CA2384767A1

CA2384767A1 - Cellulose dope and process for producing the same

Info

Publication number: CA2384767A1
Application number: CA002384767A
Authority: CA
Inventors: Chihiro Yamane; Kunihiko Okajima; Seiji Shimizu
Original assignee: Individual
Current assignee: Asahi Kasei Corp
Priority date: 1999-11-08
Filing date: 2000-10-26
Publication date: 2001-05-17
Also published as: AU7959100A; WO2001034655A1; EP1245576A4; US7108907B1; EP1245576A1

Abstract

A cellulose dope comprising an aqueous caustic soda solution and a cellulose dissolved in the solution, characterized in that the concentration of causti c soda (CNa) is 6.5 to 11 wt.%, the cellulose content (CC) is 4 to 12 wt.%, an d zero-shear viscosity of the cellulose dope (.eta.0), the cellulose content (CC), and the viscosity-average degree of polymerization of the cellulose satisfy the following relationship (1): .eta.0 = kCCm .times. DPCp. In the relationship, .eta.0 represents zero-shear viscosity of the cellulose dope (mPa.s); CC represents cellulose content of the cellulose dope (wt.%) DPC represents viscosity-average degree of polymerization of the cellulose in cellulose dope; K = 3.9 .times. 10-11; 5 <= m <= 7; and 3 <= p < = 4.

Description

TITLE OF THE INVENTION
Cellulose dope and method for producing the same BACKGROUND OF THE INVENTION
Field of the Invention The present invention relates to a cellulose dope.
More particularly, the present invention is concerned with a cellulose dope comprising an aqueous sodium hy-droxide solution and cellulose dissolved in the solu-tion, wherein the cellulose dope has a sodium hydroxide concentration (CNa) of from 6.5 to 11 ~ by weight and a cellulose content (Cc) of from 4 to 12 ~ by weight, and wherein the zero-shear viscosity (~o) of the cellulose dope, the cellulose content (Cc) of the cellulose dope, and the viscosity average degree of polymerization of the cellulose in the cellulose dope satisfy a specific relationship. The present invention is also concerned with a method for producing the cellulose dope. The cellulose dope of the present invention is stable and free from gelation even when the cellulose dope has a high content of cellulose having a high degree of po-lymerization. By the use of the cellulose dope of the present invention, it becomes possible to produce, without using a large amount of a poisonous substance, a regenerated cellulose shaped article (such as a fiber or a film) which has a mechanical strength sufficient for practical use. Therefore, the cellulose dope of the present invention is commercially very advantageous.
Further, the present invention is also concerned with a cellulose shaped article obtained by subjecting the cellulose dope to coagulation treatment, and a cellulo-se slurry used for producing the cellulose dope.
Prior Art Cellulose is a polysaccharide having a linear chain comprising a number of D-glucose (D-glucopyranose) molecules, wherein the mutually adjacent molecules are bonded to each other through ~-1,4-bond.
Cellulose is a very important substance in industries, which has been used in various fields.
An important example of the usage of cellulose is the use as a material for the so-called regenerated cellulose shaped article. A regenerated cellulose shaped article can be produced by a method which com-prises dissolving cellulose in an appropriate solvent to obtain a cellulose solution, and subjecting the ob-tained cellulose solution to an appropriate chemical treatment, thereby coagulating the cellulose solution.
However, cellulose is insoluble in any of water and or-ganic solvents generally used in the art (e. g., alco-hols). Therefore, for producing a cellulose solution for use in the production of a regenerated cellulose shaped article (hereinafter, such a solution is fre-quently referred to as a "cellulose dope"), a special solvent and a special chemical treatment for cellulose are needed.
Most representative examples of regenerated cellu-lose shaped articles include a fiber and a film. A fi-ber of regenerated cellulose is called a "rayon", and a film of regenerated cellulose is called a "cellophane".
Both of them are very widely used. Further, in some cases, regenerated cellulose shaped articles are used in a particulate form or used in the form of a coating formed on a substrate.
Further, by coagulating a cellulose dope having incorporated therein various edible components, such as a polysaccharide, a polypeptide and a natural resin, an edible shaped article containing the cellulose as a substrate can be obtained (hereinafter, such an edible shaped article is frequently referred to as an "edible cellulose article").
At present, the method for the production of re-generated cellulose shaped articles which ~is commer-cially practiced is performed mainly by either of two processes, namely, the viscose process and the cupram-monium process.
The viscose process comprises reacting cellulose with carbon disulfide in the presence of sodium hydrox-ide to obtain sodium cellulose xanthate, dissolving the sodium cellulose xanthate in an aqueous sodium hydrox-ide solution to obtain a cellulose dope (viscose), and coagulating the cellulose dope by contacting the cellu-lose dope with an aqueous acidic solution to thereby obtain a regenerated cellulose shaped article.
On the other hand, the cuprammonium process com-prises dissolving cellulose in a cuprammonium solution to thereby obtain a cellulose dope, and contacting the cellulose dope with water and then, with an aqueous acidic solution to coagulate the cellulose dope, there-by obtaining a regenerated cellulose shaped article.
However, both of these two processes need a large amount of a poisonous substance, such as ammonia, car-bon disulfide or a heavy metal (copper), in the step for preparing the cellulose dope or for shaping the cellulose dope. Therefore, the environment in the workshop for performing these processes is inevitably polluted.
Moreover, needless to say, these processes neces-sitate a step for recovering a poisonous substance. If the recovery step is incomplete, a large amount of the poisonous substance is inevitably caused to be dis-charged in the environment. Therefore, these processes are also disadvantageous from the viewpoint of protec-5 tion of the environment.
Furthermore, these processes are disadvantageous in that these processes cannot be employed for produc-ing an edible cellulose article.
In order to solve the problems of these processes, various proposals have been made and reported with re-spect to the environment friendly methods for producing regenerated cellulose shaped articles, which do not use a poisonous substance. As an example of such methods, there can be mentioned a method in which cellulose is dissolved in an aqueous alkali solution, such as an aqueous sodium hydroxide solution, to obtain a cellu-lose dope, and the obtained cellulose dope is used for producing a regenerated cellulose shaped article.
For easy understanding of the techniques for pro-ducing a regenerated cellulose shaped article by using a cellulose dope, abbreviations used for indicating the characteristics of cellulose and a cellulose dope are enumerated below.
DPc: viscosity average degree of polymerization of cellulose.
Cc: cellulose content (~ by weight) of a cellu-lose dope, that is, the ratio of the weight of the cellulose contained in the cellulose dope (i.e., the sum of the weight of the cellulose dissolved in the cellulose dope and the weight of the cellulose remaining undissolved in the cellulose dope) to the weight of the cellulose dope.

