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US2558054A - Purification of cellulosic materials - Google Patents

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US2558054A
US2558054A US81742A US8174249A US2558054A US 2558054 A US2558054 A US 2558054A US 81742 A US81742 A US 81742A US 8174249 A US8174249 A US 8174249A US 2558054 A US2558054 A US 2558054A
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pulp
weight
mixture
temperature
cellulosic materials
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Mervin E Martin
Daniel L Sherk
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Celanese Corp
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/08—Removal of fats, resins, pitch or waxes; Chemical or physical purification, i.e. refining, of crude cellulose by removing non-cellulosic contaminants, optionally combined with bleaching
    • D21C9/083—Removal of fats, resins, pitch or waxes; Chemical or physical purification, i.e. refining, of crude cellulose by removing non-cellulosic contaminants, optionally combined with bleaching with inorganic compounds

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  • This invention relates to the purification of cellulosic materials, and relates more particularly to the purification of wood pulps.
  • Cellulosic materials such as wood pulps that are to be employed for the production of cellulose derivatives, such as cellulose esters, must have a high content of alpha cellulose, and must be substantially free from or have a very low content of lignin, pentosans, coloring materials and other impurities. If the cellulosic materials do not meet these requirements, the cellulose derivatives produced therefrom will be hazy and dark, and will not be completely soluble in the solvents normally employed to dissolve them.
  • a further object of this invention is the provision of an improved process for purifying cellulosic materials, which purified materials will yield cellulose derivatives that are clear and colorless and completely soluble in the solvents normally employed to dissolve them.
  • wood pulp produced by the sulfite process is subjected to an initial alkali boil, which may optionally be omitted, and is then chlorinated, and given another alkali boil at a temperature exceeding about 160 C.
  • the wood pulp is also bleached at some point in the process, to brighten the pulp and improve its color.
  • wood pulp is treated for between about 15 and 30 minutes with a sufiicient quantity of an aqueous solution of sodium hydroxide having a concentration of 2 Claims. (01. 8-105) between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight.
  • the treatment is preferably carried out in a closed vessel at a temperature of between about and C. and under a pressure of between about 15 and 35 pounds per square inch.
  • the wood pulp is then separated from the aqueous solution of sodium hydroxide.
  • water is added to the wood pulp to form a mixture having a consistency of between 2.0 and 3.5% by weight, and the mixture is treated for between 30 and 60 minutes with from about 50 to 70% of the chlorine demand of the pulp at this stage as determined by the permanganate number thereof.
  • the chlorination is preferably carried out at a room temperature of from about 10 to 30 C.
  • the initial alkali treatment may be omitted and the purification of the pulp may begin with its chlorination.
  • the pulp is drained and washed with a dilute solution of sodium hydroxide having a concentration of between about 0.02 and 0.20% by weight until the pulp is rendered alkaline. Thereafter, the pulp is treated with a sufficient quantity of an aqueous solution of sodium hydroxide having a concentration of between 0.1 and 5.0% by weight to form a mixture having a consistency of between about 1 and 12% by weight.
  • the temperature during this alkaline treatment must be at least about C. and may reach about 185 C.
  • the sodium hydroxide need not all be present in the mixture from the very outset, but may be added gradually as treatment proceeds.
  • this treatment may be carried out in two or more stages, employing a fresh solution of alkali for each stage.
  • the temperature may be above about 160 C. during each stage of treatment, or the temperature during certain of the stages may be below this level. In all cases, however, the temperature during at least one stage of treatment must be'aboveabout 160 C. to effect a removal of the pentosans from the pulp.
  • the alternate treatment of the pulp with chlorine and with an alkali will remove the major portion of the impurities therefrom, but will not remove certain coloring materials, which darken the pulp and the products produced therefrom.
  • the partial ly purified pulp may be bleached by treatment for about 120 to 240 minutes with a sufficient quantity of an aqueous hypochlorite solution having a concentration of from about 0.25 to 1.0% by weight, of available chlorine based upon the pulp to be bleached, to form a mixture having a consistency of from about 3.5 to 14% by weight.
  • This treatment is preferably carried out at a temperature of from about 25 to 40 0., and during the treatment the pH of the mixture is maintained at about 10.5 by the addition of alkali, if necessary.
