PROCESS FOR PULPING LIGNO-CELLULOSIC MATERIAL

Abstract: A process for making defibered pulp material compris­ ing the steps of treating fibrous ligno-cellulosic material with aqueous nitric acid (10,17) having an HNO₃ concentration of about 0.15 to 9.0 wt.% and containing aluminium sulphate in an amount of about 0.8 to 1.3 parts per each 10 parts by weight of HNO₃, or to alternatively use for grassy fibrous materials nitrate salts such as NaNO₃ or KNO₃ or NH₄NO₃, so as to nitrate ligneous component of said material; and thereafter defibering directly, (15,21) or treating the nitrated ligno-cellulosic material with alkali to separate the ligneous component from the cellulosic pulp, and, optionally, recom­ bining a part or all of the ligneous component with the cel­ lulosic pulp.

Description: Accelerated Pulping Process This invention relates to an improved process of making fibre in a form ranging from a moderately digested product fit for animal feed to pulps that can be utilized as conventional semi-chemical, chemical types for packaging papers or fully delignified pulps for bleaching from fibrous, ligno-cellulosic raw material, More particularly, it relates to a nitration pulping process using nitric acid or nitrate salts in which the time required for nitration and the second step extraction of the nitrated ligneous components in the fibrous raw material is substantially shortened due to the inclusion in the nitric acid of a small amount of aluminium sulphate (paper maker's alum), and by use of the inherent flexibility of the process time, temperature and chemical concentration , the utilization of controlled delignification to produce animal feed, building board, packaging boards and paper. So far as I am aware, nitric acid pulping processes, of which many have been proposed, have never been carercially successful for various reasons, chief among which is the relatively long chemical treatment time that they required far exceeding the present day conventional methods. Shortened times were possible if strong nitric acid was used, or if pressurized vessels and high temperatuns were employed, but those conditions create other problems such as excessive and explosive emission of toxic nitrogen oxide fumes and damage to the cellulosic fibre structure. Moreover, recovery of the acid has not been possible, and the use of relatively concentrated nitric acid, e.g. 15 to 42 t.by wt.HNO3, becomes therefore prohibitively expensive. In short, the nitric acid pulping processes heretofore proposed have offered no advantages and many disadvantages over present day conventional systems. As recently as 1960 a published comprehensive review on nitric acid pulping by Crown Zellerbach Corporation stated that while nitric acid was specific for the reaction with lignin, the use of acid reagent was excessive and uneconomicland pollution problems remained unsolved. The process of this invention uses only 0.15 - 9.0% nitric acid in relation to fibre yield which, together with the alkali used for delignification, is no more than with conventio- nal methods of pulping without chemical recovering systems while eliminating the complex requirements of recovery and/ or manufacture of the cooking liquors. Furthermore, since the process is a two step one, the nitrating solution can, except for that absorbed in the fibre structure, be recovered virtually intact and recycled. More importantly, unlike previous attempts with nitric acid, this new process does not dissolve the lignin content of fibrous structures in the acid stage. Conventional pulp mills require high investment due to the high temperatures and pressure involved, and if water and air pollution is controlled and chemical recovery is practiced costs are substantially higher. The process of this invention uses simple chemicals available in crystall:ne or dissolved form, does not require superatmospheric pressure, or temperatures over 100 C, offers minimal problems of air and water pollution, and offers economic usability of the products normally wasted by burning or dumping. I have now discovered that in a chemical pulping process involving impregation of particulate, fibrous, lignocellulosic raw material with nitric acid which may be or not be followed by alkaline extraction from the material of the resulting nitrated lignin, leaving softened, partially defibered cellulosic structures which can be completely defibered by mechanical pulping means, the total time required for the nitration and extraction steps can be shortened considerably by including a small amount of aluminium sulphate (paper maker's alum) in the nitric acid. While the precise time required for the nitration-extraction operation is dependent upon the variables of particle thickness, temperature and reagent concentration, it can be said for the process of the present invention that it generally enables one to perform the nitration-extraction operation somewhere in the range from about 20 minutes minimum for high yield wood chemical pulps for packaging papers and boards, to a maximum time of 50 minutes for easily bleached pulps without using pressure and with temperatures not exceeding 1000C. Those times are to be compared to the conventional sulphite process times of 6.25 hours and 7.50 hours and the sulphate process times of 2.5 and 5.0 hours,respectively,at high pressures and temperatures, as set forth in the following table I: Table I Pulping Processes Compared Liquor Total Temperature, Pressure, Fibre Total Concentration, Cooking C P.S.I.G. Species Yield, % Wt.% Time 1. Casey, "Pulp and Paper" Vol. 1, p. 169 Sulphite-Bleach Grade Calcium Base 6.0 6.25 hrs. 140 80 Western Conifer 45.4 Ammonia Base 6.0 7.50 hrs. 146 80 Western Conifer 45.0 2. Casey, pp. 230-264 Sulphate - High Yield 18.5 2.50 hrs. (1) 170 140 U.S. So. Pine 60.0 Sulphate - Bleachable 22.0 5.00 hrs. (1) 160 100 U.S. So. Pine 43.0 (1) includes time to bring to temperature 3. TAPPI CA Report, 52 pp. 17-19 Bagasse - Soda Process 6.5 26.50 min. (2) 170 114 Bagasse 56.0 (2) includes cooking time in blow tank 4. TAPPI CA Report, 52, pp. 26-27 Bamboo - Kraft Process 17-19 1.25 hrs. 150 85 Bamboo 56.0 5. Accelerated Pulping Examples (Invention) HNO3 NaOH High Yield Grade 5.5 / 0.3 30 min. 85-100 None U.S. So. Pine 56.0 Bleachable Grade (1 st sequence) 3.0 / 0.3 30 min. 85-100 None Norway Spruce 45.0 (2 nd sequence) 1.5 / 0.1 20 min. 85-100 None Bagasse 0.8 / 0.2 30 min. 85-100 None Bagasse 52.0 Bambo 3.0 / 0.2 30 min. 85-100 None Bamboo 44.0 Although the invention is described below mainly referring to the embodiment involving an alkaline extraction of ni trated lignin after the nitration step, it is recognized that, though preferable, an alkaline extraction is not absolutely necessary for the production of paper pulps. However, the addition of alkali is necessary for the pro duction of animal feeds and would be normally used in the production of semi-chemical pulp where maximum defibetiza tion for minimum chemical treatment is desired. The ability of the present process to be conducted under atmospheric pressure eliminates the need of explosive re lease of pressure that is used in conventional chemical pulp systems to defibre the fibrous structures within chips or chopped materials. The basic preservation of the fi brous structure permits easy recycling of the fibrous structure through an additional gentle cooking cycle, if required, and easy drainage of cooking liquor and washing out of the residual black liquor leaving the fibrous struc ture substantially intact. Defiberization is then accompli shed mechanically with gentleness and rapidity, with minimum loss of fibre length and degradation of basic fibre structure. Additionally, the defiberization can be closely controlled to preserve long thin fibre bundles from fibrous structures made up of very short (under 0.5mm) fibres such as straw thus improving strength and drainage characteristics. All forms of ligno-cellulosic materials can be subjected to the pulping process of the present invention. That in cludes, without limitation, woody materials such as U.S. Southern pine, spruce, beech and bamboo, as well as grassy materials which find minor usage such as straws, bagasse and kenaf. In addition to these normally used sources of paper making fibre, other, now wasted, fibrous plants as rape seed straw and rice husks which resist conventional pulping methods can easily be reduced to potentially useful fibre by this process. High yield shrub growth such as coppice willow found extensively in Ireland and presently unused produces, including its bark, an acceptable, clean and economic paper making fibre. Besides such virgin materials, the process of the present invention can be used to delignify and further defibre paper wastes, such as waste corrugated boxes containing semi-chemical board. Finally, it becomes practical to economically pulp small accumulations of wood slab waste and sawdust which are most often burned. The raw material should be in particulate form before being submitted to the nitration step. Virgin plant material, for example, should be chopped, crushed, chipped or flaked. Paper wastes should be mechanically pulped in water to the defibered state, for example to obtain a slurry containing about 7 to 9 wt.