CNa sodium hydroxide concentration (~ by weight) of a cellulose dope.

Sc: dissolution ratio ($ by weight) of cellulose in a cellulose dope, that is, the ratio of the weight of the cellulose dissolved in the cellulose dope to the weight of the cellu-lose contained in the cellulose dope (i.e., the sum of the weight of the cellulose dis-solved in the cellulose dope and the weight of the cellulose remaining undissolved in the cellulose dope).

Rc: amount of undissolved cellulose in a cellulose dope, more specifically, the vol-ume (ml) of the undissolved cellulose contained in 20 liters of the cellulose dope.
An explanation is made below with respect to specific examples of the above-mentioned environment friendly methods. Unexamined Japanese Patent Applica-tion Laid-Open Specification Nos. 62-240328 and 62-240329 disclose a method in which cellulose is subject-ed to steam explosion treatment to render the cellulose soluble in an aqueous alkali solution, the obtained cellulose is dissolved in an alkali solution to thereby obtain a cellulose dope, and the cellulose dope is sub-jected to wet shaping. The cellulose dope obtained and shaped in this method has a cellulose content (Cc) of only about 5 ~ by weight.
In the above-mentioned method, any of poisonous substances, such as carbon disulfide, a heavy metal and an organic solvent, is not used. However, in the above-mentioned method, the solubilization of the cel-lulose is unsatisfactory.
In the process for producing a fiber, a film or the like from a cellulose dope, when the cellulose dope used has a Cc value of 5 ~ by weight or more, it is re-quired that the dissolution ratio (Sc) of the cellulose in the dope be 99.0 ~ by weight or more.
When the cellulose dope has a Cc value of 5 ~ by weight and an Sc value of 99.0 ~ by weight, the cellu-lose dope has an undissolved cellulose amount (Rc) of about 7.9 ml. In the above-mentioned process, a filter is used in order to remove the undissolved cellulose contained in the cellulose dope. When the cellulose dope has a high Rc value, the filter is likely to be clogged. Specifically, when the cellulose dope has an Rc value higher than about 7.9 ml (which is an Rc value obtained when, for example, the cellulose dope has a Cc .value of 5 ~ by weight and has an Sc value lower than 99.0 ~ by weight), the filter is frequently clogged, so that a commercial scale production of a fiber, a film or the like becomes practically impossible.
In an actual process for producing a fiber, a film or the like from a cellulose dope, it is required that the Rc value of the cellulose dope be lowered to about 1.6 ml by increasing the Sc value of the cellulose dope to about 99.8 ~ by weight.
In view of this requirement, the cellulose dope obtained by the methods disclosed in the above-mentioned Unexamined Japanese Patent Application Laid-Open Specification Nos. 62-240328 and 62-240329 cannot be used in an actual process for producing a fiber, a film or the like, because the cellulose dopes obtained in these methods have a cellulose dissolution ratio (Sc) of less than 99.0 ~ by weight and, hence, have an undissolved cellulose amount (Rc) as large as 10 ml or more.

