FI97977C - Method for making a cellulosic product - Google Patents

Description

- 97977

Method for making a cellulosic product

The invention relates to a process for the production of a cellulose product, such as bleached cellulose, cellulose I having a high alpha-cellulose content, cellulose II, i.e. the so-called to prepare mercerized cellulose or cellulose acetate, which may be cellulose acetate of high purity and reactivity. The essential characteristics of the method are set out in the appended claim 1.

10

Prior to the invention of the process of separating lignin from cellulose and hemicellulose, there was no known, economically viable process for purely cleaving crosslinks between chemically reactive hemicellulose ligin and the xylan component with non-reactive cellulose in the cellulose.

20 In this specification, "lignocellulosic material" includes plant materials such as bagasse, rice husk, wheat husk, oat husk, barley husk and various species of wood, especially deciduous trees. The lignocellulosic material consists of three main chemical components, lignin-25, hemicellulose and cellulose in the following approximate proportions, plus ash, oils and trace elements:

Deciduous trees: lignin 21% 30 hemicellulose 27% cellulose 50%

Annual plant material (stem, bagasse, etc.): lignin 15% hemicellulose 35% 35 cellulose 48%

Cellulose and hemicellulose are both carbohydrates. Cellulose is nature's most common organic chemical, hemicellulose is the second most common and lignin is the third most common. Cellulose consists of six-carbon (glucose) blind molecules. The xylan component (about 70%) of the heme part of annual plants and leafy plants is an amorphous carbohydrate olymer consisting mainly of five-carbon (xylose) sugar molecules. Lignin is a complex amorphous hydrocarbon molecule composed of many chemical components present in oil and gas, such as phenol, benzene, propane. The function of these three materials in the composite complex is as follows: 10 - The core of the liquid cell fiber consists mainly of cellulose. Cellulose is the ranko and structural bone part of the fibrous structure. It occurs as bundles of crystalline fibrils, which are hinged at about ioka 300. Every glucose molecule and iotka support the tissue of a tree or plant.

15 - The hemellin and lignin are cross-linked to form a matrix which surrounds the web and holds the structure together in the same manner as in the resin glass fiber composite.

Figure 3 shows a single particle fiber, in which the dotted area 46 is referred to as the central flake. The central lamella 46 is an adhesive that holds adjacent fibers together. It contains saturated lignin and xylan in a ratio of about 70:30. The primary wall 48 is an outer sheath around the fiber optic in much the same way as a sheath in a telephone underground cable. It contains approximately equal amounts of 25 μl of lignin and xylan and a small amount of cellulose, which provides structural bone. The fiber bundle or core 50. 51 and 52 consists of closely bound sei uiosafi glasses. Each fibril is bound to adjacent fibrils by the addition of lignin and xylan. The ratio of lignin to xylan in the fiber core is 30:70, but due to the large amount of lignin compared to the middle lamella and the primary wall, 70% of it is present in the fiber bundle. The fibrils in the fiber bundle form 35 slight spirals along the length of the fiber and each fibril is hinged by an amorphous region present at approximately every 300 molecular weight molecules in the fibril. It is this hinge that is the weakest link in the fibril and is the point at which the fibrils break and change, so that the k f of i br i 1J does not appear in the 3 97977 flash process when performed in accordance with the teachings of Canadian Patent 1,217,765. Finally, the ducts 54 are a hollow area in the center of the fiber bundle, where liquids pass through the iiqnosel1 float composite, feeding the plant.

5 It is this 1 ionin / hemicellulose matrix surrounding the cellulose that provides natural protection against microbial attack. It also makes the material water-resistant and inaccessible to chemical reagents.

Applying the passages of Canadian patents 1,217,765 and 10,111,376 has solved a problem that has plagued scientists and engineers for more than a century, namely how to break the cross-bridges between molecules of lioanine and hemisphere without causing substantial degradation of either of these chemicals. Once the intermolecular crosslinks in the liq-15 nosellulose material are severed, it is relatively simple to separate the material into its three main chemical components (liquin, xylan, and cellulose) using mild organic solvents or weak base solutions.

