87 2.10 31 167 52 39.0 2.58 0.52 3.10 19.27

22 2.65 0.31 84 184 76 34.1 2.52 0.65 3.16 19.24

23 2.47 0.47 57 194 61 46.9 2.39 0.77 3.16 26.27

24 2.92 0.17 60 182 62 38.5 2.65 0.65 3.29 15.93

25 2.50 0.38 73 189 54 39.3 2.58 0.84 3.42 27.78

26 2.39 0.43 49 179 45 30.7 2.65 0.84 3.48 18.02

27 2.77 0.23 110 191 44 12.5 2.52 1.03 3.55 22.80

28 3.20 0.13 53 199 73 23.3 2.65 1.16 3.81 24.56

29 2.80 0.36 61 188 67 24.8 2.97 1.29 4.26 17.00

30 2.99 0.12 86 186 47 27.9 2.97 1.42 4.39 18.12 Chat ctetization of the NRSI of derivatives of native lignin tecovered from thtee species of softwoods.

Each of the lignin derivative subsamples produced above were assessed for its radical scavenging index (RSI). The potential antioxidant activity of each PL lignin derivative was determined as described above. The NRSI values for lignin derivatives recovered from hybrid spruce biomass are shown in Table 4(a). The NRSI values for lignin derivatives recovered from radiate pine biomass are shown in Table 4(b). The NRSI values for lignin derivatives recovered from loblolly pine biomass are shown in Table 4(c).

EXAMPLE 3: Recovery of derivatives of native lignin from three annual fibre feedstocks.

Three annual fibre feedstocks were prepared from : (1) wheat straw from Alberta Canada, (2) sugarcane bagasse from Brazil, and (3) corn cobs from crops produced in Europe. Subsamples of the three plant species were individually pulped using an autocatalysed ethanol pulping process based on the Alcell ^® organosolv process wherein a different set of pulping conditions was used for each subsample.

The individual sets of pulping conditions applied to annual fiber feedstocks are listed in Tables 5(a)— 5(c). Twenty seven different combinations of pulping conditions were tested with each of Alberta wheat straw (Table 5(a)) and European corn cobs (Table 5(c)), and twenty six combinations were tested with Brazilian sugarcane bagasse (Table 5(b)).

For each subsample, the ethanol pulping solvent was prepared as listed in its respective table. First, the ethanol was partially diluted with water after which, a suitable amount of sulphuric acid was added to achieve the target final acidity after which, the ethanol solution was further diluted with water to achieve the target ethanol concentration.

The raw lignin content of each fibrous biomass subsample was determined using the Klason lignin determination method. Then, after adding the fibrous biomass subsample to a pressure vessel (100-700 g odw chips), the tailored ethanol-based pulping solvent was added to the vessel (6:1 liquorwood ratio) after which it was brought up to the target temperature and pressure listed in the table. The biomass subsample was then "cooked" for the specified period of time after which, the pulping process was stopped. After pulping, the derivatives of native lignin were recovered by transferring the contents of pressure vessel to a press. The solids were then squeezed in a press and filtered through a coarse silk screen which separated the chip residues from the fine particles and the liquids. Next, the fine particles were separated from the liquids by filtering the suspension separated from the chip residues, through fine filter paper. The fine particles represent derivatives of native lignin that were extracted and which precipitated from solution after cooling and is herein referred to as self-precipitated derivatives of native Ugnin designated in the tables as "SPL". Finally, the derivatives of native lignin still remaining in the filtered liquid were precipitated from solution by dilution with cold water. The derivatives of native lignin precipitated by cold-water dilution are referred to herein as precipitated lignin or "PL". After determination of the dry weights of SPL and PL derivatives of native lignin, the relative yield of each Hgnin derivative was determined in reference to the Klason lignin value determined for the biomass sample before pulping. The yields of SPL and PL derivatives of native lignin for each subsample are expressed on a weight % basis relative to its total lignin value, and listed in Tables 5(a)-5(c) for the annual fibre feedstocks in columns next to the processing conditions used for each subsamples. The chip residues remaining after the first filtering step were pressed, dried and weighed. The yield of de-lignified residues, referred to in Tables 5(a)-5(c) as "PBY", are expressed on a % yield basis relative to the dry weight of the pre- pulping biomass subsample.

Characterization of the aliphatic hydroxyl content of derivatives of native lignin recovered from three species of annual fibre feedstocks.