As a method which solves the problem accompanying the techniques of the above patent documents, a method is proposed in which, in an attempt to solubilize the cellulose to a satisfactory level (i.e., to increase the Sc value) to thereby lower the Rc value of the cel-lulose dope, a slurry comprising cellulose dispersed in an aqueous medium is prepared, and a cellulose dope is produced by using the obtained slurry.
For example, Unexamined Japanese Patent Applica-tion Laid-Open Specification No. 9-316101 discloses the following two methods.
1) Cellulose is added to a first aqueous alkali solu-tion having a low alkali concentration, wherein the particle size of the cellulose has not been adjusted and the viscosity average degree of polymerization (DPc) of the cellulose has been adjusted to 750 or less.
The resultant mixture is stirred to disperse the cellu-lose in the first aqueous alkali solution, thereby ob-taining a slurry. To the obtained slurry is added a second aqueous alkali solution having a high alkali concentration, followed by stirring at a high speed to dissolve the cellulose in the aqueous alkali solution, thereby obtaining a cellulose dope, wherein the second aqueous alkali solution is used such that the final al-kali concentration of the cellulose dope becomes 7 to 11 ~ by weight.
2) Cellulose is pulverized in water such that the av-erage particle diameter of the cellulose becomes 20 Eun or less, thereby obtaining a slurry. To the obtained 5 slurry is added an aqueous alkali solution having a high alkali concentration, followed by stirring at a high speed to dissolve the cellulose in the aqueous al-kali solution, thereby obtaining a cellulose dope, wherein the aqueous alkali solution is used such that 10 the final alkali concentration of the cellulose dope becomes 7 to 11 ~ by weight.
The above-mentioned Unexamined Japanese Patent Ap-plication Laid-Open Specification No. 9-316101 de-scribes that, by the above-mentioned two methods, it is possible to produce cellulose dopes having a cellulose content (Cc) of 2 ~ by weight or more and a cellulose dissolution ratio (Sc) of 99 ~ by weight or more.
Specifically, the cellulose dopes obtained in the above-mentioned patent document include cellulose dopes which respectively contain 8 ~ by weight of cellulose having a DPc value of 230, 5 ~ by weight of cellulose having a DPc value of 350 and 2 ~ by weight of cellu-lose having a DPc value of 750. These cellulose dopes have a cellulose dissolution ratio (Sc) of 99 ~ by weight or more.