% cellulose. When it is wood that is to be pulped, the required nitration extraction time will be shorter and the pulp more uniform if the wood particles are thinner. It has been found expecially advantageous to use wood flakes, i.e. particles about 0.3 to 0.8 mm thick obtained by cutting the log tangentially to the circumference. Flaking is the cutting process used in manufacturing particleboard. At the present time the paper manufacturing industry uses wood chips almost exclusively, the thickness of which is usually in the range of about 6 to 10mum. Horsepower consumption for the flaking of logs is roughly equivalent to that for chipping, as are production levels and flexibility in handling short or long or different diameter logs. The use of flakes does require higher cubic handling and cooking capacities than does chips, but flaking is nonetheless economically acceptable in the pulping process of this invention because high pressure pressurized cooking vessels with restricted volumes are not required. Use of wood flakes, rather than the thicker chips, speeds nitric acid impregnation and also shortens the time required for outward diffusion of dissolved lignin in the subsequent alkaline extraction step. Additionally, flaking is accomplished by cutting around the circwmferencz of the log, much as veneers are made, whereas chipping is performed by cutting at the end of the log, the fibre length is essentially preserved in flakes and the fibre ends are not crushed. Chipping, on the other hand, fractures the fibres and crushes their ends. The more intact fibre structures and greater exposed surface of the flakes are more easily penetrated by the chemicals used in the nitration and extraction steps of the present process. The fibres produced from flakes are marginally shorter than those of conventional chips. Where a pulp is required for rough papers, i.e. brown or packaging papers and boards, conventional chips can be used after subjecting them to conventional crushing which reduces them to rough splinters 1.5 - 3.0mm thick, 4.0 8.0mm side and 25mm long. The nitration (cooking) of the ligno-cellulosic raw material is accomplished by submerging or wetting with recycled acid the material in a sufficient amount of aqueous nitric acid at elevated temperature, preferably 85 to 1000C to penetrate the fibrous structure and react with the lignin. In order to permit the use of an open vessel for the nitration step, without the emission of harmful nitrogen oxide vapors, it is preferred to use very dilute nitric acid, say having an HN03 concentration of about 0.15 to 9.0 weight percent, e.g. 0.15 to 5.5 weight percent, preferably less than 5.5 weight percent and most preferred less than 5 weight percent. It can be preferred to subject the lignocellulosic raw material to an impregnation step before the cooking-nitration step. The impregnation is done with a dilute concentration of the cooking liquor at low tem peratures (e.g. 700C or below, e.g. 500C or below) and serves three purposes: a) Utilization of drained concentrated liquor after the cooking process together with the dilute cooking liquor from the washing process, b) conservation of heat by recycling liquor, and c) even moisture distribution throughout the fibrous structure before cooking. Whereas the cooking step is not necessarily preceeded by an impregnation step, an impregnation step is always followed by a cooking step. The preferred acid strength in the cooking-nitration step depends upon the nature of the ligno-cellulosic raw material being pulped. For U.S. Southern pine, for example, which is relatively high in lignin content (over 30 wt.%), and contains a high percentage of resins and waxes it is preferred to use an HN03 concentration of at least 4.5 or 5.5 wt.%. Wheat straw, on the other hand, is low in lignin content (about 15 wt.%) and is preferably cooked and nitrated with nitric acid having an HN03 concentration of only about 0.8 to 1.5 wt.% for production of chemical pulp. These concentrations are based on a normal nitration period of 15 minutes and production of chemical type pulp. Where impregnation periods and longer time is used the acid concentration can be drastically reduced. For example, spruce flakes-impregnation 30 minutes at 0.5% concentration plus cooking and nitration, respectively, 45 minutes at 1.75%. Where a pulp of lower purity (i.e. less delignification) is required the said concentration can be reduced, as in animal feed or semi-chemical pulp. As a practical matter it will usually be woody plant material that is twice subjected to the cookingnitration/lignin-extraction sequence, since grassy plant materials and paper wastes can have their ligneous components nitrated and almost completely extracted in one sequence using relatively stror.- ger, but still dilute, nitric acid, and obtain pulp of adequate cellulosic purity and easy bleachability. Even with woody raw materials, a single nitration-eYtraction sequence is all that is required where the pulp product is to be used to make linerboard and lower brightness pa- pers and not to make high purity cellulose or ih brightness paper. In the process of the present invention the nitric acid impregnation lic¯.cr is augmented with a nitration accelerating amount of aluminum sulphate, preferably about 0.8 to 1.3 parts thereof per each 10 parts b. weigh. of l J03. As stated above, the presence of the aluminum sulphate te in the nitric acid serves to shorten dramatically ehe time required to dissolve the nitrated lignin in the subsequent alkaline extraction step. Normal usage is 1.0 part of the aluminum sulphate per each 10 parts by weight of . 3. fas ). The amount of nitric acid used in the nitration step should be sufficient to completely react by submergence or contact by recirculation the particulate ligno-cellulosic material and adequate on a stoichiometric basis to nitrate all of the lignin content of the raw materials. This ii usually mean formation of a mixture of 5 parts of liquid acid to 1.0 part of dry wood to 10 parts of liquid ac c for 1.0 part of dry grass fibre (straw). Where the acid liquor can be circulated and heated indirectly lower ratios can be used. Additionally the acid can be sprayed or foamed in low concentration on grassy fibres to form an intimate mixture to a composite moisture content of 35 to 50% and then subjected to heat for reaction at once or at later date - six months or more without degredation. The temperature at which the nitric acid cooking step, is performed should be adequate to effect nitration of the lignin, but is preferable not so high as to cause degradation of the cellulosic fibres. Temperatures within the range of about 85 to 1000C, in particular about 85 to 950C, are preferred. Since the nitration-extraction portion of the process of the present invention can be performed in such a short period of time, it is possible to conduct both of those steps under atmospheric pressure conditions, although superatmospheric pressures, e.g. from 10 to 35 p.s.i.g.,can be used if it is desired to shorten the nitration time slightly but chiefly to provide ease of processing on a continuous basis. The improvement provided by the present invention is independent of whether the process is conducted under atmospheric pressure or at elevated pressures. The introduction of a non pressure system is designed specifically for use in new and relatively small pulping installations (10 - 50 tons per day) throughout the world. However, it is recognized that the requirement for larger production units can be met and that in many instances existing pulp mill equipment could be utilized to reduce investment costs in preventing present pollution problems. All present systems use high pressures