  • the pulp may be bleached immediately after chlorination by treatment for between about 120 and 240 minutes'with a sufficient quantity of an aqueous hypochlorite solution having a concentration of between about 0.25 and 1.0% by weight, of available chlorine based upon the weight of pulp to be bleached, to form a mixture havinga consistency of between about 3.5 and 14% by weight.
  • the bleaching is preferably carried out at a temperature of between about 25 and 40 C., and during the bleaching step the pH of the mixture is maintained .at about 10.5 by the addition of alkali, if necessary.
  • the pulp may be bleached further by treatment for between about 60 and 120 minutes with a sufficient quantity of an aqueous hypochlorite solution having a concentration of between about 0.25 and 0.50% by weight of available chlorine based upon pulp to be bleached, to form a mixture having a consistency of between about 3.5 and 14% by weight.
  • the bleaching is preferably :carried out at a temperature of between about 25 and 40 C., and during the bleaching step the pH of the mixture is maintained at about 10.5 by the addition of alkali, if necessary.
  • the pulp is then washed to remove all traces of the treating agents therefrom, and is finally dried.
  • the alpha cellulose content of the pulp purified in accordance with this invention may reach as high as between about 94 and 95%, and the pentosan content may drop to about 0.7 or even less.
  • cellulose derivatives such as cellulose esters
  • the products obtained are clear and colorless. They are also completely soluble in the solvents, that are normally employed to dissolve cellulose esters, such as acetone, for example.
  • cellulose derivatives which may be prepared from the wood pulp purified in accord-- ance with this invention are not only the cellu lose esters such as cellulose-acetate, cellulose pro- ,pionate, cellulose acetate-proprionate, cellulose acetate-butyrate, but also the celllulose ethers such as ethyl cellulose and benzyl cellulose.
  • the purified wood pulp of this invention may also be employed for the production, by the viscose process, of regenerated cellulose filaments or sheets.
  • the wood pulp of this invention may be admixed with other cellulosic materials such as cotton linters, or it may be employed alone.
  • the purification of wood pulp by the process of our invention is best carried out in a vertical refiner of the type shown diagrammatically in the accompanying figure, wherein the reference numeral ll designates a vertically disposed tank into which the wood pulp may be loaded through a removable cap 12-.
  • the pulp is circulated from the bottom to the top of the tank i I through conduits l3 and M by means of a centrifugal pump 15, which circulation improves the efiiciency of purification and reduces the time necessary therefor.
  • a valve l6 positioned in the conduit 14 controls the rate of circulation of the pulp to prevent overloading of the pump l5.
  • Example I A sufficient quantity of wood pulp produced by the sulfite process is added to a 0.4% by weight aqueous solution of sodium hydroxide to form a mixture having .a consistency of 8% by weight.
  • the mixture is heated for 15 minutes to a tem perature of 122 C. at a pressure of 15 pounds per square inch in a closed digester.
  • the pulp is drained and added to a sufficient quantity of water to form a mixture having a consistency of 2% by weight.
  • To this mixture are added 1.5 parts by weight of chlorine for each parts by weight of the pulp and chlorination permitted to proceed for 50 minutes at a temperature of 25 C. After chlorination, the pulp is drained and washed alkaline with a 0.2% solution of sodium hydroxide.
  • a sufiicient quantity of the pulp is then entered into a 1.3% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6.25% by weight.
  • the mixture is heated in a closed digester to a temperature of 170 C. and held at this temperature for 15 minutes. Even without bleaching the pulp has an alpha cellulose content of 93% and a pentosan content of only 0.6%.
  • the pulp is drained and a sufficient quantity thereof is entered into an aqueous solution of sodium hypochlorite having a concentration of 0.30% by weight of available chlorine based upon the pulp to form a mixture having a consistency of 3.5% by weight.
  • the pulp is washed and dried.
  • the purified pulp produces an ester which is clear and colorless, and completely soluble in acetone.