However, in the methods of the above patent docu-ment, if cellulose having a DPc value higher than that of the cellulose used in the above patent document is used or if a cellulose dope having a Cc value higher than that of the cellulose dope produced in the above patent document is produced (for example, if a cellu-lose dope containing 10 ~ by weight of the cellulose having a DPc value of 230 is produced), the produced cellulose dope has a problem in that the cellulose is not satisfactorily dissolved in the aqueous alkali so-lution or in that the cellulose dope is very unstable and susceptible to gelation. Needless to say, such a cellulose dope susceptible to gelation cannot be used in the commercial scale production of a regenerated cellulose shaped article. As seen from the above, in the above-mentioned methods, at least one of the Cc value of the cellulose dope and the DPc value of the cellulose cannot be satisfactorily increased.
Generally, it is considered that the gelation of a cellulose dope occurs due to the association of molecu-lar chars of cellulose, which association of the mo-lecular chains is formed through the hydrogen bonds.
(The association of the molecular chains of cellulose is one of the inherent characteristics of cellulose.) Specifically, it is considered that a plurality of molecular chains of the cellulose are associated with each other, wherein unsatisfactorily dissolved portions of the cellulose molecular chains, which portions are not satisfactorily solvated in the aqueous alkali solu-tion, serve as cores of the association, so that the cellulose dope as a whole loses its fluidity, leading to a gelation of the cellulose dope.
By a method generally employed in the art, it is difficult to produce a cellulose shaped article having a strength sufficient for practical use from a cellu-lose dope containing cellulose having a low DPc value or a cellulose dope having a low Cc value. For obtain-ing a cellulose shaped article having a strength suffi-cient for practical use from such a cellulose dope, it is required to coagulate the cellulose dope in a spe-cial medium having a very high dehydration ability, such as a concentrated aqueous sulfuric acid solution having a concentration as high as 50 to 80 ~ by weight.
Further, when a cellulose dope containing cellu-lose having a low DPc value or a cellulose dope having a low Cc value is used for producing a cellulose shaped article, it is very difficult to produce a desired cel-lulose shaped article (especially, a fiber or a film) by a method generally employed in the art and, hence, it becomes necessary to conduct the production of a cellulose shaped article by a special method. As an example of such special method, there can be mentioned a method in which, in a process for producing a fiber or a film from a cellulose dope, which comprises coagu-lating a cellulose dope, a net is used in an early sta-ge of the coagulation (see Unexamined Japanese Patent Application Laid-Open Specification No. 7-278941). The reason for the use of a net is as follows. The fiber or film during the course of the coagulation has an un-satisfactory mechanical strength such that it is impos-sible to reel up the fiber or film by a generally em-ployed process. Therefore, a net is used for re-inforcing the fiber or film during the course of the coagulation. However, when a net is used, the opera-tions involved in the production become cumbersome and the production efficiency becomes disadvantageously low.
In addition, as in the case of the production of a fiber or a film, the use of the cellulose dope contain-ing cellulose having a low DPc value or the cellulose dope having a low Cc value in the production of the above-mentioned edible cellulose article is also accom-panied by the problem caused by the poor mechanical strength of a cellulose shaped article (i.e., edible cellulose article) during the course of the coagulation.
Therefore, the shape of the cellulose shaped article produced is inevitably limited. For example, in the case of the production of an edible cellulose article in the form of a fiber, the diameter of the edible cel-lulose article needs to be large; and, in the case of the production of an edible cellulose article in the form of a film, the thickness of the edible cellulose article needs to be large. Further, the blending ratio of a polysaccharide, a polypeptide or a natural resin in the edible cellulose article needs to be low.
Therefore, the characteristics (such as palatableness) of the edible cellulose article cannot be satisfactori-1y improved.
With respect to the slurry comprising cellulose dispersed in an aqueous medium, many other examples are known. For example, such a slurry is disclosed in U.S.
Patent No. 5,123,962. However, the slurry described in this patent document is intended to be used as an edi-ble additive, and is not intended to be used in a proc-ess in which a cellulose dope is produced from the slurry and the obtained cellulose dope is used for pro-ducing a general cellulose shaped article. Further, the cellulose used for producing the slurry has a DPc value of about 200 or less, so that, at least by an or-dinary method, it is impossible to produce from the slurry a cellulose shaped article having a strength sufficient for practical use.
Descriptions on slurries used for producing a cel-lulose dope are also found in patent documents other than the above-mentioned Unexamined Japanese Patent Ap-5 plication Laid-Open Specification Nos. 62-240328, 62-240329 and 9-316101. For example, Unexamined Japanese Patent Application Laid-Open Specification No. 9-124702 discloses a technique for rendering cellulose soluble in an aqueous alkali solution by microfibrillating cel-10 lulose. In the technique of this patent document, cellulose is subjected to wet pulverization treatment using a stone mill type wet pulverizer to obtain a slurry comprising a microfibrillated cellulose disper-sed in an aqueous medium, in which the number of micro-15 fibrils having a fiber diameter of 1 Eun or less amounts to 95 ~ or more, based on the total number of microfi-brils (in a preferred mode, the number of microfibrils having a fiber diameter of 500 nm or less amounts to 90 ~ or more, based on the total number of microfi-brils).
This patent document also describes that, when a cellulose dope having a cellulose content (Cc) of 5.4 by weight is produced by using a slurry obtained by subjecting cellulose having a DPc value of about 700 to the above-mentioned treatment, and an aqueous sodium hydroxide solution having a sodium hydroxide concentra-tion of 9.2 ~ by weight, the produced cellulose dope has a cellulose dissolution ratio (Sc) of about 95 Further, the above patent document also describes that, when a cellulose dope having a cellulose content (Cc) of 7 ~ by weight is produced by using a slurry ob-tained by subjecting to the above-mentioned treatment cellulose having a DPc value of about 300 (crystal type: cellulose II) which is produced from an alkali cellulose for use in the production of a rayon, and an aqueous sodium hydroxide solution having a sodium hy-droxide concentration of 8.5 ~ by weight, the produced cellulose dope has a cellulose dissolution ratio (Sc) of about 90 However, as mentioned above, in the process for producing a fiber, a film or the like from a cellulose dope, when the cellulose dope used has a Cc value of 5 ~ by weight or more and has an Sc value of less than 99.0 ~ by weight, it is practically impossible to pro duce a fiber, a film or the like on a commercial scale.
Therefore, the cellulose dope cannot be used in an ac-tual process for producing a fiber, a film or the like unless an operation for removing a substantial amount of the undissolved cellulose from the cellulose dope is conducted.