The apparatus used to carry out this process is shown in Figure 1, in which 1 there is a pressure vessel with an outlet pipe 2 with a valve at the bottom and a charge valve 3 at the top. 4 is a steam supply valve. 5 and 6 are thermocouples. iotka is designed to measure the temperature of the material in the pressure vessel 25. 9 is a thermopard in a steam supply pipe which measures the temperature of the supply steam. 10 is a pressure gauge that measures the pressure of the supply flow. 7 is a condensate trap containing water condensate formed during the heating period of the material when the hot steam is mixed with the other flotation material of the fire. When the material absorbs heat from the steam, condensate is formed which flows into the bottom of the cooking vessel and into the condensate trap 7. 8 is an optional nozzle which can provide various orifice structures to provide greater or lesser abrasion under explosive pressure depending on the final application of the processed material. 11 is a mechanically milled glucocellulose feedstock.

Briefly, the steam blasting process places the entire liq-nosel 1 .mu.l of material 1 in a softened state (at a settling temperature of cellulose 97977 4) by heating the material to 234 ° C, whereupon its pressure is explosively reduced through a narrow orifice. The enormous shear forces present in the flare depolymerize the macromolecules into smaller units mechanically. Cellulose is cleaved from its amorphous hinges, which are the weakest links in the cellulose chain. This swells to cellulose, which has a DP value between 200 and 500. If it is desired to obtain a higher DP value, the portion feed material may be processed in accordance with the teachings of Canadian Patent 10,111,375. The cross between the xylan component of hemicellulose and lianine are broken and Iranin is released from the carbohydrate.

Although conventional pulp pre-filters and filters can be used, the preferred method of solvent extraction of the separated material takes place in a column (see Figure 2).

ioka contains particulate material. Various solvents such as water, alcohol and base are poured through the material as a plug stream in the extreme barrier of water, alcohol and base or water and base. After alkali extraction, the high purity screen material aged 20 can be bleached in conventional bleaching systems or is preferably bleached by passing a bleaching agent, usually buffered hypochlorite, through the material while still in the column.

The typical purity of this bleached residual cellulose material 1 in aspen wood shows a polysaccharide content of more than 98%, of which about 3.5% is xylose, 0.4% is mannose and more than 96% is alucose. In addition, the material may contain about 1.3% vegetable oil and 0.1-0.5% ash depending on the mineral content of the water used in the extraction.

Figure 2 is a sketch of a column used to dissolve the various detached chemical components of the explosively processed particulate material and thus achieve their first stage separation. Column 1 is a tube open at both ends. The tube can have almost any geometric cross-sectional shape from round to triangular and rectangular ine. The column 1 is loaded with a loosely packed, processed liquid cellulosic material 6. At the bottom of the column is a filter 2, the duct is dense enough to prevent the processed material from passing through it, but still coarse enough to allow the solute-containing eluent to flow through so quickly. The column is mounted on a tapered base 3 to introduce the eluent into the neck, which has an outlet pipe 4 with a valve for adjusting the flow rate of the column if necessary. Temperature, pH, flow rate and other sensors are located at the bottom of the column 10 to provide control information to the column command and control system. The dense screen 5 is screened to the top of the column to evenly disperse the feed solvent over the material at the top of the column. This prevents the material in the column from being unduly compressed.

Solvents such as water 7, then alcohol 8, then dilute base 9, and then bleach, or any combination thereof, can then be fed to the top of the column and their eluents, which contain solids soluble in that solvent, flow through the processed lycnocellulose material. recovered to obtain the product from the bottom of the column as water-soluble 11, alcohol-soluble 12, base-soluble 13 and bleach-soluble substances 14 or even a combination thereof. The column can be used for various treatment processes, such as acid or alcohol resistance, when it is desired to obtain a uniform treatment of the residual material, and in particular when it is desired to crush one liquid over another.