and temperatures coupled with long cooking periods for fully defibered or chemical pulps from either wood or grasses. It has been found that by cooking with light pressures (15-35psig) while holding temperatures at 11 00C or below, preferably below 1 000C (most preferably 95 C) the nitration period can be shortened to 5 - 7 minutes for wood flakes, straw, etc. Conventional sized wood chips can also be readily pulped although the cooking time period is extended to one hour requiring two nitration steps with a preliminary defibering step between. Alternatively, the chips can be crushed previous to filling the digester and the nitration step limited to one step which additionally avoids the possibility of over and under reacted fibrous structures. These methods of using light pressures with either wood flakes or chips makes practical, for example, the conversion of existing sulphite pulp mills to this process. Other pulping systems such as the "Kamyr" or "Pandia"-s stem, which are continuous, oera- ting at high pressure,150 - 175 psig, are also adaptable for processing wood chips in one stage producing a semichemical type after normal mechanical defibering or full chemical pulp. Thus, in a special embodiment of the inventive process the nitration step is operated at a pressure of about 100 to 150 psig when using as starting material crushed wood chips as used in conventional processes today. See Table IIa "Comparative Hun03 Pressure Nitration Cycles . Normal Chemical or Delignified pulp. Additionally it has been found that the use of pressure permits full defibering of the fibrous structure in the nitration stage without production of black liquor thus avoiding the lignin alkali extraction phase. This is accomplished by raising the N03 liquor concentration by 2.5 - 3.5% over that required for the nitration-alkali delignification sequence and extending the time of reaction slightly, 3-5 minutes. Thus, without using pressure, i.e. conducting the process under approximately atrnospherc pressure conditions, the HNO liquor concentration is preferably at most 5.5 weight percent, in particular at most 5 weight percent. When employing pressure, the HN03 concentration can go up to 9.0 weight percent and preferably it is no more than 7.5 or 7.0 weight percent. Of course, the lower concentrations as stated for the pressurized nitration step can be advantageously used. The process without delignification produces a fibre for different and limited end use papers than that of the Table IIa Comparative HNO3 Pressurized Nitration Cycles, Normal Chemical or Deliquified Pulp with Alkali Stage A. Non Pressure Syste - Wood Flakes or Equivalent Pine Spruce Beech Straw Cooking Time Minutes 15 15 15 15 Temperature C 85 85 85 85 Liquor Concentration % 5.5 5.0 4.0 1.0 B. Pressure 15 - 35 p.s.i.g. - Wood Flakes or Equivalent Pine Beech Straw Bamboo Cooking Time Minutes 7 7 5 7 Temperature C 110 110 110 110 Liquor Concentration % 5.5 3.5 0.5 2.5 C. Pressure 15 - 35 p.s.i.g. - Wood Chips Spruce Beech Cooking Time Minutes 45 45 Temperature C 110 110 Liquor Concentration % 4.5 3.5 Defiberization x x Time - Non Pressure Minutes 15 15 Temperature C 85 85 Liquor Concentration % 2.5 2.0 D. Pressure 100 - 150 p.s.i.g. - Wood Chips Beech Spruce Beech Semi-Chemical Cooking Time Minutes 45 45 10 Temperature C 110 110 110 Liquor Concentration % 4.5 3.5 3.0 Deberization - - x delignified type fiber. It is of very light colour, high yield and can be easily bleached to high brightness levels, but not by normal alkaline bleaching. The reduced handling of the fibrous structure greatly improves its drainage properties and facilitates washing which is a major problem today in bleaching short fibre structures such as straw. In all theses uses of pressure it is not necessary to vent any gases; in fact it is economic that with the gases be contained and retain to create a false pressure and keeping operating temperatures below 1000C thus avoiding cellulose degradation. The degree of fals pressure created is dependent on acid concentration. See following Table IIb "Comparative HNO, Pressure Witra- tion Cycles . No Delignification Stage. Where additional pressure is needed as in the'amyr"-process to facilitate operation it can be obtained with air injections. The ability to conduct the nitration step at atmospheric pressure means that substantially open vessels can be employed providing substantial savings in equipment cost compared to conventional superatmospheric pulping processes. Although an open vessel can be employed for the nitration step, it is preferred to maintain closure with recycling of vapors to prevent possible troublesome emission of nitrogen oxide vapors. Present environmental laws in the U.S.A. permit a maximum nitrogen oxide emission level of only 185ppm. The precise temperature at which nitrogen oxide will be released from the slurry in the nitration step will depend upon the concentration of the nitric acid, since the higher the acid concentration, the lower will be the temperature at which nitrogen oxide vapor emissions will occur. By way of further explanation, nitric acid decomposes at Table IIb Comparative HNO3 Pressurized Nitration Cycles, Alkali Delignification Stage Eliminated A. Pressure 15 - 35 p.s.i.g. - Wood Flakes or Equivalent - Chemical Pulp Pine Beech Straw Bamboo Cooking Time Minutes 10 10 6 10 Temperature C 110 110 110 110 Liquor Concentration % 9.0 5.5 2.5 5.0 B. Pressure 100 - 150 p.s.i.g. - Wood Chips Chemical Pulp Spruce - Beech Cooking Time Minutes 45 45 Temperature C 110 110 Liquor Concentration % 8.0 5.5 C. Pressure 35 - 150 p.s.i.g. - Wood Chips - Semi-Chemical Pulp Mixed Hardwoods Beech Cooking Time Minutes 10 Temperature C 100 Liquor Concentration % 4.0 about 860C into water and nitrogen oxide gas, which is potentially lethal and can be explosive. The nitrogen cas is somewhat soluble in water, however : about 130cc wil dissolve in a litre of cold water, about 660cc wll dis - solve in a litre of hot water. If nitric acid having an HNO3 concentration greater than about 3.0 wt.% is heate in the presence of cellulose to above about 65 C then a exothermic reaction with the cellulose will result. for this reason, where an ipregnation step becomes preferabl to economize on nitric acid consumption through recycling of partly spent or diluted acid it is cesiaD o ain- tain low temceratres, e.g. 50 C or below. Temperat@res over 850C will produce nitrogen oxide gas which cepending on the acid concentration will be more thin the water can hold in solution and will have to be contained. when an open vessel is being used to conduct the nitration stop in the process of the present invention, it will usuall be preferred to employ a ternperature nc higher than about 900C or 950C. However, as stated herein before, when operating the nitration step under pressure a t..H of up to 110 C. preferably up to 100 C, can be employed. It is an outstanding advantage of the process of the pre sent invention that it can be performed in non-pressure vessels in short time periods, without causing air po1,u- tion problems. The nitration step, and indeed the entire process of the, present invention, can be carried out continuously, sei continuously, or batchwise, whichever is desired Selection of equipment will of course depend upon that choice. It is generally more economical to conduct the process continuously in which event the nitration step can advantageous- ly be conducted in some type of screw conveyor unit. Batchwise nitrations can be carried out quite well in 2 hydrapulper making possible the economic operation of very small mills. The nitric acid impregnation and cooking steps are conducted for a time sufficient to produce the required residual level of the ligneous component of the ligno-cellulosic raw material after extraction of the lignin. If the nitration-extraction sequence is performed twice, each nitration step can be conducted for a shorter period than if it were performed 1u5t once. The time required to effec the desired degree of nitration is dependent, of course, on the strength of the nitric acid used, as well as the temperature employed, since higher acid strengths and higher temperatures promote the nitration reaction. . - Additional considerations are the type and particle size of the ligno-cellulosic material being processed. In general, with the process of the present invention the total nitration time, whether performed in one step or broken down into two nitration-extraction sequences, can be