Further, as mentioned above, in the technique of Unexamined Japanese Patent Application Laid-Open Speci-f ication No. 9-124702, cellulose is microfibrillated by using a stone mill type wet pulverizer in order to pro-s duce a slurry containing a microfibrillated cellulose.
However, the produced slurry has an extremely high vis-cosity, so that, in the production of a cellulose dope by the use of the slurry, the slurry needs to be stir-red under a very high shearing stress. As described below, the extremely high viscosity of the slurry is considered to be caused by a network of microfibrils formed by the interaction between microfibrils of the cellulose. Further, as the degree of polymerization of the cellulose increases, the yield shearing stress of the slurry increases, so that a high shearing stress is needed for stirring the slurry. Therefore, it is very difficult to produce a cellulose dope by using the above-mentioned slurry.
In general, as a pretreatment conducted prior to the production process of the above-mentioned viscose (i.e., cellulose dope obtained by dissolving sodium cellulose xanthate in an aqueous sodium hydroxide solu-tion), the cellulose is pulverized in an aqueous alkali solution. As the aqueous alkali solution, an aqueous alkali solution having an alkali concentration as high as 10 ~ by weight is generally used. It is considered that the aqueous alkali solution having such a high al-kali concentration is used for the purpose of improving the pulverization efficiency. However, when cellulose is contacted with an aqueous alkali solution having such a high alkali concentration, the cellulose is con-verted into a crystalline alkali cellulose. Since a crystalline alkali cellulose is completely insoluble in an aqueous alkali solution, the slurry obtained by the above-mentioned method cannot be used for producing a cellulose dope containing an aqueous alkali solution as a solvent.
Unexamined Japanese Patent Application Laid-Open Specification No. 4-348130 discloses a method for pro-ducing particulate cellulose by aging cellulose in the presence of an alkali.
However, the cellulose used has a viscosity aver-age degree of polymerization (DPc) of from 20 to 150.
As already explained above, it is extremely difficult to produce a cellulose shaped article for practical use by the use of cellulose having such a low degree of po-lymerization. Moreover, it should be noted that the above-mentioned aging in itself is a technique for con-verting cellulose into a crystalline alkali cellulose which is completely insoluble in an aqueous alkali so-lution. Therefore, the technique of the above patent document cannot be used for the production of a cellu-lose dope containing an aqueous alkali solution as a solvent.
From the above, it is apparent that a conventional cellulose dope containing an aqueous alkali solution as a solvent for cellulose, which is produced by the con-ventional method, has various problems caused by the unsatisfactory solubilization of the cellulose. The problems can be enumerated as follows:
the cellulose dope contains a large amount of undis-solved cellulose, so that the cellulose dope cannot be used in an actual production process;
~ the amount of cellulose having a satisfactory degree of polymerization, which is dissolved in the cellulose dope, is not sufficient for producing a cellulose shaped article having a sufficient strength for practi-cal use; and the cellulose dope is unstable and susceptible to ge-lation.
Thus, the conventional cellulose dope has a problem in that there are fatal defects with respect to the mechanical properties of the cellulose shaped article produced from the conventional cellulose dope and the procedure necessary for producing the cellulose shaped article from the conventional cellulose dope.
SUMMARY OF THE INVENTION
In this situation, the present inventors have made 5 extensive and intensive studies with a view toward de-veloping a cellulose dope which is stable and free from gelation even when it has a high content of cellulose having a high degree of polymerization and which can be used for producing, without using a large amount of a 10 poisonous substance, a regenerated cellulose shaped ar-ticle (such as a fiber or a film) having a mechanical strength sufficient for practical use. As a result, it has unexpectedly been found that, when a cellulose dope comprising an aqueous sodium hydroxide solution and 15 cellulose dissolved in the solution exhibits a zero-shear viscosity (r~o) which satisfies a specific rela-tionship between the cellulose content (Cc) of the cel-lulose dope and the viscosity average degree of polym-erization (DPc) of the cellulose in the cellulose dope, 20 the cellulose dope is stable and free from gelation even when it has a high content of cellulose having a high degree of polymerization.
It has also been found that the cellulose dope can be produced by using a cellulose slurry having unique physical properties, which slurry has been produced by a specific method.
Based on these findings, the present invention has been completed.
Accordingly, it is a primary object of the present invention to provide a cellulose dope which is stable and free from gelation even when it has a high content of cellulose having a high degree of polymerization.
It is another object of the present invention to provide a method for producing the cellulose dope.
It is still another object of the present inven-tion to provide a cellulose shaped article obtained by subjecting the cellulose dope to coagulation treatment.
It is still another object of the present inven-tion to provide a cellulose slurry used for producing the cellulose dope.
The foregoing and other objects, features and ad-vantages of the present invention will be apparent from the following detailed description and appended claims taken in connection with the accompanying drawings.
BRIEF DESCRIPTION OF THE DRAWINGS
In the drawings:
Fig. 1 is a viscosity-stress curve showing the viscosity characteristics of the cellulose slurry of the present invention;