The result is a high crystallinity, high purity, remarkably reactive, low polymerized-grade (DP) but narrow DP-Backing product, which can then be bleached with various reagents for high value-added end products such as screening. . carboxymethylcellulose, cellulose nitrate, high alpha-cellulose, beta-cellulose, mercerized cellulose and microcrystalline cellulose. For example, after bleaching, the bleaching agent is sprayed with water or alcohol to stop the bleaching reaction. Alcohol would only be used if the cellulose was to be dried before further processing. Alcohol reduces the thermal energy required to dry the cellulose and maintains the high reactivity of the cellulose by preventing the formation of hydrogen bonds during the drying cycle. The cellulose can then be aged into two ages, one with a high alpha-cellulose (DP above 100) and the other with a high beta-cellulose (DP below 100) (see Figure 4).

Figure 4 shows two curves of the degree of cellulose polymerization (DP) 10. Curve 1 is the cellulose obtained by the flash process 11a, prepared in accordance with the teachings of Canadian Patent 1,217,765. The curve was measured by acetalizing the bleached cellulose and then measuring the DP orophil of the cellular triacetate by high pressure liquid chromatography. It is assumed that the DP of cellulose decreases only slightly during acetylation. Findings from many samples have yielded remarkably consistent data, which would suggest that the assumption is substantially correct. The fact that the cellulose tibrils are mechanically broken at the hinge point in the flash process.

20 explains a very high but narrow aging peak, the center of which is at DP 280.

Curve 2 is a conventional DP curve of leaching mass. The curve was taken from the 25 textbook descriptions of the Classical DP curve of a conventional leaching compound. The wide DP distribution curve can be explained by the fact that the decrease in DP in a leachate pulp mill is a chemical process that acts on the particulate chain in a random manner.

30 DP region 3 is an arbitrary but ancient definition of beta-selululose le (DP less than 100). DP region 4 is the classical definition of alpha-cellulose (DP uli 100). The beta-sel1 float is susceptible to excessive swelling during base treatments.

It often forms an oeel, which gives the cellulose poor filtration properties. Cellulose beta-iae is easier to solubilize than ai fa-sel1 uioosaiae.

If high mercerized alpha-cellulose II-containing iaett is required. The beta-sel1 portion can be made and then extracted by filtration using a 3 molar solution of potassium hydroxide (see Table 1). Potassium hydroxide is used to ensure good filterability properties. This extraction yields a soluble beta-sel1 leachate. ioka is 5 16-19% of the initial weight of bleached cellulose on a dry basis. The alpha-cellulose content of the residual cellulose II is more than 90%. Ai concentrations of 95% can be achieved in the second extraction step. DP with a high mercerized alpha-cellulose has a remarkably narrow aging, with a peak 10 between DP 200 and DP 500. Both alpha and beta-cellulose are in mercerized (cellulose II) form and are crystalline, highly absorbent. and reactive. If it is desired to obtain a non-mercerized alpha crystalline form of cellulose which forms hydrogen bonds upon drying, the α1 / beta separation 15 should be made with a 2 molar solution of the base solvent (see Table 1) to extract the beta-acid. Again, potassium hydroxide is preferred to prevent excessive swelling and thus to ensure good filterability properties. The lower base concentration performs efficient beta-lactic separation, but does not mercerize cellulose I to cellulose II. The water-washed high-alpha-containing cellulose I end product easily forms hydrogen bonds upon drying for pharmaceutical and food applications.