  • Example II A suflicient quantity of wood pulp produced by the sulfite process is added to water to form a mixture having a consistency of 3.5 by weight. To this mixture is added 60% of the chlorine demand of the pulp and chlorination permitted to proceed for 30 minutes at a temperature of 25 C. After chlorination, the pulp is drained and Washed alkaline with a 0.20% solution of sodium hydroxide. A suiiicient quantity ofthe pulp is entered into a 0.9% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6% by weight. The mix ture is heated in a closed digester to a temperature of 160 C. and held at this temperature for minutes. Even without bleaching the pulp has an alpha cellulose content of 94.4% and a pentosan content of only 1.1%. The pulp is drained and bleached as set forth in Example I.
  • Example III A sufiicient quantity of wood pulp which has been chlorinated and washed alkaline as described in Example II is entered into a 0.7% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6.6% by weight.
  • the mixture is heated in a closed digester to a temperature of 170 C. and held at this temperature for 15 minutes.
  • the pulp is drained and a sufficient quantity thereof is entered into an aqueous solution of sodium hypochlorite having a concentration of 0.50% by weight of available chlorine based upon the pulp to form a mixture having a consistency of 3.5% by weight. After bleaching for 120 minutes at 35 C.
  • the pulp is drained and a sufilcient quantity thereof is entered into an aqueous solution of sodium hydroxide having a concentration of 0.1% by weight to form a mixture having a consistency of 6% by weight.
  • the mixture is heated in a closed digester to a temperature of 173 C. and maintained at this temperature for 30 minutes. After washing and drying, the purified pulp has an alpha cellulose content of 95.0% and a pentosan content of only 1.0%.
  • a process for purifying cellulosic materials the steps which comprise treating said cellulosic materials for between about 15 and 30 minutes at a temperature of between about 120 and 135 C. with a sufficient quantity of sodium hydroxide having a concentration of between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight, treating said cellulosic materials in the form of an aqueous mixture having a consistency of between about 2.0 and 3.5% by weight with chlorine in an amount of from about 50 to of the chlorine demand of the cellulosic material for between about 30 and 60 minutes at a temperature between about 10 and 30 0., and treating said cellulosic materials for up to about 30 minutes at a temperature between about 160 and 185 C. with a sufficient quantity of an aqueous solution of sodium hydroxide having a concentration of between about 0.1 and 5.0% by weight to form a mixture having a consistency of between about 1 and 12% by weight.
  • a process for purifying cellulosic materials the steps which comprise treating said cellulosic materials for between about 15 and 30 minutes at a temperature between about and C. with a suhicient quantity of an aqueous solution of sodium hydroxide having a concentration of between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight, treating said cellulosic materials in the form of an aqueous mixture having a consistency of between about 2.0 and 3.5% by Weight with chlorine in an amount of from about 50 to 70% of the chlorine demand of the cellulosic material for be-- tween about 30 and 60 minutes at a temperature between about 10 and 30 0., treating said cellulosic materials for up to about 30 minutes at a temperature between about and C.

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Description

June 26, 1951 M E, MARTIN ETAL 2,558,054
PURIFICATION OF CELLULOSIC MATERIALS Filed March 16, 1949 INVENTORS MERWN E. MARTlN DANIEL SHEER.
ATTORNEYS.
Patented June 26, 1951 PURIFICATION OF CELLULOSIC MATERIALS Mervin E. Martin and Daniel L. Sherk, Cumberland, Md., assignors to Celanese Corporation of America, a corporation of Delaware Application March 16, 1949, Serial No. 81,742
This invention relates to the purification of cellulosic materials, and relates more particularly to the purification of wood pulps.
Cellulosic materials such as wood pulps that are to be employed for the production of cellulose derivatives, such as cellulose esters, must have a high content of alpha cellulose, and must be substantially free from or have a very low content of lignin, pentosans, coloring materials and other impurities. If the cellulosic materials do not meet these requirements, the cellulose derivatives produced therefrom will be hazy and dark, and will not be completely soluble in the solvents normally employed to dissolve them.
It is an important object of this invention to provide a process for purifying cellulosic materials that are to be employed for the production of cellulose derivatives, which will be especially etficient in operation.
A further object of this invention is the provision of an improved process for purifying cellulosic materials, which purified materials will yield cellulose derivatives that are clear and colorless and completely soluble in the solvents normally employed to dissolve them.
Other objects of this invention will be apparent from the following detailed description and claims.