Fig. 2 is a graph showing the relationship between the viscosity average degrees of polymerization (DPc) of the celluloses which are used in Examples 25 to 27 and Comparative Examples 22 and 23 and the strengths of gel films which are produced in Examples 25 to 27 and Comparative Examples 22 and 23 (hereinafter, each of the celluloses used in Examples 25 to 27 is referred to as an "alkali/cellulose slurry" and each of the cellu-loses used in Comparative Examples 22 and 23 is referred to as an "water/cellulose slurry"); and Fig. 3 is a graph showing that the cellulose dopes produced in Examples 9, 11, 12, 14 and 15 exhibit zero-shear viscosity (~o) values which satisfy formula (1) which is shown below.
DETAILED DESCRIPTION OF THE INVENTION
According to the present invention, there is provided a cellulose dope comprising an aqueous sodium hydroxide solution and cellulose dissolved in the solu-tion, the cellulose dope having a sodium hydroxide con-centration (CNa) of from 6.5 to 11 ~ by weight and a cellulose content (Cc) of from 4 to 12 ~ by weight, wherein the cellulose dope exhibits a zero-shear viscosity (~o) which satisfies the following formula (1):
= kCcm x DPcp (1) wherein:
represents the zero-shear viscosity (mPa~s) of the cellulose dope, Cc represents the cellulose content (~ by weight) of the cellulose dope, DPc represents the viscosity average degree of polymerization of the cellulose in the cellu-lose dope, k = 3.9 x 10-11, m is a number of from 5 to 7, and p is a number of from 3 to 4.
For easy understanding of the present invention, the essential features and various preferred embodi-ments of the present invention are enumerated below.
1. A cellulose dope comprising an aqueous sodium hy-droxide solution and cellulose dissolved in the solu-tion, the cellulose dope having a sodium hydroxide con-centration (CNa) of from 6.5 to 11 ~ by weight and a cellulose content (Cc) of from 4 to 12 ~ by weight, wherein the cellulose dope exhibits a zero-shear viscosity (~o) which satisfies the following formula (1):
'r~o = kCcm x DPcp ( 1 ) wherein:
~o represents the zero-shear viscosity (mPa~s) of the cellulose dope, Cc represents the cellulose content (~ by weight) of the cellulose dope, DPc represents the viscosity average degree of polymerization of the cellulose in the cellu-lose dope, k = 3.9 x 10-11, m is a number of from 5 to 7, and p is a number of from 3 to 4.
2. The cellulose dope according to item 1 above, wherein the viscosity average degree of polymerization (DPc) of the cellulose is from 350 to 1,200, and the cellulose content (Cc) is from 5 to 10 ~ by weight, and wherein m and p are from 6.3 to 6.5 and from 3.2 to 3.5, respectively.
3. The cellulose dope according to item 1 or 2 above, wherein, in the NMR analysis of the cellulose dope, the 6-position carbon atoms of the glucose units of the cellulose exhibit a longitudinal relaxation time (ic) of from 10 to 400 ms, and the 1-position carbon atoms of the glucose units of the cellulose exhibit a longi-tudinal relaxation time (ic) of from 200 to 10,000 ms.

4. The cellulose dope according to item 3 above, wherein, in the NMR analysis of the cellulose dope, the 6-position carbon atoms of the glucose units of the cellulose exhibit a longitudinal relaxation time (ic) 10 of from 10 to 200 ms.
5. The cellulose dope according to any one of items 1 to 4 above, wherein the hydroxyl groups of the cellu-lose are partially modified by reaction with a reagent 15 which is reactive with a hydroxyl group in the presence of an alkali .
6. The cellulose dope according to item 5 above, wherein the reagent is selected from the group consist-20 ing of an etherification agent and a xanthation agent.
7. The cellulose dope according to item 5 or 6 above, wherein the reagent is used in an amount of 0.1 mole or less per mole of glucose units in the cellulose.