Table 1. - KOH extraction at 20 ° C 25 KOH concentration Experiment 1 Experiment 2 at 20 ° C beta yield beta yield 1 molar 8% 8% 2 molar 16% 15% 2,5 molar 19% 19.2% 30 3-molar 17% 17% 4-molar 15% 14.6% 5-molar 15% 14.7% Thus, the use of potassium hydroxide achieves two industrially useful results compared to the almost universally used sodium hydroxide treatment. First, it prevents excessive swelling and thus guarantees good filterability properties. Second, the separation of potassium hydroxide (2.5 molar) ai fa-ia bet a sei 1uose oakose 8 97977 coincides quite exactly with the optimum concentration of potassium hydroxide required to achieve mercerization. Thus, alpha / beta separations can be effectively achieved to increase the alpha-cellulose content of the final product by selecting either mercerized or non-mercerized cellulose by changing the KOH solvent concentration from 3 molar to 2 molar. In this specification, the separation of alpha and beta cellulose and the simultaneous mercerization of bleached fumed blast cellulose are performed at room temperature (20 ° C). The contact time in potassium hydroxide is short, usually about 7 minutes. The combination of optimal KOH-solvent extraction and mercerization efficiency is a unique phenomenon, which is particularly well suited for blast process cellulose, which has a remarkably low hemisululose but high beta-sel1 content. In the pulp leaching industry, sodium hydroxide is used to dissolve beta-cellulose and hemicellulose propellants from conventional leaching pulp at a concentration of 10% and a temperature of 20-25 ° C. Mercerization conditions using sodium hydroxide to produce aliquot (mercerized) cellulose require 17-19% NaOH concentrations at elevated temperatures between 35-58 ° C. Fiber morpholar factors, the content of fines, the homogeneity of the slurry, the consistency and temperature of the slurry are all important factors that affect the quality of the portion obtained from conventional solvent pulp sources. However, with the exception of the viscose process, mercerization must be avoided because the reactivity of conventional dried mercerized pulp fiber is low and can therefore cause difficulties in the subsequent acylation of the pulp. In addition, the hemicellulose content of Merse-30 alkali becomes quite high (15-35 q / l) in the case of sodium hydroxide treatment. This strong alkali hemicellulose contamination erodes its reuse as the contaminants accumulate and contaminate the next 35 cartridges. Blast process cellulose is less susceptible to these problems because its hemispheric content after the bleaching cycle is less than 2% compared to a conventional leaching pulp of hemi sei 1 ui, which varies up to 10% and is rarely

II

9 97977 less than five percent. Potassium hydroxide is recovered from the solubilized beta-reverse reverse osmosis and beta-cellulose is recovered by mixing cellulose by adding water or acid to the beta concentrate, followed by filtration.

Cellulose triacetate is one of the most important organic acid esters of cellulose. It is used for the spinning of fibers for the textile industry and as fibers for the manufacture of cigarette filters. Sei 1 ui osatriacetate1 can 1a has excellent brightness for transparent packages, film shots, film films and magnetic tapes. It is used in injection molding plastic applications. Sei 1 osioate triacetate is often hydrolyzed to a lower degree of substitution to produce sei osiosatiacetate, commonly referred to as cellulose acetate, and is used in a wide variety of other applications.

Normally, cellulose triacetate is prepared from a very pure (over 95% fence cellulose) pulp of acetylation. It is common practice to flocculate the pulp in a milling unit where it is shredded to increase its surface area for acetylation. The pulp is then pretreated with vinegar and water at a pulp concentration of about 6% for about an hour at 25-40 ° C to ensure that it is completely wetted.

Large amounts of acetic acid are then used in the solvent exchange process to reduce the water present to very low concentrations, as the acetic anhydride used in the acetylation is converted to acetic acid in the presence of water.

Thereafter, the active step is carried out in a mixture of acetic acid and cellulose by adding sulfuric acid in an amount of 1-2% by weight of the cellulose. The activation time is 1-2 hours. This step lowers the average DP value of the cellulose to the desired DP value of the final product. Average DP levels between 35 and 300 are the most common. After the activation step, the cellulose is transferred to an acetylation reactor and acetic acid anhydride is added to acetylate the cellulose to a final product of cellulose acetate.