We have now discovered that when cellulosic materials, such as wood pulp produced by the sulfite process, are purified by alternate treat ments with chlorine and with an alkali, the pentosan content of the pulp after these treatments may be materially reduced by carrying out at least a part of the alkali treatment at a temperature exceeding about 160 C. Moreover, since the reaction between the impurities in the wood pulp and the alkali proceeds at a much more rapid rate at these elevated temperatures, the time necessary for such treatments may be reduced, which permits important savings to be effected both in steam consumption and in required equipment capacity.
I In accordance with the process of our invention, wood pulp produced by the sulfite process is subjected to an initial alkali boil, which may optionally be omitted, and is then chlorinated, and given another alkali boil at a temperature exceeding about 160 C. The wood pulp is also bleached at some point in the process, to brighten the pulp and improve its color.
' A preferred embodiment of an apparatus for carrying out the process of our invention is shown in the accompanying drawing, wherein the Figure is a diagrammatic view of a vertical refiner.
In carrying out our novel process, wood pulp is treated for between about 15 and 30 minutes with a sufiicient quantity of an aqueous solution of sodium hydroxide having a concentration of 2 Claims. (01. 8-105) between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight. The treatment is preferably carried out in a closed vessel at a temperature of between about and C. and under a pressure of between about 15 and 35 pounds per square inch. The wood pulp is then separated from the aqueous solution of sodium hydroxide.
Following the alkali treatment and washing, if desired, water is added to the wood pulp to form a mixture having a consistency of between 2.0 and 3.5% by weight, and the mixture is treated for between 30 and 60 minutes with from about 50 to 70% of the chlorine demand of the pulp at this stage as determined by the permanganate number thereof. The chlorination is preferably carried out at a room temperature of from about 10 to 30 C. As has previously been pointed out, the initial alkali treatment may be omitted and the purification of the pulp may begin with its chlorination.
After the chlorination is completed, the pulp is drained and washed with a dilute solution of sodium hydroxide having a concentration of between about 0.02 and 0.20% by weight until the pulp is rendered alkaline. Thereafter, the pulp is treated with a sufficient quantity of an aqueous solution of sodium hydroxide having a concentration of between 0.1 and 5.0% by weight to form a mixture having a consistency of between about 1 and 12% by weight. For the effective removal of the pentosans, the temperature during this alkaline treatment must be at least about C. and may reach about 185 C. The sodium hydroxide need not all be present in the mixture from the very outset, but may be added gradually as treatment proceeds. Since the reaction between the sodium hydroxide and the impurities in the wood pulp proceeds very rapidly at temperatures above about 160 C. the time necessary for this treatment is very short and the maximum consumption of alkali will be reached after about 30 minutes at a temperature of about 160 C. At temperatures above about C., the reaction between the sodium hydroxide and the impurities in the pulp will generally be completed by the time the pulp is brought up to temperature. However, it may be desirable to hold the mixture at the maximum temperature for about 30 minutes even at temperatures above about 170 C. to insure as complete a purification of the pulp as possible.
Instead of subjecting the pulp to a single stage of high temperature alkali treatment, this treatment may be carried out in two or more stages, employing a fresh solution of alkali for each stage. The temperature may be above about 160 C. during each stage of treatment, or the temperature during certain of the stages may be below this level. In all cases, however, the temperature during at least one stage of treatment must be'aboveabout 160 C. to effect a removal of the pentosans from the pulp.
The alternate treatment of the pulp with chlorine and with an alkali will remove the major portion of the impurities therefrom, but will not remove certain coloring materials, which darken the pulp and the products produced therefrom. To remove these coloring materials, the partial ly purified pulp may be bleached by treatment for about 120 to 240 minutes with a sufficient quantity of an aqueous hypochlorite solution having a concentration of from about 0.25 to 1.0% by weight, of available chlorine based upon the pulp to be bleached, to form a mixture having a consistency of from about 3.5 to 14% by weight. This treatment is preferably carried out at a temperature of from about 25 to 40 0., and during the treatment the pH of the mixture is maintained at about 10.5 by the addition of alkali, if necessary.