as short as 5 minutes or extended to 45 minutes. For straw or bagasse which will go into dry storage before ligrification a simple spray or foam application at lower levels of acid -concentration at room temperatures is all that is necessary. Following the nitration step the ligno-cellulosic material is separated from the nitric acid solution and preferably washed with water to remove surface acid. The wash water is preferably hotoe.g. at a temperature of about 85 to 1000C and is used in minimal amounts. One efficient method of separating and washing the nitrated ligno-cellulosic material is by spindraining the slurry in a rotary dryer, foliow:4by water washing the solids in the same vessel. Another method, if a continuous system is used, is draining followedby reverse flow washing. Alternatively, draining, followed by flooding with wash water and a second raining can be used. The separated nitric acid is advantageously recycled to the nitration step to be used again, as is the acidic wash water. Both solutions will be relatively clear, but ray be slightly coloured due to the presence of small amounts dissolved material. The recycled nitric acid stream will be fortified with concentrated nitric acid and with fresh aluminum sulphate so as to restore the concentratios of those reagents to the desired levels. The nitrated fibrous structures remain intact and appear to be essentially the same as when those particles were introduced to the nitric acid submersion step, except fcr some softening and a slightly darker colour. The nitrated fibrous structures can be held in storage for months it- out either deteriorating or causing problems in the lignin extraction and defibering steps which follow. This storability feature can be of special advantage in the case where straw, bagasse or similar grassy plants are to De pulped. Grassy plants are usually harvested during ala- tively short seasons, causing temporary, seasonal surges in supply of that raw material to the pulp mills. Since the demand for the finished pulp is relatively constant, however, it becomes necessary to periodically store largo quantities of the excess ligno-cellulosic raw material. This presents a problem because grassy plants are particularly susceptible to bacterial or fungi attack during storage. By the process of the present invention the excess raw material can be nitrated without delay, by spraying or foaming a dilute solution of acid to obtain intimate, cn;erall contact with the fibre to a total moisture content of 30 to 50%, anot held in storage in that form without being degraded by bacteria. :- tended periods of storage have zeend experienced up to one year in contact with the acid at a moisture level of 30-502 permitting usage a very low percentage of acid to dry fibre, i.e. 1-3%. The nitrated lignocellulosic material is next submerged in an al1 line, aqueous extraction solution, e.g. a solution of sodium, potassium, and/or ammonium hydroxide, so as to dissolve most of the nitrated lignin out of the fibrous structure. The lignin nitrate is substantially insoluble in acidic aqueous media, but is readily dissolved in basic aqueous media, for example having a pH of about 12. The alkaline concentration of the extraction solution must be sufficient that the solution will leach out by dissolving most of the nitrated ligneous material in the fibrous structure. Usually it is preferred to use an alkaline strength (NaOH, KOH, or NH4OH) of preferably about 0.1 to 0.5 wt.%. If the nitration-extraction sequence is performed twice on the ligno-cellulosic material, then the alkaline strength used in the second extraction step need not be as high as that employed for the first extraction. Often the concentration of the alkaline solution used in the second nitration-extraction sequence will be about one-fifth to one-half that which is used in the initial sequence. The alkaline consumption is basical ly one of bringing the starting pH to about 12Jand is therefore somewhat dependent on the concentration of residual acid remaining. The amount of the alkaline extraction solution used should be adequate to completely submerge the ligno-cellulosic material and dissolve most of the nitrated ligneous components. Usually the amount of alkaline extraction solution used will provide a slurry containing about 5 to 8 wt. of the cellulosic fibre. The temperature at which the alkaline extraction step is conducted should be sufficiently high to effect dissolution of most of the nitrated ligneous material. Preferably a temperature of about 75 to 1ODOC is used. Temperatures as low as 150C can be used which will extend the time necessary for delignification. These low temperatures are particularly important in producing animal feed or partially ci0;cr & pulp from agria1t'Za residucs. ere straw as an example for an agricultural residue has been sprayed with nitric acid and held in storage, delignification with alkali under 500C will produce a fully defibered pulp. The alkaline extraction step is best performed under atmospheric pressure conditions, thereby permitting the use of an open vessel and avoidance of expensive high pressure equipment. If desired, however, for example to further shorten the extraction time or utilize existing pressurized euuiprnent, high temperatures and superatmospheric pressures, e.g. up to 10 or 15 p.s.i.g., can be used for the extraction. Increased time and temperatures using alkaline solutions will result normally in some degradation of the cellulose. As discussed above with regard to the nitration step, the nitration extraction sequence can be conducted just once, or it can be repeated, in which event each extraction step can be performed for a shorter period of time than if it were performed just once. It will be recognized that the time required to effect the desired degree of extra2- tion is dependent on the particle size and type of the ligno-cellulosic material, and the temperature at which the extraction is conducted. In general, however, the total time required for the ligninextraction, whether performed in one step or broken down into two extractions, will be no more than about 20 minutes, often being within the range of about 5 to 15 minutes If an open vessel is used for the extraction step, it can advantageously be a hydrapulper. If a closed vessel is used, a screw conveyor may be preferred. After treatment with the alkaline extraction solution, the fibrous, cellulosic material is separated from the lignin-containing solution, preferably in a high density press. If, however, the fibre bundles are to be subjected to a second nitration-extraction sequence, then it will suffice to just drain off the extraction liquor. After the extraction step, the alkaline solution contains dissolved ligneous components and is reddish brown in colour. It is usually referred to as "black liquor". During start-up of the process all of the separated black liquor, together with the alkaline wash water, can be returned to the extraction vessel for reuse. As the process is continued, however, the content of dissolved solids in the black liquor will grow to a maximum tolerable concentration,e.g., somewhere in the range of about 10 to 25 wt.%, depending upon the quality of product desired. At that point an appropriate portion of the black liquor should be regularly removed and replaced with make up clear alkali liquor in order to prevent further increase in the concentration of the dissolved solids. The black liquor purge stream could be disposed of by various means such as by dumping as waste, or by concentrating and burning. Alternatively, the black liquor purge stream can be combined with the completely defibered pulp to supply ligneous binder for fiber web products prepared from the pulp, especially paperboard. When the alkali lignin extraction process is complete the pH of the black liquor will be almost neutral, about 7.5 to 8.5 which is far lower than that of conventional alkaline processes the pH of which is usually in the range of 12-14. This factor of almost neutral pH makes the black liquor substantially more amenable to being handled in subsequent chemical processing. Sulphite acid systems produce black liquor in a pH range of 1.0 - 2.0. Additionally, the black liquor has a very low range of BOD5 (Biological Oxygen Demand - 5 day) and COD (Chemical Oxygen Demand) which together with its chemical make up permits its discharge in controlled amounts, up to 30%, in the normal urban effluent stream. Typical comparative