10 97977

Prior to the addition of sulfuric acid in the activation step, large amounts of acetic acid are used to reduce the amount of water present in the solvent exchange process to very low levels because acetic anhydride reacts with water to form acetic acid. This reaction is exothermic and can result in unacceptably high temperatures in the reactor if water is too much present, in addition to consuming acetic anhydride, which is expensive. In this case, too, a cooling cycle is usually used to prevent overheating of acetic acid, acetic acid anhydride and acid catalyst during acetylation, since high temperatures in the presence of sulfuric acid cause accelerated and uncontrolled deo-1 polymerization of cellulose. The temperature is thus maintained at 50 ° C. When the cellulose is completely dissolved to a clear solution, the acetylation is stopped by adding the solution to water to convert the acetic anhydride to acetic acid, which is then recovered. This application was made by an age-improved process for the preparation of ethyl acetate and triacetate which does not require any grinding unit or long activation processes. All that is required is that the cellulose obtained from the flash process be moistened with water.

Until now, my cellulose triacetate has not been purchased. It is necessary to buy a very pure acetate grade solvent mass as a starting material. Due to the high purity requirements, cellulose produced from hair by conventional leaching pulp processes has been expensive. As discussed above, the pulp's further processing to standardize and otherwise prepare it for acetification has been expensive due to costly yield losses and the use of large amounts of acetic acid and recovery from water in the process.

In nature, the cellulosic material consists of a plurality of fibrils consisting of crystalline cellulose with a paracrystalline or amorphous region hinged together. This study has shown that the hinge is a weak link in the pulp chain. When the pre-blast process lv preconception is implemented in accordance with Canadian Patent 1,217,765

II

11 97977, it breaks substantially all of the hinges in the cellulose, producing a highly crystalline cellulose product having a significantly narrow DP distribution, with the hip peak at about DP 280 (see Figure 4). DP 280 is close to ideal for conversion to cellulose triacetate. In fibers, plastics and inexpensive mechanical properties such as tensile strength, impact strength, elongation and bending (new gear), the polymerization (DP) and DP retraction are associated with the degree of polymerization. The mechanical properties 10 are significantly improved and leveled off when the DP of the cellular triacetate is increased from 200 to 250. If higher DP cellulose is required for a particular application, the blasting process can be performed according to the teachings of Canadian Patent 1,141,376.

In one embodiment of this specification, cellulose triacetate can be prepared from highly crystalline cellulose in a column at the end of bleaching without separating the α / β / beta or mercerizing the cellulose by bleaching the bleach in the column with a plug stream and then stirring with water. In the case of a 150 cm moth luck. less than one column volume is sufficient to displace substantially all of the water in the cellulose and extract all of the remaining vegetable oil. The conventional triacetate process contaminates the water with several solvent changes in an endless dilution process. In this case, even if acetic acid is recovered, massive amounts of acetic acid, which are normally associated with water, will incur high art costs. which significantly increases the cost of the product. In this improved embodiment, the cellulose is highly reactive and has a DP that is optimal for the final triacetate product. Thus, the activation step, which lowers the DP value of the pulp, is avoided. Saturated cellulose 35 of acetic acid. 11a is transferred directly to an acetylation reactor containing additional acetic acid as a solvent for ethyl acetate and covers for the acetic anhydride required for the acetylation reaction. i n.

12 97977

In the present study, perchloric acid with less than 1% anhydride content has been used as the preferred catalyst. Sulfuric acid has been deliberately avoided because it was found that sulfuric acid decomposed the cellulose into a significantly lower DP and a wider DP distribution. If a low DP end product with a broad DP distribution is desired in the final product, sulfuric acid should be used. If substantially no reduction in DP is desired, perchloric acid is a potent catalyst for use with the cellulose produced by the blasting process. When replacing water with glacial acetic acid by passing the plug plug operation of the column, the water content is negligible and results in only a temperature increase of about 10 ° C in the reactor, including a heat generated by the acetylation reaction of about? 0 ° C. oil temperature.i 1 year. This very slight rise in temperature indicates the complete displacement of water by glacial acetic acid 1 i uot i nvai bt. at the stage using a column. This also means that the use of acetic anhydride can be kept to the minimum required for acetification, since it is not consumed in the conversion to acetic acid by the action of residual water in the acetic acid solvent. In less than 20 minutes in the reactor, the cellulose is sufficiently acetylated to dissolve into a clear solution. After a further less than 15 minutes to ensure complete substitution of acetic acid, the dissolved acetylcellulose is filtered to remove insoluble impurities and precipitated in water and then further washed to ensure complete recovery of the residual acetic anhydride to acetic acid, after which the acetic acid is taken up. The amount of precipitation method can be varied to produce either 30 powders or flakes.