Since the high temperature alkali treatment of the pulp renders the coloring materials some-' what more diflicult to remove, it may ice-desirable to carry out part of the bleaching before said treatment. Fo example, the pulp may be bleached immediately after chlorination by treatment for between about 120 and 240 minutes'with a sufficient quantity of an aqueous hypochlorite solution having a concentration of between about 0.25 and 1.0% by weight, of available chlorine based upon the weight of pulp to be bleached, to form a mixture havinga consistency of between about 3.5 and 14% by weight. The bleaching .is preferably carried out at a temperature of between about 25 and 40 C., and during the bleaching step the pH of the mixture is maintained .at about 10.5 by the addition of alkali, if necessary.
Then, after the high temperature alkali treatment, the pulp may be bleached further by treatment for between about 60 and 120 minutes with a sufficient quantity of an aqueous hypochlorite solution having a concentration of between about 0.25 and 0.50% by weight of available chlorine based upon pulp to be bleached, to form a mixture having a consistency of between about 3.5 and 14% by weight. The bleaching is preferably :carried out at a temperature of between about 25 and 40 C., and during the bleaching step the pH of the mixture is maintained at about 10.5 by the addition of alkali, if necessary.
The pulp is then washed to remove all traces of the treating agents therefrom, and is finally dried. The alpha cellulose content of the pulp purified in accordance with this invention may reach as high as between about 94 and 95%, and the pentosan content may drop to about 0.7 or even less. On conversion of the purified pulp to cellulose derivatives, such as cellulose esters, the products obtained are clear and colorless. They are also completely soluble in the solvents, that are normally employed to dissolve cellulose esters, such as acetone, for example.
Among the cellulose derivatives which may be prepared from the wood pulp purified in accord-- ance with this invention are not only the cellu lose esters such as cellulose-acetate, cellulose pro- ,pionate, cellulose acetate-proprionate, cellulose acetate-butyrate, but also the celllulose ethers such as ethyl cellulose and benzyl cellulose. The purified wood pulp of this invention may also be employed for the production, by the viscose process, of regenerated cellulose filaments or sheets. In preparing cellulose derivatives, the wood pulp of this invention may be admixed with other cellulosic materials such as cotton linters, or it may be employed alone.
The purification of wood pulp by the process of our invention is best carried out in a vertical refiner of the type shown diagrammatically in the accompanying figure, wherein the reference numeral ll designates a vertically disposed tank into which the wood pulp may be loaded through a removable cap 12-. During the purification, the pulp is circulated from the bottom to the top of the tank i I through conduits l3 and M by means of a centrifugal pump 15, which circulation improves the efiiciency of purification and reduces the time necessary therefor. A valve l6 positioned in the conduit 14 controls the rate of circulation of the pulp to prevent overloading of the pump l5. Steam and water, as required, are introduced into the tank H, to heat and dilute .the pulp therein, through a conduit H, which enters the side of the tank adjacent its base. Chemicals for purification are introduced into the pulp as it flows through the conduit 13 by means of a conduit I8, and are thoroughly mixed with said pulp as it passes through the centrifugal pump l5, insuring a more uniform purification. After purification, the pulp is discharged from the tank H by means of the centrifugal pump l5 through a conduit I9 opening into .the conduit 1 4 and provided with a valve 20 to control the flow of the pulp therethrough.
The following examples are given to illustrate this invention further.
Example I A sufficient quantity of wood pulp produced by the sulfite process is added to a 0.4% by weight aqueous solution of sodium hydroxide to form a mixture having .a consistency of 8% by weight. The mixture is heated for 15 minutes to a tem perature of 122 C. at a pressure of 15 pounds per square inch in a closed digester. The pulp is drained and added to a sufficient quantity of water to form a mixture having a consistency of 2% by weight. To this mixture are added 1.5 parts by weight of chlorine for each parts by weight of the pulp and chlorination permitted to proceed for 50 minutes at a temperature of 25 C. After chlorination, the pulp is drained and washed alkaline with a 0.2% solution of sodium hydroxide. A sufiicient quantity of the pulp is then entered into a 1.3% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6.25% by weight. The mixture is heated in a closed digester to a temperature of 170 C. and held at this temperature for 15 minutes. Even without bleaching the pulp has an alpha cellulose content of 93% and a pentosan content of only 0.6%. The pulp is drained and a sufficient quantity thereof is entered into an aqueous solution of sodium hypochlorite having a concentration of 0.30% by weight of available chlorine based upon the pulp to form a mixture having a consistency of 3.5% by weight. After bleaching for minutes at 35 C., the pulp is washed and dried. When-converted to cellulose acetate by conventional methods, the purified pulp produces an ester which is clear and colorless, and completely soluble in acetone.