Derivatives of native lignin recovered from annual fiber feedstocks were analyzed as described above to determine mmol primary hydroxyl groups/g sample (OH-pr mmol/g) and mmol secondary hydroxyl groups/g sample (OH-sec mmol/g). These data were then used to calculate mmol aliphatic hydroxyl groups/g sample (OH-al mmol/g)

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty seven samples of wheat straw biomass are shown in Table 5(a). The contents ranged from 2.03 mmol/g in 2.03 run 1 to 3.59 mmol/g in run 27.

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty six samples of sugarcane bagasse biomass are shown in Table 5(b). The contents ranged from 1.72 mmol/g in run 1 to 3.70 mmol/g in run 26.

The aliphatic hydroxyl contents of the PL lignin derivatives from each of the twenty seven samples of corn cob biomass are shown in Table 5(c). The contents ranged from 1.58 mmol/g in run 1 to 4.59 mmol/g in run 27. Table 5(a): Organosolv processing conditions for annual fibre feedstocks.

Alberta wheat straw

Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # PH NRSI min °C % % mmol/g mmol/g mmol/g

1 2.86 90 195 41 38.17 1.20 0.82 2.03 54.02

2 2.15 39 189 50 47.53 1.31 1.15 2.46 44.71

3 2.26 49 192 37 37.01 1.36 1.10 2.47 55.32

4 2.23 100 190 67 56.88 1.53 0.96 2.49 55.76

5 1.80 42 179 51 52.09 1.66 0.89 2.55 34.17

6 2.09 32 187 69 49.66 1.59 0.97 2.56 37.02

7 2.07 67 189 51 54.08 1.52 1.05 2.58 52.10

8 1.85 70 185 47 47.92 1.59 0.99 2.58 43.22

9 1.96 56 175 68 53.59 1.74 0.87 2.60 35.85

10 2.21 87 181 66 46.06 1.62 1.19 2.81 36.46

11 2.24 48 184 65 43.48 1.67 1.15 2.82 36.63

12 1.76 37 180 36 24.73 1.75 1.10 2.84 41.10

13 2.03 66 166 71 46.36 1.77 1.08 2.85 27.90

14 2.10 106 176 38 35.07 1.61 1.25 2.86 45.20

15 2.34 99 183 54 53.25 1.71 1.19 2.90 40.66

16 2.49 53 185 72 30.91 1.69 1.34 3.03 35.02

17 2.59 27 163 63 19.82 1.29 1.75 3.05 25.41

18 2.40 94 178 61 36.39 1.64 1.42 3.06 39.29

19 2.03 77 176 42 40.81 1.66 1.42 3.08 42.17

20 2.20 64 165 65 23.88 1.69 1.47 3.16 30.85

21 1.97 93 165 40 31.81 1.69 1.47 3.16 40.17

22 2.65 59 182 45 25.31 1.67 1.52 3.19 29.68

23 2.61 72 162 70 19.08 1.55 1.64 3.19 24.37

24 2.67 74 175 53 9.24 1.72 1.48 3.19 29.51

25 2.21 48 174 57 9.82 1.65 1.65 3.30 27.51

26 2.45 79 178 49 39.27 1.80 1.56 3.36 36.83

27 2.12 62 172 35 20.65 1.66 1.93 3.59 24.59 Table 5(b): Brazilian sugarcane bagasse

Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # PH NRSI min °C % % mmol/g mmol/g mmol/g