pollution data are as follows: Values in mg/litre Accelerated Waste Paper Sulphite Pulping Mill Mill Black Black Liquor Effluent Liquor (From Spruce) 5 day biological oxygen demand 1500 8010 High Chemical oxygen demand 5685 16700 230,000 Permanganate number 11215 - 400,000 The BOD5 value when related to recently recorded (North America) BOD discharges per ton of pulp produced shows 5 the following values; sulphite mill 109 kg; integrated sulphate pulp and paper mills 15 kg; waste paper mill 10 kg; and the accelerated pulping process:30 kg. The low figure of the sulphate mill is reached only by burning all the black liquor solids produced to recover the major portion of the chemicals used in the process and the strict control of pollutants. Although the black liquor could be discharged in a controlled manner into normal drainage facilities, it can be utilized uniquely and economically in a variety of ways as a binder, water repellent or size, extender for fortified rosin size, stiffening agent in paper board, fertilizer, hygroscopic additive to soil, extender for resins such as phenolics, and retention agent in papermaking. The solids in the black liquor are referred to as ligneous component. Although there are other chemical components than lignin and lignin nitrate, respectively, such as gums, waxes, etc. the lignin is the major component. Moreover, when precipitating the lignin, some of the said further components precipitate with the lignin. This is to be recognized when speaking of ligneous component. The useful ligneous component can be precipitated from its mother black liquor by acidifying, preferably to a pH of 5.5 with any acid, but of particular usefulness are ordinary papermaker's alum (aluminum sulphate), recycled nitric acid from the process, and phosphoric acid. For normal papermaking the black liquor precipitant (ligeous component) resulting from acidification, e.g./with nitric acid or alum, can be added to the cellulosic pulp slurry, foamed (either in precipitated form or in form of the extraction liquor itself) and added at the wet presses or size press,or can be added in its neutral pH form (black liquor) and acidified or not at the size press or wet presses. Unlike kraft liquor the black liquor under any normal treatment either in solution or precipitated exhibits the minimum and non-troublesome amount of foaming. The foaming of the black liquor, either itself or in concentrated form (precipitated ligneous component) can be done by using a commercial surfactant or non-surfactant foaming chemical to foam water with air and then add as required the black liquor. This kind of application is known to the expert per se. However, not with the ligneous component. Addition of the precipitated black liquor (ligneous component) to the pulp slurry immediately lowers the stock freeness, i.e. drainage rate as it holds or retains the fine suspended particles usually lost through drainage on the paper machine wire. Addition of the black liquor to paperxfibres in normal amounts up to 15% based on the solids and calculated on the dry weight of the fibre will increase the strength properties, i.e. burst strength and stiffness,in an approximate ratio of improvement of 1:1 to 2:1 for equal weight of cellulose fibre depending on the degree of openness of the fiber web making up the paper. When combined with the starch solution and added at high temperature (65 C or above) at the size press, a satisfactory sizing of the board (COBB 50) will be obtained, and the effectiveness of the starch on improving paper quality is greatly improved permitting reduced starch usage. A percentage of 0.4 to 0.6% of black liquor solids on the dry fibre content is sufficient. Addition in its neutral form (up to 60% solids) to a solution of 20% neutralized urea and 20% fortified rosin size will obtain sizing properties essentially equal to that of the rosin size when used alone. This combination can be precipitated on fibre suspensions in the conventional manner with alum. The neutral form of the black liquor precipitate is hygroscopic when dried and can be used when combined with fast draining materials such as sandy soils to retain moisture and chemicals. When the fibre cooking process and subsequent precipitation is formulated with all or part of those three chemicals essential to plant life, nitrogen (nitric acid), potassium ( potassium hydroxide) phosphorus (phosphoric acid), the black liquor becomes a complete fertilizer in itself in addition to its retention properties. This can be readily achieved by using pc- tassium hydroxide in the alkaline extraction step and by precipitating the ligneous component out of the extraction liquor by using phosphoric acid. Official government tests show normal germination and growth rates for barley and oats when this liquor is added to an inert clay. For easy handling, it can be combined with diatomaceous earth to inhibit hygroscopic properties. The acidified form of the black liquor, i.e. precipitant, can add its binding properties to such resins as melamine or phenolics permitting extension of these relatively expensive products. The neutral black liquor can be used in the preparation of resins since its nitrated form is com patible chemically with that of many other resins. The acidified black liquor precipitant may be resolubilized by changing the pH to 7.5 with alkali and then again precipitated with acid at pH 5.5 making possible the concentration of the ligneous component through precipitant and then resolubilizing for further use in a neutral fcr During the alkaline extraction step most of the lignin trate dissolves in the alkaline solution, leaving the fibrous structure softened and partially defiberized. At this point the concentrated black liquor should be drained off for recycling or purging from the system as required. Sine little mechanical and/or explosive force has been exerted the point of fibre liberation will not have been reached under normal pulping conditions. Some of the ligneous com,- ponent remains partially around the fibres, holding them together, but defibering can be readily accomplished by appropriate mechanical means, for example, by subjecting the softened structure to the action of a double disc defibrator or a deflaking unit, machines which will physically break apart the soft fibre bundles without causing substantial injury to the fibres themselves. It is preferable after mechanical defibering except for animal feed and semi-chemical type pulps to wash the fibres with water to remove surface alkali and black liquor. Washing is preferably accomplished with a minimal amount of hot water e.g. at a temperature of about 85 to 100 C. The washing can be performed in any suitable manner. Following mechanical defibering and wasin the cellulosic pulp can be subjected to a second nitration-extraction sequence, as discussed above, or it can be used in any of the conventional ways to make cellulosic fibre webs. For pulps other than those intended for semi-chemical board or animal feed it Lji Mill be necessary to screen the pulp, to remove any fibre bundles that withstood the pulping process, which bundles can then be returned to the nitration step or further defibering action. Most commonly, the screened pulp will be supplied to the headbox of a paper machine, alone or in admixture with other types of fibres and there used to make paper products. In the previous text, substantial reference has been made to the processing of agricultural fibre residues, straw, bagasse into paper making fibres, using nitric acid as a nitrating agent, and aluminum sulphate (alum). It is a feature of this invention which sets it apart from all previous experimentation with nitric acid, that in the case of fibrous structures,such as straw, that both nitration and delignification can be accomplished in one step using a solution of neutral nitrate salts such as NaN03, NH4N-03 or KN03 alkalized to a pH of about 11 to 12, e.g. 12, with NaOH, KOH, NH40H or other suitable alkali. The ease of nitration in this case is dictated by the open structure of these fibrous materials, particularly so after shredding, coupled with the relative thin form of grassy fibrous structures compared to even 0.5mm thin wood flakes, their low lignin content of 10-15% vs, 25-358 for wood, and their low percentage of extraneous materials such as waxes and resins and other hydrophilic materials. As previously stated, previous art using nitric acid, a highly aggressive agent, has employed high