Example II A suflicient quantity of wood pulp produced by the sulfite process is added to water to form a mixture having a consistency of 3.5 by weight. To this mixture is added 60% of the chlorine demand of the pulp and chlorination permitted to proceed for 30 minutes at a temperature of 25 C. After chlorination, the pulp is drained and Washed alkaline with a 0.20% solution of sodium hydroxide. A suiiicient quantity ofthe pulp is entered into a 0.9% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6% by weight. The mix ture is heated in a closed digester to a temperature of 160 C. and held at this temperature for minutes. Even without bleaching the pulp has an alpha cellulose content of 94.4% and a pentosan content of only 1.1%. The pulp is drained and bleached as set forth in Example I.
Example III A sufiicient quantity of wood pulp which has been chlorinated and washed alkaline as described in Example II is entered into a 0.7% by weight aqueous solution of sodium hydroxide to form a mixture having a consistency of 6.6% by weight. The mixture is heated in a closed digester to a temperature of 170 C. and held at this temperature for 15 minutes. The pulp is drained and a sufficient quantity thereof is entered into an aqueous solution of sodium hypochlorite having a concentration of 0.50% by weight of available chlorine based upon the pulp to form a mixture having a consistency of 3.5% by weight. After bleaching for 120 minutes at 35 C. the pulp is drained and a sufilcient quantity thereof is entered into an aqueous solution of sodium hydroxide having a concentration of 0.1% by weight to form a mixture having a consistency of 6% by weight. The mixture is heated in a closed digester to a temperature of 173 C. and maintained at this temperature for 30 minutes. After washing and drying, the purified pulp has an alpha cellulose content of 95.0% and a pentosan content of only 1.0%.
It is to be understood that the foregoing detailed description is given merely by way of i1lustration and that many variations may be made therein without departing from the spirit of our invention.
Having described our invention, what we desire to secure by Letters Patent is:
1. In a process for purifying cellulosic materials, the steps which comprise treating said cellulosic materials for between about 15 and 30 minutes at a temperature of between about 120 and 135 C. with a sufficient quantity of sodium hydroxide having a concentration of between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight, treating said cellulosic materials in the form of an aqueous mixture having a consistency of between about 2.0 and 3.5% by weight with chlorine in an amount of from about 50 to of the chlorine demand of the cellulosic material for between about 30 and 60 minutes at a temperature between about 10 and 30 0., and treating said cellulosic materials for up to about 30 minutes at a temperature between about 160 and 185 C. with a sufficient quantity of an aqueous solution of sodium hydroxide having a concentration of between about 0.1 and 5.0% by weight to form a mixture having a consistency of between about 1 and 12% by weight.
2. In a process for purifying cellulosic materials, the steps which comprise treating said cellulosic materials for between about 15 and 30 minutes at a temperature between about and C. with a suhicient quantity of an aqueous solution of sodium hydroxide having a concentration of between about 0.25 and 1.25% by weight to form a mixture having a consistency of between about 1 and 12% by weight, treating said cellulosic materials in the form of an aqueous mixture having a consistency of between about 2.0 and 3.5% by Weight with chlorine in an amount of from about 50 to 70% of the chlorine demand of the cellulosic material for be-- tween about 30 and 60 minutes at a temperature between about 10 and 30 0., treating said cellulosic materials for up to about 30 minutes at a temperature between about and C. with a sufficient quantity of an aqueous solution of sodium hydroxide having a concentration of between about 0.1 and 5.0% by weight to form a mixture having a consistency of between about 1 and 12% by weight, and bleaching said cellulosic materials with an aqueous solution of sodium hypochlorite before said cellulosic materials are treated with an aqueous solution of sodium hydroxide at a temperature between about 160 and 185 C.
MERVIN E. MARTIN. DANIEL L. :SHERK.