1 2.08 48 184 65 45.13 0.93 0.79 1.72 35.80

2 2.19 61 178 66 49.76 1.02 0.73 1.74 52.34

3 2.36 34 180 45 44.27 0.99 0.99 1.99 49.32

4 2.01 23 170 66 39.56 1.19 0.89 2.09 41.80

5 2.43 79 178 49 40.84 1.57 0.60 2.17 40.56

6 2.44 50 192 43 37.36 1.02 1.17 2.20 46.90

7 2.50 26 183 71 45.82 1.66 0.58 2.24 32.49

8 2.06 47 176 38 34.11 1.15 1.15 2.30 50.07

9 2.19 54 164 58 44.95 1.31 1.02 2.34 38.73

10 2.51 78 166 62 44.94 1.28 1.05 2.34 42.49

11 2.10 28 171 46 43.75 1.36 1.13 2.49 48.63

12 2.08 44 161 52 44.20 1.43 1.07 2.50 38.93

13 2.93 69 184 42 30.26 1.47 1.05 2.51 37.80

14 2.77 95 168 53 39.46 1.64 1.00 2.64 34.10

15 2.68 57 188 63 47.51 1.74 1.02 2.76 29.49

16 2.37 52 172 50 42.06 1.91 0.85 2.76 33.41

17 2.38 42 173 60 43.37 1.70 1.06 2.76 30.85

18 2.41 68 162 47 35.99 1.79 1.00 2.79 34.71

19 2.84 98 174 37 24.45 1.31 1.52 2.83 41.37

20 2.91 59 182 39 28.67 1.59 1.28 2.87 42.05

21 3.26 32 197 51 42.14 1.53 1.39 2.92 39.05

22 2.92 88 171 73 8.67 1.51 1.51 3.02 24.49

23 3.19 81 181 57 31.83 1.50 1.69 3.19 25.37

24 2.63 72 162 70 32.48 1.79 1.48 3.26 22.37

25 2.55 27 163 63 43.46 2.05 1.28 3.33 22.85

26 2.75 37 167 40 21.56 1.31 2.39 3.70 24.20 Table 5(c): European corn cobs

Time Temp. Ethanol PL OH-pr OH-sec OH-al

Run # pH NRSI min °C % % mmol/g mmol/g mmol/g

1 2.18 100 190 67 56.58 0.95 0.63 1.58 45.15

2 1.76 37 180 36 33.32 0.66 0.98 1.64 45.32

3 1.85 42 179 51 52.34 0.71 1.03 1.73 52.54

4 1.93 70 185 47 49.02 0.65 1.16 1.81 43.90

5 2.10 67 189 51 52.01 0.64 1.22 1.86 45.98

6 1.89 56 175 68 49.73 0.56 1.31 1.87 39.29

7 2.21 48 184 65 49.62 0.50 1.62 2.12 40.34

8 2.33 49 192 37 29.35 1.49 0.65 2.14 53.29

9 1.98 66 166 71 47.93 0.68 1.48 2.15 39.88

10 2.04 32 187 69 45.27 0.74 1.42 2.16 38.37

11 2.14 87 181 66 52.93 0.69 1.50 2.19 43.54

12 1.93 93 165 40 35.49 1.58 0.76 2.34 32.56

13 2.17 99 183 54 50.71 1.24 1.11 2.35 49.00

14 2.11 106 176 38 32.28 0.82 1.58 2.39 42.20

15 2.18 53 185 72 42.72 0.60 1.81 2.41 31.73

16 2.00 77 176 42 38.75 0.81 1.61 2.42 40.61

17 2.54 72 162 70 20.05 0.75 1.74 2.49 26.80

18 2.81 61 178 66 31.52 0.89 1.66 2.55 36.15

19 2.53 27 163 63 18.86 0.83 1.77 2.61 24.98

20 2.09 48 174 57 47.17 0.61 2.01 2.63 35.41

21 2.36 79 178 49 45.43 1.29 1.41 2.69 44.17

22 2.28 64 165 65 41.20 0.69 2.01 2.69 29.68

23 2.31 94 178 61 47.72 0.80 1.97 2.77 38.29

24 2.42 79 169 59 27.61 1.21 1.59 2.80 26.24

25 2.19 39 189 50 47.01 1.85 0.99 2.84 47.24

26 2.50 59 182 45 37.77 1.37 1.79 3.16 51.41

27 1.90 62 172 35 23.86 2.29 2.29 4.59 43.98 Characterization of the RSI of derivatives of native lignin recovered from three species of annual fibre feedstocks.

Each of the lignin derivative subsamples produced above was assessed for its radical scavenging index (RSI). The potential antioxidant activity of each PL lignin derivative was determined by measuring its radical savaging capacity as described above.

The NRSI values for lignin derivatives recovered from wheat straw biomass are shown in Table 5(a). The NRSI values for lignin derivatives recovered from sugarcane bagasse biomass are shown in Table 5(b). The NRSI values for lignin derivatives recovered from corn cob biomass are shown in Table 5(c).

EXAMPLE 4: Predictive equations for selective recovery of lignin derivatives having targeted aliphatic hydroxyl contents, from organosolv pulping of hardwood biomass feedstocks

BC Aspen:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of aspen shown in Table 1 (a), the intervals used for model generation were: (a) pH = [1.64, 3.30]; (b) Ethanol concentration in the organic solvent (% w/w) = [41, 79]; (c) pulping time duration (min) = [21, 115]; and (d) pulping temperature (°C) = [166, 205].