usage and concentrations and lengthy time of treatment particularly for wood. The use of alum as an accelerator permits low consumption, low concentration and minimum processing time for woody fibrous structures in particular and grassy fibrous structures. The use of nitrate salts with their milder actions as opposed to the use of nitric acid plus alum is not practical for wood pulping and would not be economic for processing agricultural fibre residues, except for the possibility of combining the features of the process of this invention in providing controlled delignification, and the potential utilization of the black liquor as fertilizer, binder, sizing agent or resin extender. The process of deligniFication serves to dissociate the fibres making up the natural fibre structure freeing the lignin and providing fibres which can be formed into a web for production of paper or board. On a modified or reduced scale of delignification in a relatively dry state ( 50% moisture) the lignin can be released in situ to act as a binder for the production of building board in which the fibrous structure remains essentially intact. Delignification will also increase the digestibility of fibrous structures by herbivores, cows and sheep etc. Animal feed is being produced commercially today from straw by addition of circa 5% NaOH to the dry weight of straw in a process which makes cubes or pellets with additional food additives. Additionally, work has been done with NH40H, liquid or gaseous NH3, but this has not proven practical. Utilization of feed produced with NaOH is limited because the improvement in digestibility (food value) is low and the alkali content is high. An improvement to some 300% would be required to meet the food value of corn silage. Levels of improvement presently obtained processing straw are less than one tenth of this, and maximum utilitzation in the animals diet has not exceeded 15%. This invention provides a controlled method of delignification which increases digestibility to the point that the processed straw can comprise a minimum of 50% of the animals total diet. Mixed during processing with other food supplements, molasses, dried milk, etc a complete food can be formulated. Of equal importance is the potential of this process to be economic in small installations which further makes possible a joint production facility producing alternatively as required, animal feed and paper making fibre, providing flexibility to meet market demands local and long distance. It is characteristic of agricultural residues that they are bulky making it impossible to meet minimum weight requirements of shipping carriers resulting in high freight costs. Processing under this invention makes viable the production of a compact finished or semi-finished product of high density which greatly reduces freight and handling cost. The alternative provided by this invention in accomplishing nitration and subsequent delignification of agricultural residues extend to choices of acidic (nitric acid) or a variety of neutral nitrate salts in nitration, various levels of chemical concentration varying time and temperature for both nitration and delignification steps and a choice of alkaline chemicals (KOH, NaOH, NH4OH) to accomplish the pH level necessary for solution of the nitrated lignin Consequently a variety of inexpensive mechanical installations for processing widely varied from present conventional pulping systems becomes not only possible but preferable. Schematic diagrams of two such possibilities are submitted as part of this invention. Figure 18, an ultra simple process involving a modified hydrapulper for the production of pulp for paper which would provide an economic and viable unit for production levels as low as 10 tons per day. Figure 19 shows a completely flexible unit for the production of animal feed and for paper pulp uti lizing hot air (which could be derived from burning agricultural residues) to achieve rapidly sufficient nitration temperatures (100 C) and the drying of the end product to a specific moisture level, as necessary. The choice between the use of nitrate salts vs nitric acid would be dictated by economics: (1) Twice as much salt would be necessary to achieve the same level of delignification as with nitric acid. (2) The reduced capital investment cost using salts since stainless steel would not be required for processing equipment. (3) The desired chemical content of the black liquor is provided, e.g. sodium ion built up in the soils if used for fertilizer would not be acceptable. (4) Differences in acceptability and digestibility by various animals digestive system or the chemical requirements required for further processing -of the residual black liquor into sizing, binders or resin extenders. The ability to spray or foam the nitrating liquid on dry agricultural residues makes possible a process that is essentially dry and permits the leaching out of the nitrated lignin after the alkaline liquor is added by spray or foam (an action that can follow immediately after the acid nitrating stage), when the moist mass (35-50% moisture) is subjected to heat and pressure. Enough lignin is released to provide a hardened binding material base sufficient to bind the shredded straw when subjected to an appropriate hardening agent such as alum and the usual pressures and temperatures used in the manufacture of flake board from wood residues. In this way an inexpensive building board, water resistant and stiff can be made from straw by generating its own binding materials eliminating the use of expensive resins such as phenolics. The following examples are given as illustrations of the present invention; although it is not intended that they limit its scope in any way a wide variety of conditions and changes in variables is shown to illustrate the flexibility of the system. Example 1 Southern pine wood flakes, cut tangentially to the log circumference to a thickness of about O.6mm, are continuously fed into a screw conveyor 10, as shown in Figure 1 attached hereto. The wood has a lignin content of about 35 wt.%. The flakes are submerged and cooked in about six times their weight of a solution of 5 wt.% nitric acid to which has been added aluminum sulphate in the ratio of 1 part aluminum sulphate to 10 parts H for a period of about 15 minutes at a temperature of about 950C. The slurry of flakes in acid is then fed into a spin 11 where the flakes are drained of the acid and then washed with a minimal amount of hot water. The drained excess acid and wash water are combined, fortified with alum and concentrated nitric acid as needed, and recycled for use in the initial nitration step. The flakes are then conducted to a storage vessel 12, from which they are fed into a screw conveyor 13 containing about six times their weight of a solution of about 1.5 wt.% sodium hydroxide at a temperature of about 950C. There they are cooked for about 15 minutes. The flakes, partially defibered, are drained of the alkaline solution (in which the ligning-nitrate has dissolved) for its recycling or purging by a spin dryer 14; then are put through a defibrator 15 in order to separate the fibres partially, following which they are washed in a rotary washer 16 with a minimal amount of hot water. The dilute black liquor that is drained off in the spin dryer 14 is recycled to the first extraction step. In order to obtain a product with a higher degree of cellulose purity,i.e., bleachable pulp, not necessary for linerboard grade pulp, the nitration and digestion stem can be repeated. To do so, the semi-pulped flakes are fed into a screw conveyor 17 which contains about six times their weight of a solution of about 1.5 wt.% nitric acid to which aluminium sulphate has been added in the ratio of about I part to 10 parts HNO There the semi-pulped flakes are cooked for a period of about 15 minutes at a temperature of about 950C. The semi-pulp is then drained of excess acid and washed with a minimal amount of hot water in a spin dryer 18. The drain acid and wash water are combined and recycled to the second nitration step. The semi-pulp is then fed into a screw conveyor 19 which contains about six times its weight of a solution of about 0.8 wt.