SeiJui parts made with this new process. The degree of substitution is at least 3. Consequently, and. also due to its remarkably narrow DP distribution (cf. Fig. 35 41 it dissolves very rapidly and completely in dichloromethane for casting or spinning without the need for alcohol to increase the inherent solvent power of dichloroacetate. Component of solvent a 1 increases 1 i. Avoiding solvent recovery simplifies solvent recovery). , since the evaporation temperature of dichloromethane is 97 ° C and is only 40 ° C at atmospheric pressure and is hydrophobic.

In another embodiment of the present invention, a high purity, high alpha content form of cellulose triacetate can be prepared from either high fence mercerized cellulose or high alpha non-mercerized cellulose by reacting the bleached cellulose from the column with an aqueous wash. with. In either case, the potassium hydroxide dissolves the beta-cellulose agent, which is recovered by filtration, preferably under pressure, to obtain the maximum amount of the potassium hydroxide solvent containing the beta-cellulose moiety. Potassium hydroxide 15 is then recovered in a reusable form by separating the solvent from the beta fraction by reverse osmosis 11a. The mercerized beta-cellulose cake is then recovered by blending and filtration. The high alpha mercerized or non-mercerized cellulose wafers are, after filtration, exchanged with water and then returned to the column to drain. The water in the cellulose is then passed through a column of vinegar. The cellulose saturated with ethyl acetate is then transferred to an acetylation reactor containing additional acetic acid as a solvent for ethyl acetate and the acetic anhydride required for the acetylation reaction plus a catalyst. The acetylation procedure described above for bleached cellulose only is followed to acetylate highly mercerized or non-mercerized, high alpha cellulose, i.e., oliosatriacetate. Acetylated, mercerized cellulose produces a finely divided, pure, highly reactive end product in the form of wood. The significantly increased reactivity of mercerized cellulose compared to non-mercerized cellulose is shown by it. that complete dissolution in normal acetic acid, et.ik kabappoanhvdr.i di -35 ia perchloric acid concentration in occurs in about two mi.nuu-t. i s s a.

In another embodiment of the present invention, drying of the cellulose between its separation and setting 14 97977 is provided. In this case, only bleached cellulose or mercerized or non-mercerized high fence cellulose containing water passed after bleaching to bleach the residual potassium hydroxide after beta extraction can be fermented in a column with an alcohol selected from ethanol, methanol or isopropanol. Both alcohol and acetic acid significantly reduce heat, which is required to dry the material, and the cellulose retains a small percentage of alcohol or acetic acid, which prevents the formation of hydrogen bonds during the drying cycle and thus maintains the reactivity of the cellulosic material. Only in the case of bleached cellulose can alcohol be used to svr etch the bleach from the liquid / liquid-15 exchange of bleach with water. In the case of cellulose impregnated with acetic acid, the acetic acid aged after drying not only preserves the reactivity of the cellulose by preventing the formation of hydrogen bonds, but also prevents the restoration of color. The dried cell product is reactivated with water and returned to the column to run before use in vv or other value-added conversions or applications.

Claims (2)