The equation derived from the aliphatic hydroxyl data shown in Table 1 (a) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content from the range of about 0.48 mmol/g to about 4.94 tnmol/g, is:

13.9417-0.0764507*Temperature-0.20763*Ethanol+0.566778*pH *pH- 0.00303132*pH*Time+0.00106268*Temperature*Ethanol EQ 1

Fig. 1 shows aliphatic hydroxyl contents of lignin derivatives recovered from aspen as a function of organic solvent concentration [Ethanol] and pulping temperature [Temperature] at constant pH of 2.47 and pulping time of 68 min., and shows process conditions suitable for producing lignin derivatives of the present disclosures have either decreased or increased aliphatic hydroxyl contents. Chilean acacia:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of acacia shown in Table 1(b), the intervals used for model generation were: (a) pH = [1.79, 3.20]; (b) Ethanol concentration in the organic solvent (% w/w) = [41, 79]; (c) pulping time duration (min) = [21, 115]; and (d) pulping temperature (°C) = [166, 205].

The equation derived from the aliphatic hydroxyl data shown in Table 1 (a) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content from the range of about 0.68 mmol/g to about 7.28 mmol/g, is:

44.4758-17.3944*pH-0.342106*Temperature+0.373582*Ethanol- 0.0133583*pH*Time+0.124198*pH*Temperature+0.000205204*Time*T ime- 0.00333743*Ethanol*Ethanol EQ 2

Fig. 2 shows aliphatic hydroxyl contents of lignin derivatives recovered from acacia as a function of pulping time [time] and acidification of the organic solvent [pH] at constant organic solvent concentration of 60.0% (w/w) and pulping temperature of 185.5°C, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.

Chilean eucalyptus:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of eucalyptus shown in Table 1(c), the intervals used for model generation were: (a) pH = [1.65, 3.22]; (b) Ethanol concentration in the organic solvent (% w/w) = [41, 79]; (c) pulping time duration (min) = [21, 115]; and (d) pulping temperature (°C) = [166, 205].

The equation derived from the aliphatic hydroxyl data shown in Table 1(a) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content from the range of about 0.63 mmol/ g to about 6.07 mmol/ g, is:

42.1508+4.21822*pH-0.5579848Temperature+0.352034*Ethanol- 0.0197431*pH*Time+0.000758397*Time*Ethanol+0.00148659*Temper ature*Temperat ure-0.000837671*Temperature*Ethanol-0.00251297*Ethanol*Ethan ol EQ 3 Fig. 3 shows aliphatic hydroxyl contents of lignin derivatives recovered from eucalyptus as a function of acidification of the organic solvent (pH] and pulping temperature [Temperature] at constant organic solvent concentration of 60.0% (w/w) and pulping time of 68 min, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.

EXAMPLE 5: Predictive equations for selective recovery of lignin derivatives having targeted aliphatic hydroxyl contents, from organosolv pulping of softwood biomass feedstocks

BC hybrid spruce:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of hybrid spruce shown in Table 4(a), the intervals used for model generation were: (a) pH = [1.72,3.15]; (b) Ethanol concentration in the organic solvent (% w/w) = [42, 79]; (c) pulping time duration (min) = [31, 110]; and (d) pulping temperature (°C) = [167, 199].

The equation derived from the aliphatic hydroxyl data shown in Table 4(a) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content of about 5.23 mmol/g or less, is:

65.2341-0.689028*Temperature+0.170969*Ethanol+0.0217104*p H*Temperature- 0.0267202*pH*Ethanol-

0.000116382*Time*Temperature+0.000382542*Time*Ethanol+0.0 0156337*Temperatur e*Temperature-0.00113549+Ethanol*Ethanol EQ 4

Fig. 4 shows aliphatic hydroxyl contents of lignin derivatives recovered from hybrid spruce as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 60.5% (w/w) and pulping temperature of 183°C, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.

Chilean radiata pine:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of radiata pine shown in Table 4(b), the intervals used for model generation were: (a) pH = [1.72,3.08]; (b) Ethanol concentration in the organic solvent (% w/w) = [42, 79]; (c) pulping time duration (rnin) = [31, 110]; and (d) pulping temperature (°C) = [167, 199].

The equation derived from the aliphatic hydroxyl data shown in Table 4(b) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content of about 1.96 mmol/g to about 5.60 mmol/g, is:

13.9072-0.103563*Temperature+0.124245*Ethanol-

1.31731*pH*pH+0.0386197*pH*Temperature+0.040326*pH*Ethano l+0.000100503*Ti me*Time-0.000526035*Time*Ethanol-0.00112536*Temperature*Etha nol EQ 5

Fig. 5 shows aliphatic hydroxyl contents of lignin derivatives recovered from radiata pine as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 60.5% (w/w) and pulping temperature of 183°C, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.

Southeastern USA loblolly pine:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of loblolly pine shown in Table 4(c), the intervals used for model generation were: (a) pH = [1.49, 3.52]; (b) Ethanol concentration in the organic solvent (% w/w) = [37.8, 90.2]; (c) pulping time duration (min) = [27.9, 121]; and (d) pulping temperature (°C) = [150.3, 218.9].