REFERENCES CITED The following references are of record in the file of this patent:
UNITED STATES PATENTS Number Name Date 1,283,113 Drewson Oct. 29, 1918 1,283,114 Drewson Oct. .29, 1918 1,741,540 Richter Dec. 31, 1929 2,198,706 Sheldon Apr. 30, 1940 2,295,215 Joachim Sept. 8, 1942 2,408,849 Haney Oct. 8, 1946 2,424,797 Casciani July 29, 1947

Claims (1)

1. IN A PROCESS FOR PURIFYING CELLULOSIC MATERIALS, THE STEPS WHICH COMPRISES TREATING SAID CELLULOSIC MATERIALS FOR BETWEEN ABOUT 15 AND 30 MINUTES AT A TEMPERATURE OF BETWEEN ABOUT 120 AND 135* C. WITH A SUFFICIENT QUANTITY OF SODIUM HYDROXIDE HAVING A CONCENTRATION OF BETWEEN ABOUT 0.25 AND 1.25% BY WEIGHT TO FORM A MIXTURE HAVING A CONSISTENCY OF BETWEEN ABOUT 1 AND 12% BY WEIGHT, TREATING SAID CELLULOSIC MATERIALS IN THE FORM OF AN AQUEOUS MIXTURE HAVING A CONSISTENCY OF BETWEEN ABOUT 2.0 AND 3.5% BY WEIGHT WITH CHLORINE IN AN AMOUNT OF FROM ABOUT 50 TO 70% OF THE CHLORINE DEMAND OF THE CELLULOSIC MATERIAL FOR BETWEEN ABOUT 30 AND 60 MINUTES AT A TEMPERATURE BETWEEN ABOUT 10 AND 30* C., AND TREATING SAID CELLULOSIC MATERIALS FOR UP TO ABOUT 30 MINUTES AT A TEMPERATURE BETWEEN ABOUT 160 AND 185* C. WITH A SUFFICIENT QUANTITY OF AN AQUEOUS SOLUTION OF SODIUM HYDROXIDE HAVING A CONCENTRATION OF BETWEEN ABOUT 0.1 AND 5.0% BY WEIGHT TO FORM A MIXTURE HAVING A CONSISTENCY OF BETWEEN ABOUT 1 AND 12% BY WEIGHT.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2882965A (en) * 1955-02-23 1959-04-21 Columbia Cellulose Company Ltd High viscosity, high percentage alpha cellulose from sulfite pulp
US3884752A (en) * 1973-09-17 1975-05-20 Int Paper Co Single vessel wood pulp bleaching with chlorine dioxide followed by sodium hypochlorite or alkaline extraction

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1283113A (en) * 1918-01-24 1918-10-29 West Virginia Pulp & Paper Company Process of refining wood-pulp for nitrating or similar purposes.
US1283114A (en) * 1918-06-19 1918-10-29 West Virginia Pulp & Paper Company Process of refining sulfite wood-pulp for nitrating or similar purposes.
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US2424797A (en) * 1943-12-18 1947-07-29 Niagara Alkali Company Process for the purification of cellulosic material

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US1283113A (en) * 1918-01-24 1918-10-29 West Virginia Pulp & Paper Company Process of refining wood-pulp for nitrating or similar purposes.
US1283114A (en) * 1918-06-19 1918-10-29 West Virginia Pulp & Paper Company Process of refining sulfite wood-pulp for nitrating or similar purposes.
US1741540A (en) * 1925-12-16 1929-12-31 Brown Co Process for the production of high-alpha cellulose fiber for the manufacture of cellulose derivatives
US2198706A (en) * 1936-11-23 1940-04-30 Cellulose Res Corp Refining wood pulp
US2295215A (en) * 1940-09-16 1942-09-08 Maui Agricultural Company Ltd Alpha cellulose pulp
US2408849A (en) * 1943-03-12 1946-10-08 Celanese Corp Cellulose purification
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US2882965A (en) * 1955-02-23 1959-04-21 Columbia Cellulose Company Ltd High viscosity, high percentage alpha cellulose from sulfite pulp
US3884752A (en) * 1973-09-17 1975-05-20 Int Paper Co Single vessel wood pulp bleaching with chlorine dioxide followed by sodium hypochlorite or alkaline extraction

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