15 97977 1. A process for the production of a cellulose product such as bleached cellulose, high alpha-cellulose I cellulose I, cellulose II, i.e. so-called for the preparation of mercerized cellulose 5 or cellulose acetate, which may be cellulose acetate of high purity and reactivity, characterized in that (a) the dissociated lignocellulosic material is extracted with vanillin, syringaldehyde, furfuraldehyde, protein, acetic acid to remove xylose monomers and oligomers, followed by (b) extracting the remaining water-insoluble material with an alcohol selected from isopropanol, ethanol and methanol to remove vegetable oil and lignin, followed by treatment with a dilute base solution of less than 2%; selected from sodium hydroxide, lithium hydroxide and potassium hydroxide, high polymerization xylose oligomers and lignin / furfuraldehyde copolymer, i.e. to dissolve and extract the pseudolignin, or to extract the water-insoluble material directly with a dilute base of less than 2% selected from sodium hydroxide, lithium hydroxide and potassium hydroxide, followed by (c) bleaching with a water, alcohol and / or base extract, , the concentration of which is less than 2%, after which the solvent is changed with water to terminate the bleaching effect, and optionally (e) the solvent is changed with acetic acid to prevent the formation of hydrogen bonds and color recovery during drying, after which 97977 (f) is dried with acetic acid. cellulose to recover the acetic acid by evaporation, or alternatively 5 (g) the solvent is bleached with alcohol to terminate the bleaching effect and prevent the formation of hydrogen bonds during drying, followed by (h) drying with alcohol. to recover alcohol-10 by evaporation, and possibly to prepare high alpha-cellulose cellulose I by separating beta-cellulose from bleached cellulose, 15 (a) transfer the bleached cellulose at a temperature of about 20 ° C to a solution of potassium hydroxide in dilute cellulose results in a base strength of about 2 molar, after which the cellulose is thoroughly mixed with the base solution to dissolve the beta-cellulose component, after which (c) the potassium hydroxide solvent containing the beta-cellulose fraction is separated by filtration, and (d) the solvent is changed to high alpha-cellulose content residual potassium hydroxide solution in water, or to prepare cellulose II, i.e. mercerized cellulose, from bleached cellulose by separating beta-cellulose therefrom to increase the alpha-cellulose content of the product, 1 (a) is transferred bleached cellulose at a temperature of about 20 ° C to a potassium hydroxide solution which, when diluted with residual water in the cellulose, results in a base strength of about 3 molar, after which 97977 (b) thoroughly mixing the cellulose with a base solution to mercerize the cellulose and simultaneously dissolve the beta-cellulose component; then 5 (c) separating the potassium hydroxide solvent containing the beta-cellulose fraction by filtration, then (d) exchanging the solvent for a solution of 10 residual potassium hydroxide in the mercerized cellulose II product having a high alpha-cellulose content with water, or acetylating the bleached cellulose cellulose in a column with glacial acetic acid, after which (b) the cellulose saturated with glacial acetic acid is transferred to an acetylation reactor containing additional glacial acetic acid acting as a solvent for cellulose triacetate, acetic anhydride and catalyst. the cellulose is allowed to dissolve into a clear solution, after which (c) the acetylation is expected to be complete, which takes less than 15 minutes, and then the clear cellulose acetate solution is filtered to remove any insoluble impurities, after which (d) precipitated cellulose triacetate in water followed by cellulose triacetate further precipitated in water to ensure that any excess acetic anhydride is converted to acetic acid, followed by (e) recovering acetic acid by solvent extraction or evaporation to form a substantially pure and reactive cellulose extract; either mercerized or non-mercerized cellulose 5 (a) slurry the dried cellulose with water and place it on a column to drain, (b) displace the water obtained from the bleached non-mercerized or mercerized cellulose in a column with glacial acetic acid, wherein then (c) transferring the cellulose saturated with glacial acetic acid to a acetylation reactor containing additional glacial acetic acid as a solvent for cellulose triacetate and acetic anhydride and catalyst, and allowing the cellulose to dissolve into a clear solution, after which (d) acetylation is expected to proceed, which takes less than 15 minutes, after which the clear cellulose triacetate solution