8. A method for producing the cellulose dope of item 1 above, which comprises:
(1) providing a cellulose slurry comprising an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average parti-cle diameter of 30 ~m or less, the cellulose slurry having a sodium hydroxide concentration of from 0.5 to less than 6.5 ~ by weight and a cellulose content of 5 ~ by weight or more, (2) adjusting the sodium hydroxide concentration of the cellulose slurry to 6.5 to 11 ~ by weight, and (3) stirring the cellulose slurry at 10 °C or less by means of a stirrer under stirring conditions satis-fying at least one requirement selected from the group consisting of the requirement that the stirring is per-formed at a shear rate of 9,000/sec or less and the re-quirement that the stirring is performed at a stirring speed of 500 m/min or less in terms of the speed at which the outer end of an agitating element of the stirrer is rotated, the steps (2) and (3) being conducted in the order of step (2) and step (3) or simultaneously, thereby causing the particulate cellulose to be dissolved in the cellulose slurry to the extent that the cellulose has a dissolution ratio of 99.0 ~ by weight or more, to obtain a cellulose dope, wherein the cellulose slurry satisfies the follow-ing formula (2):
~T - KlexP (klCNa) (2) wherein:
QT represents the yield stress (Pa) of the slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and CNa is the sodium hydroxide concentration (~ by weight) of the slurry, and wherein, in the solid state NMR analysis of the slurry, the cellulose in the slurry exhibits a non-crystallinity (Xam) of 0.5 or more, the non-crystallinity being defined by the following formula (3):
Xam - Ihigh ~ ( Ihigh + Ilow) ( 3 ) wherein:
Xam is the non-crystallinity of the cellulose in the slurry, and Inigh and Ilow respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of the slurry, wherein the peaks are, respectively, ascribed to the higher magnetic field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in the slurry, and wherein separation between the peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of the peaks is approximated to the Gaussian dis-tribution function.
9. The method according to item 8 above, wherein the cellulose slurry satisfies the following formula (4):
6T = K2 + k2DPc (4) wherein:
aT represents the yield stress (Pa) of the slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in the slurry.
10. The method according to item 8 or 9 above, wherein the cellulose in the cellulose slurry has an average particle diameter of 20 dun or less .
11. The method according to any one of items 8 to 10 above, wherein the cellulose in the cellulose slurry has a viscosity average degree of polymerization (DPc) of from 350 to 1,200.
12. The method according to any one of items 8 to 11 above, wherein the hydroxyl groups of the cellulose in the cellulose slurry are partially modified by reaction with a reagent which is reactive with a hydroxyl group in the presence of an alkali.
13. The method according to any one of items 8 to 11 above, which further comprises, at a point in time whi-ch is after step (1) and before the end of step (3), adding to the cellulose slurry a reagent which is reac-tive with a hydroxyl group in the presence of an alkali.
14. The method according to item 12 or 13 above, wherein the reagent is selected from the group consist-ing of an etherification agent and a xanthation agent.
15. The method according to any one of items 12 to 14 above, wherein the reagent is used such that the amount of the reagent is 0.1 mole or less per mole of glucose units in the cellulose in the cellulose dope.

16. A cellulose shaped article obtained by subjecting the cellulose dope of any one of items 1 to 7 above to at least one coagulation treatment selected from the group consisting of drying coagulation, gelation coagu-5 lation and neutralization coagulation.
17. The cellulose shaped article according to item 16 above, wherein the cellulose dope contains at least one additive selected from the group consisting of a poly-10 saccharide, a polypeptide and a natural resin.
18. The cellulose shaped article according to item 16 or 17 above, which is a fibrous body, a flat film, a tubular film, a hollow fiber, a particle, a sponge body 15 or a coating.
19. A cellulose slurry comprising an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average particle diameter of 30 ~m 20 or less, the cellulose slurry having a sodium hydroxide concentration of from 0.5 to less than 6.5 ~ by weight and a cellulose content of 5 ~ by weight or more, wherein the cellulose slurry satisfies the follow-25 ing formula (2):