% sodium hydroxide. The semi-pulp is there cooked for about 10 minutes at a temperature of about 950C. The semi-pulp is then drained of the excess alkaline solution (black liquor) in a high density press 20, after which it is fed into a defibrator 21 for additional defibering and finally washed in a rotary washer 22 with a minimal amount of hot water. The black liquor removed from the press 20 is partially recycled to the screw conveyor 19 for reuse, with the remaining portion being sent to waste disposal. The alkaline wash water from rotary washer 22 is also recycled to the second extraction step. The pulp leaving the rotary washer 22 has been almost completely delignified and defiberized. It is then screened by conventional screening equipment 23 to remove oversized particles which have not been defiberized, which are returned to the nitration step for reprocessing. Examples 2 - 7 The process of Example 1 is repeated, using different ligno-cellulosic raw materials, as indicated in the following Table III. In each example the nitric acid contains 1 part alminum sulphate for each 10 parts of i{t'3. The same applies for examples 8 through 14. In examples 4 through 7 the ligno-cellulosic material is subjected to only one nitration-extraction sequence. Example 8 This example simulates the use of a sulphite digester producing bleachable pulp (Kappa No. 8) using pressure under conditions as follows: WOOD SPRUCE FORM FLAKES 0.5-0.6mm thick CHARGE 1.3kg (DRAY) DIGESTER STATIONARY CIRCULATING IMPREGNATION TIME 15 MINUTES IMPREGNATION TEMPERATURE 700C IMPREGNATION CHEMICAL CON CENTRATION 5% HNO COOKING TIME 15 MINUTES TIME TO COOKING TEMPERATURE 2 MINUTES COOKING TEMPERATURE 85-950C COOKING CHEMICAL 7.5% HUN03 RATIO LIQUOR TO DRY WOOD 4:1 PRESSURE 7-22 P.S.I.G. GAS OFF NONE DELIGNIFICATION STAGE 20 MINUTES DELIGNIFICATION TEMPERATURE 95-1 000C DELIGNIFICATION CHEMICAL 0.25% NaOH DELIGNIFICATION PH 10.0 - 8.0 Test results on the paper produced were as follows: Table III EMI32.1 Example <tb> Ligno- <SEP> Cellulosic <tb> Fibrous <SEP> Material <tb> Lignin <SEP> in <SEP> Fibrous <SEP> HNO3 <SEP> Stjrength, <SEP> Wt. <SEP> ratio, <SEP> Acid <SEP> NaOH <SEP> Strength, <SEP> Wt. <SEP> Ratio, <SEP> Base <SEP> HNO3 <SEP> Strength, <SEP> Wt. <SEP> Ratio, <SEP> Acid <SEP> NaOH <SEP> Strength, <SEP> Wt. <SEP> Ratio, <SEP> Base <SEP> Nitric <SEP> Acid <SEP> Alkali <tb> Material, <SEP> Wt.% <SEP> Wt.% <SEP> to <SEP> Fibrous <SEP> Material <SEP> Wt.% <SEP> to <SEP> Fibrous <SEP> Material <SEP> Wt.% <SEP> to <SEP> Fibrous <SEP> Material <SEP> wt.% <SEP> to <SEP> Fibrous <SEP> Material <tb> First <SEP> Sequence <SEP> Second <SEP> Sequence <SEP> Approximate <SEP> Total <tb> Nitric <SEP> Acid <SEP> Sodium <SEP> Hydroxide <SEP> Natric <SEP> Acid <SEP> Sodium <SEP> Hydroxide <SEP> Chemical <SEP> Usage, <tb> <SEP> Wt.% <SEP> of <SEP> Fibre <SEP> Used <tb> 2 <SEP> Spruce <SEP> (Norway) <SEP> 33 <SEP> 4,4 <SEP> 4:1 <SEP> 0.3 <SEP> 5:1 <SEP> 1.5 <SEP> 8:1 <SEP> 0.1 <SEP> 20:1 <SEP> 5.0 <SEP> 2.0 <tb> (0.5 <SEP> mm <SEP> flakes) <tb> 3 <SEP> Beech <SEP> 23 <SEP> 3.2 <SEP> 4:1 <SEP> 0.3 <SEP> 5:1 <SEP> 1.1 <SEP> 8:1 <SEP> 0.1 <SEP> 20: :1 <SEP> 4.5 <SEP> 2.0 <tb> (0.8mm <SEP> flakes) <tb> 4 <SEP> Bagasse <SEP> 19 <SEP> 1.5 <SEP> 7:1 <SEP> 0.2 <SEP> 20:1 <SEP> - <SEP> - <SEP> - <SEP> - <SEP> 4.0 <SEP> 1.8 <tb> (screened) <tb> 5 <SEP> Straw <SEP> 16 <SEP> 1.5 <SEP> 10:1 <SEP> 0.1 <SEP> 20:1 <SEP> - <SEP> - <SEP> - <SEP> - <SEP> 4.0 <SEP> 1.8 <tb> (shredded) <tb> 6 <SEP> Newsprint <SEP> waste <SEP> 25 <SEP> 1.0 <SEP> 15:1 <SEP> 0.2 <SEP> 20:1 <SEP> - <SEP> - <SEP> - <SEP> - <SEP> 8.0 <SEP> 3.0 <tb> (pulped) <tb> 7 <SEP> Bamboo <SEP> 24 <SEP> 3.0 <SEP> 5:1 <SEP> 0.2 <SEP> 20: :1 <SEP> - <SEP> - <SEP> - <SEP> - <SEP> 4.0 <SEP> 1.8 <tb> (flaked) <tb> REFINING-MINUTES 0 5 7 10 13 TEST FREENESS, OSR 21 27 39 46 52 BASIS WEIGHT, GR/M2 81.7 80.9 78.5 80.0 80.9 CALIPER, MM 0.115 0.100 0.094 0.089 0.089 APPARENT DENSITY, KG/MM3 0.710 0.809 0.835 0.899 0.909 ELONGATION, % 1.9 2.9 2.8 2.7 3.2 TENSILE STRENGTH, MTR 6660 7400 7360 7480 8240 MULLEN ABS, KPG 258 360 324 312 380 MULLEN INDEX}KPA 316 444 412 390 470 TEAR-BRECHT IMSET, MN 1118 1187 942 922 1109 Example 9 A non-pressure process using low concentration circulated chemical and longer times producing linerboard pulp, Kappa No. 37 used the following conditions: WOOD SPRUCE FLAKES, 0.5-0.6mm CHARGE 1.3 KG.DRY IMPREGNATION TIME 30 MINUTES IMPREGNATION TEMPERATURE 500C IMPREGNATION CHEMICAL 0.5% HNO SOLUTION COOKING TIME 45 MINUTES COOKING TEMPERATURE 950C COOKING CHEMICAL 1.8% HNO SOLUTION DELIGNIFICATION NaOH,pH 12,950C Example 10 A non-pressure process using a hydrapulper producing a bleachable straw pulp Kappa No. 16. WHEAT STRAW MECHANICALLY SHREDDED CHARGE 1.2 KEG., DRY IMPREGNATION TIME 15 MINUTES IMPREGNATION TEMPERATURE 500C IMPREGNATION CHEMICAL 0.5% HNO3 SOLUTION COOKING TIME 15 MINUTES COOKING TEMPERATURE 950C COOKING CHEMICAL 1.5% HNO3 SOLUTION DELIGNIFICATION NaOH, pH 12,95 C Example 11 A non-pressure process using a hydrapulper producing an animal feed grade of straw: WHEAT STRAW MECHANICALLY SHREDDED CHARGE 1.2KG.,DRY IMPREGNATION TIME 15 MINUTES IMPREGNATION TEMPERATURE 500C IMPREGNATION CHEMICAL 0.05% HNO3 SOLUTION COOKING TIME 15 MINUTES COOKING TEMPERATURE 950C COOKING CHEMICAL 0.15% HNO3 SOLUTION DELIGNIFICATION NaOH1 pH 12, 950C Example 12 A spray storage system for straw to produce pulp for packaging papers: : WHEAT STRAW MECHANICALLY SHREDDED STARTING MOISTURE 12% (BEFORE SPRAYING) FINISHING MOISTURE 35% CHEMICAL SPRAYED 3% e (100%)OF DRY FIBRE TAa HEAT APPLIED NONE STORAGE PERIOD SIX MONTHS DELIGNIFICATION NaOH, pH 12 DELIGNIFICATION TIME 10 MINUTES DELIGNIFICATION TEMPERATURE 500C Example 13 A non-pressure process using an open hydrapulper producing a semi-chemical type pulp for use as corrugating medium combined with waste fibre and straw black liquor (lignin) solids. WHEAT STRAW MECHANICALLY SHREDDED CHARGE 1. 2 KG ATRO IMPREGNATION TIME 15 MINUTES IMPREGNATION CHEMICAL 0.05% HNO3 CONC. IMPREGNATION TEMPERATURE 500C COOKING TIME 30 MINUTES COOKING CHEMICAL 0.15% HNO3 CONC. COOKING TEMPERATURE 950C DELIGNIFICATION 15 MINUTES, NaOH to pH 12-950C Board Composition DEFIBERED UNSCREENED PULP 42 MIXED WASTE FIBER 33 UNMODIFIED LIGNIN SOLIDS 25 Test Results - Produced on Paper Machine BASIS WEIGHT, GR/M2 105 MULLEN INDEX, KPA 233 ELMENDORF TEAR, MD/CD-MN 677/716 CONCORA, KG P 158 Example 14 A non-pressure process using an open hydrapulper producing a bleachable straw pulp. WHEAT STRAW MECHANICALLY SHREDDED CHARGE 1.2 KG ATRO IMPREGNATION TIME 15 MINUTES IMPREGNATION CHEMICAL 0.5% HNO3 CONC. IMPREGNATION TEMPERATURE 500C COOKING TIME 15 MINUTES COOKING CHEMICAL 1.5% HNO3 CONC. COOKING TEMPERATURE 950C DELIGNIFICATION 15 MINUTES, NaOH to pH 12 95 0C Test Results - Produced on Paper Machine BASIS WEIGHT, GR/M2 180 MULLEN INDEX, KPA 495 ELMENDORF TEAR,MD/CD- 739/848 SCHOPPER RIEGLER, DEGREES 50 KAPPA, NO. 16 Example 15 A non-pressure neutral pH-cooking process using an open hydrapulper producing a packaging paper pulp. BAGASSE SCREENED - DEPITHED COOKING TIME 15 MINUTES COOKING CHEMICAL NaNO3 - 3% SOLUTION COOKING TEMPERATURE 95 - 1000C DELIGNIFICATION 15 MINUTES, NaOH to pH 12, 9D C Electron micrographs of illustrative cellulosic fibres produced by the process of the present invention are shown in Figures 2 through 17. In each instance sodium hydroxide was used as the alkaline extraction agent and both the nitration step and the extraction step were conducted at temperatures within the range of about 95 to 1000C at atmospheric pressure. Final defibering was performed by two minutes in a blender; then the pulp was submitted to rough screening. The excellent length and structure of the fibres are apparent from the micrographs. r. Figures 2 and 3 are electron micrographs of fibres from U.S. Southern pine which had been subjected to a total nitration-extraction time (total for both steps) of 25 minutes, while Figures 4 and 5 show such pine fibres after only a 20 minute nitration-extraction time. Figures 6 and 7 are micrographs of fibres of spruce which had been subjected to a nitration-extraction time of 25 minutes. Figures 10 and 11 show wheat straw fibres after a nitrationextraction time of 25 minutes. Figures 12 and 13 are micrographs of beech fibres obtained from the present process using a combined nitration-extraction time of 27.5 minutes. Figures 14 and 15 are micrographs of bamboo fibres which had been subjected to a nitration-extraction time of 30 minutes. Figure 16 is a micrograph of fibres obtained from waste newspapers which had been subjected to a nitration-extraction time of 15 minutes. Figure 17 shows fibres from did U.S. corrugated paperboard which had been subjected to a nitration-extraction time of 15 minutes.