is filtered to remove any insoluble impurities, after which (e) the cellulose triacetate solution is precipitated in water to ensure that any excess acetic anhydride is converted to acetic acid, followed by (f) or by evaporation. Process according to Claim 1, characterized in that the bleaching agent is a buffered hypochlorite bleaching agent. l9 97977 1. For use in the manufacture of cellulose products from cellulose, in which cellulose I is mediated by alpha-cellulose, and in cellulose II, sk. merceric cellulose 5 or cellulose acetate with the presence of cellulose acetate with reactivity, reacting with (a) the dissociated lignocellulosic material of extra-whey with water from glossy vanillin, syringaldehyde, furfuraldehyde, protein, furfuraldehyde, and xylosmonomers and oligomers, of which (b) is quaternary in the presence of a material of extra alcohol with alcohol groups of isopropanol, ethanol and 15 methanol for the production of vegetable oil and lignin, on top of bleaching with mild, all 2 % to caustic on the part of the Group of sodium hydroxide, lithium hydroxide or potassium hydroxide for the recovery and extraction of xylosoligomers with higher polymerization values and up to 20 nin / furfuraldehyde polymer, with the addition of pseudo-lignin, direkt med mild, mindre än 2än-up caustik vald frän Gruppen av natriumhydroxid, lithiumhydroxid eller potassium hydroxide, 25 (c) is a dissociated lignocellulosic material in the form of a cotton wool, alcohol and / or caustic blacks having a concentration in the form of a concentration of 2%, 30 (d) bleaching means in the form of a water wool eventually (e) the cellulosic substance of the mixture is obtained for the purposes of the conversion and conversion of fat under the conditions of paragraph 35 (f) -sluta blekningsverkan and to enable the hindra under vätebindning by drying, after which 5 (h) Cellulosa som impregnerats with alkohol is dried for ätervinnande through Evaporation of the alcohols, Science möjligt-vis for beredning of a Cellulosa I with hög alfacellulosahalt, 10 through the Separation of betacellulosan IFRA blekta Cellulosos, (a) den blekta cellulosan överförs account in the case of potassium hydroxide, at a temperature of about 20 ° C, for a period of 15 days with a quaternary mixture of caustic soda and caustic soda (c) a potassium hydroxide solution selected from the group consisting of beta-cellulosic fractions separated by genomic filtration; , the separation of betacell-30 from the alpha-cellulose sawdust and products, (a) denoting the cellulose in the form of potassium hydroxide, at a temperature of about 20 ° C, with the aid of a quaternary cellulose, kaus-35 tikstyrka i omrädet av 3 molar, varefter li 97977 (b) cellulose omsorgsfullt blandas in In a caustic process for merceric cellulose and beta-cellulosic components of the same, 5 (c) of potassium hydroxide solubilizers are used in the preparation of a beta-cellulosic fraction for the production of a commercially available mercury-containing mercury hydroxide compound. , or for the acetylation of the cellulose triacetate to the cellulose triacetate 15 (a) the water content of the cellulose triacetate in the column of the cellulose tracetate 15, (a) the water content of the cellulose triacetate to the cellulose triacetate 15 or a solution of cellulose acetic acid, acetic anhydride and a catalyst in the form of a cellulose solution, such as (c) after a period of 15 minutes at least 25 minutes after filtration of the acetylation of the cellulose. vlägsnande av alla olösta föroreningar, varefter (d) cellulosatriacetaten falls ut i vatten, varefter den 30 utfällda cellulosatriacetaten vattentvättas ytterligare för att säkerstts att ali överskottsättiksyraanhydrid omvandlas account ättiks in the form of cellulose tritates in the form of cellulosic cells, the cellulose antimicrobials of which are present in the cell, 5 (a) in the form of cellulose cells in a cell with water and in place and in a column of the cell, if the merceric cellulose is in a column with a cell reactor, the light refter (c) the cell is then impregnated with a cellulose reactor in an acetylation reactor without the addition of a cellulose feeder to the cellulose matrix, and then the acetic acid hydride these accounts and clarifications, (d) after a period of at least 15 minutes, for which the acetylation of the cellulose is significantly reduced, the filters of the cellulose assay att hela överskottet av ättiksyraanhydrid om- vandlas account ättiksyra, varefter (f) ättiksyran ätervinnes genom vätskeextraktion eller avdunstning. 30 2. A method according to claim 1, which comprises the use of a bleaching agent and a buffered hypochlorite bleaching agent.