The equation derived from the aliphatic hydroxyl data shown in Table 4(c) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content of about 1.22 mmol/g to about 4.83 mmol/g, is:

19.7852-11.2196*pH-0.153691*Time-

2.39789*pH*pH+0.0880747*pH*Time+0.102069*pH*Temperature+0 .0203294*pH*Et hanol-0.000537328*Time*Time-0.000706365*Temperature*Temperat ure- 0.000470555*Ethanol*Ethanol EQ 6

Fig. 6 is a chart showing aliphatic hydroxyl contents of lignin derivatives of the present disclosure recovered from loblolly pine as a function of pulping time [Time] and pulping temperature [Temperature, °C] at constant pH of the pulping liquor of 2.43 and organic solvent concentration of 62% w/w ethanol, and process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents;

EXAMPLE 6: Predictive equations for selective recovery of lignin derivatives having targeted aliphatic hydroxyl contents, from organosolv pulping of annual fibre biomass feedstocks

Alberta wheat straw:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of wheat straw shown in Table 5(a), the intervals used for model generation were: (a) pH = [1.76, 2.86]; (b) Ethanol concentration in the organic solvent (% w/w) = [36, 72]; (c) pulping time duration (min) = [27, 106]; and (d) pulping temperature (°C) = [162, 195].

The equation derived from the aliphatic hydroxyl data shown in Table 5(a) for selection of two or more operating conditions for production of Ugnin derivatives having an aliphatic hydroxyl content of about 1.83 mmol/g to about 3.95 mmol/g, is:

-20.3795+5.44647*pH+0.286802*Temperature-0.218004*Ethanol - 1.35259*pH*pH+0.00661225*pH*Time+0.0170796*pH*Ethanol- 0.00016601 l*Time*Time+0.0000958888*Time*Ethanol-

0.00103049*Temperature*Temperature+0.000921376*Temperatur e*Ethanol EQ 7

Fig. 7 shows aliphatic hydroxyl contents of lignin derivatives recovered from wheat straw as a function of organic solvent concentration [Ethanol] and pulping time [Time] at constant pulping temperature of 85.5°C and organic solvent acidified to a pH of 2.2, and shows process conditions suitable for producing lignin derivatives of the present disclosures that have either decreased or increased aliphatic hydroxyl contents.

Brazilian sugarcane bagasse:

In reference to the operating conditions for the twenty six preliminary organosolv pulping runs with subsamples of sugarcane bagasse shown in Table 5(b), the intervals used for model generation were: (a) pH = [2.01, 3.26]; (b) Ethanol concentration in the organic solvent (% w/w) = [37, 73]; (c) pulping time duration (min) = [23, 98]; and (d) pulping temperature (°C) = [161, 197].

The equation derived from the aliphatic hydroxyl data shown in Table 5(b) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content of about 1.55 mmol/g to about 3.84 mmol/g, is:

37.6682-0.119057*Time-0.309507*Temperature-

0.126539*Ethanol+0.0255398*pH*Ethanol+0.000640605*Time*Te mperature+0.000691 701*Temperature*Temperature+0.000531287*Ethanol*Ethanol EQ 8

Fig. 8 shows aliphatic hydroxyl contents of lignin derivatives recovered from bagasse as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 55% (w/w) and pulping temperature of 179°C, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.

European corn cobs:

In reference to the operating conditions for the twenty seven preliminary organosolv pulping runs with subsamples of corn cob biomass shown in Table 5(c), the intervals used for model generation were: (a) pH = [1.76, 2.81]; (b) Ethanol concentration in the organic solvent (% w/w) = [35, 72]; (c) pulping time duration (min) = [27, 106]; and (d) pulping temperature (°C) = [162, 192].

The equation derived from the aliphatic hydroxyl data shown in Table 5(c) for selection of two or more operating conditions for production of lignin derivatives having an aliphatic hydroxyl content of about 1.42 mmol/g to about 5.05 mmol/g, is:

-44.7775+0.544455*Temperature-2.22722*pH*pH+0.0637232*pH* Temperature- 0.000080298*Time*Ethanol-0.00200084*Temperature*Temperature EQ 9

Fig. 9 shows aliphatic hydroxyl contents of lignin derivatives recovered from corn cobs as a function of acidification of the organic solvent [pH] and pulping time [Time] at constant organic solvent concentration of 53.5% (w/w) and pulping temperature of 177°C, and shows process conditions suitable for producing lignin derivatives of the present disclosures having either decreased or increased aliphatic hydroxyl contents.