Claims: Claims 1. A process for treating fibrous ligno-cellulosic material to form defibered pulp material comprising the steps of submerging in or spraying of the fibrous ligno-cellulosic material with aqueous nitric acid having an HNO, concentration of about 0.15 to 9.0 wt.% and containing aluminum sulphate in an amount of about 0.8 to 1.3 parts per each 10 parts by wight of HNO3,or to alternatively use for grassy fibrous materials nitrate salts such as NaNO3 or KNO3 or NH4NO3, so as to.nitrate ligneous component of said material draining the nitrated ligno-cellulosic material from said nitric acid and thereafter defibering directly by mechanical means to obtain said pulp material, or treating the said nitrated ligno-cellulosic material with an alkaline extraction liquor so as to dissolve ligneous component out of t.he material and separating the resultant cellulosic puir from the lignin containing extraction liquor as well as Op+'ionally, recombining a part or all of the ligneous cDm- ponent of the lignin containing extraction liquor with the cellulosic pulp. 2. The process of claim 1 wherein the fibrous ligno-cellulosic material is submerged in or treated by recycling in nitrating solution at a temperature of about 85 to 1100C, preferably 85 to 1000C; in particular wherein both the submersion step and the cooking step are conducted under approximately atmospheric pressure conditions and the HNO3 concentration in the nitrating step is about 0.3 to 5.5 percent by weight; in particular wherein the fibrous lignocellulosic material is submerged or subjected to treatment by recycling in the nitrating solution for about 5 to 30 minutes; in particular wherein the ligno-cellulosic material is woody material, grassy material, or waste paper containing mechanical pulp or semi-chemical fibres; in particular wherein the submersion step and the cooking step are conducted under atmospheric pressure conditions and the fibrous ligno-cellulosic material is submerged in or treated by the nitrating solution for about 10 to 20 minutes; in particular wherein pressures of 15 to 35 p.s.i.q. are used in the nitrating process holding temperatures from 85 to 1100C, preferably 85 to 100 C; in particular wherein pressures of 100 to 150 p.s.i.g. are used in the nitrating process holding temperatures between 85 and 11 00C, preferably 85 and 1000C. 3. The process of claim 1 or 2, wherein the alkaline extraction liquor is an aqueous solution of sodium hydroi- de, potassium hydroxide, or ammonium hydroxide containing about 0.1 to 0.5 wt.% NaOH, KOH or NH40H; in particular wherein the alkaline extraction liquor is an aqueous solution of sodium hydroxide containing about 0.1 to 0.5 wt. NaOH, the fibrous ligno-cellulosic material is submerged in the nitrating solution at a temperature of about 90 to 950C and the nitrated ligno-cellulosic material has its binding material removed; in particular wherein the alkali ne extraction liquor is an aqueous solution of potassium hydroxide, the lignin containing extraction liquor is mixed with phosphoric acid to precipitate the ligneous component out of the solution and the ligneous componenr is separated from its acidic mother liquor to obtain a flocculated concentrated ligneous material; in particular wherein the nitrated ligno-cellulosic material is treated in the alkaline extraction liquor at a temperature of about 75 to 1000C for grassy and woody fibrous structures; in particular wherein the nitrated ligno-cellulosic material is treated in the alkaline extraction liquor of about 40 to 500C for grassy fibrous structures. 4. The process of any of the preceeding claims wherein the ligneous component is obtained by mixing the lignin containing extraction liquor with acidic reagent to cause ligneous component to precipitate out of solution, following which said precipitated ligneous component is separated from its acidic mother liquor; in particular wherein the acidic reagent is nitric acid, phosporic acid or aluminum sulphate; in particular wherein the acidic reagent is nitric acid and the acidic mother liquor is used as a source of nitric acid for the precipitation step; in particular wherein the precipitated Ligneous component prior to be mixed with the cellulosic pulp, is redissolved in water with sufficient alkaline reagent to render the ligneous component soluble in water; in particular wherein the alkaline reagent is sodium hydroxide, potassium hydroxide or ammonium hydroxide; in particular wherein the flocculated concentrated ligneous material, optionally in combination with a deliquescence inhibiting amount of diatomaceous earth is added to quick draining soils to promote chemical retention and hygroscopic properties. 5. The process of any of the preceeding claims wherein the lignin containing extraction liquor or the redissolved ligneous component is combined with neutralized urea and fortified rosin size to extend rosin size; in particular wherein the lignin-containing extraction liquor or the precipitated ligneous component or the redissolved ligneous component is combined with starch to produce water repelie-.- cy or sizing; in particular wherein the lignin-conianning extraction liquor or the redissolved ligneous component is mixed with resins such as melamine resin or phenolic resin to act as an extender; in particular wherein the nitrated lignin can be solubilized with an alkaline solution at low temperatures of 15 to 500C. 6. The process of any of the preceeding claims wherein the separated ligneous component is combined in precipitated (concentrated) or non-precipitated form with paper:ak fibre. 7. The process of any of the preceeding claims wherein the recombination of the ligneous component with said cellulosic pulp is performed by applying a foam of the precipitated or non-precipitated ligneous component onto a web of the cellulosic pulp at the size press or wet presses; in particular wherein the recombination of the ligneous component with said cellulosic pulp is performed by adding the lignin-containing extraction liquor to the slurry of the cellulosic pulp and precipitating the ligneous component by acidification. 8. The process of any of the preceeding claims wherein the nitrating solution can be sprayed on air dry grassy agricultural residues and nitrates the said residue lignin components duriri storage without use of heat permitting delignification and defibering at a later date; in parti cular wherein the nitrating solution can be sprayed or foamed on air dry agricultural residues and followed immediately with sprayed or foamed alkaline liquor which releases a ligneous binder "in situ" when the moist mass is subjected to heat and pressure. 9.The process of any of the preceeding claims wherein the digestibility of agricultural residues for animals is improved. 10. A fertilizer composition comprising the ligneous material of claim 4 in a mixture with a deliquescence inhibiting amount of diatomaceous earth.

Inventors: PRIOR, ERIC S.
Applicants: PRIOR, ERIC S.
Application year: 1978
Main classification: D21C3
IPC codes: A23K1, D21C3, C05F7, D21H17