QT - Klexp (klCNa) (2) wherein:
QT represents the yield stress (Pa) of the slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and CNa is the sodium hydroxide concentration (~ by weight) of the slurry, and wherein, in the solid state NMR analysis of the slurry, the cellulose in the slurry exhibits a non-crystallinity (Xam) of 0.5 or more, the non-crystallinity being defined by the following formula (3).
Xam - Ihigh ~ ( Ihigh + Ilow) ( 3 ) wherein:
Xam is the non-crystallinity of the cellulose in the slurry, and Ihigh and IloW respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of the slurry, wherein the peaks are, respectively, ascribed to the higher magnetic field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in the slurry, and wherein separation between the peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of the peaks is approximated to the Gaussian dis-tribution function.
20. The cellulose slurry according to item 19 above, which satisfies the following formula (4):
aT = K2 + k2DPc (4) wherein:
6T represents the yield stress (Pa) of the slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in the slurry.
21. The cellulose slurry according to item 19 or 20 above, wherein the cellulose has an average particle diameter of 20 Eun or less .
Hereinbelow, the present invention is described in detail.
The cellulose dope of the present invention com-prises an aqueous sodium hydroxide solution and cellu-lose dissolved in the solution, wherein the cellulose dope has a sodium hydroxide concentration (CNa) of from 6.5 to 11 ~ by weight and a cellulose content (Cc) of from 4 to 12 ~ by weight, and wherein the cellulose do-pe exhibits a zero-shear viscosity (gyp) which satisfies the following formula (1):
= kCcm x DPcp (1) wherein:
represents the zero-shear viscosity (mPa~s) of the cellulose dope, Cc represents the cellulose content (~ by weight) of the cellulose dope, DPc represents the viscosity average degree of polymerization of the cellulose in the cellu-lose dope, k = 3.9 x 10'11, m is a number of from 5 to 7, and p is a number of from 3 to 4.
When the cellulose dope has a cellulose content (Cc) of less than 4 ~ by weight, the cellulose con-tained in the cellulose dope is easily solubilized, so that the stability of the cellulose dope is improved and the gelation can be effectively prevented; however, a cellulose shaped article (such as a fiber or a film) produced by using the cellulose dope has a disadvanta-geously low mechanical strength. Further, in this case, the strength of the cellulose shaped article during the production thereof is, of course, also low and, hence, it is difficult to produce stably a cellulose shaped article on a commercial scale. In addition, when the sodium hydroxide concentration (CHa) of the cellulose dope is outside of the range of from 6.5 to 11 ~ by weight, the cellulose contained in the cellulose dope cannot be satisfactorily dissolved in the aqueous sodi-um hydroxide solution.
It is generally practiced to obtain the viscosity of a polymer solution as a product of a power function of the polymer concentration of the solution, multi-plied by a power function of the molecular weight of the polymer. This means that when the natural loga-rithmic values of the viscosities are plotted against the natural logarithmic values of the polymer concen-trations or polymer molecular weights, a straight line is obtained. However, the relationship represented by such a straight line is satisfied only when the polymer concentration or polymer molecular weight is within the specific range. In other words, when the polymer con-centration or polymer molecular weight is not in the specific range, the relationship is no longer satisfied.

Specifically, for example, when the polymer concentra-tion or polymer molecular weight exceeds the specific range, the amount of change in the natural logarithmic value of the viscosity becomes markedly large, relative 5 to the amount of change in the natural logarithmic val-ue of the polymer concentration or polymer molecular weight. This is because the above-mentioned relation-ship is satisfied only when the polymer solution is in a state wherein the whole polymer is satisfactorily 10 solvated and neither association nor crosslinking oc-curs in the solution.
The above-mentioned relationship also applies to a cellulose solution (cellulose dope). Specifically, a cellulose dope exhibits a zero-shear viscosity (~o) 15 which satisfies the relationship of formula (1) above, that is, the zero-shear viscosity (~o) of the cellulose dope is a product of the power function of the cellu-lose content (Cc) of the cellulose dope, multiplied by the power function of the viscosity average degree of 20 polymerization (DPc) of the cellulose in the cellulose dope. In the case of the cellulose dope of the, present invention, the ranges of the cellulose content (Cc) and the viscosity average degree of polymerization (DPc) which satisfy formula (1) above are broad, as compared 25 to those in the case of the conventional cellulose dope.

The determination as to whether or not a cellulose dope exhibits a zero-shear viscosity (~o) which satis-fies formula (1) above can be easily conducted by the following method.
First, the weight of the cellulose dope and the zero-shear viscosity (~o) of the cellulose dope are measured. The value of the zero-shear viscosity obtained by the measurement is hereinafter referred to as the "found zero-shear viscosity".
Next, the cellulose in the cellulose dope is pre-cipitated by an appropriate method, such as a method in which the cellulose dope is neutralized by adding an acid to the cellulose dope to thereby precipitate the cellulose contained in the cellulose dope. The pre-cipitated cellulose is recovered and, after the pre-cipitated cellulose is recovered and dried, the weight of the cellulose is measured. The ratio (~ by weight) of the weight of the recovered, dried cellulose to the weight of the cellulose dope is defined as the cellu-lose content (Cc) of the cellulose dope.
Further, the viscosity average degree of polymeri-zation (DPc) of the recovered, dried cellulose is meas-ured.
Then, the obtained cellulose content (Cc) and the obtained viscosity average degree of polymerization (DPc) are substituted in formula (1) above, and the zero-shear viscosity (~o) is calculated with respect to each of the following four cases:
the case where m = 5 and p = 3;
the case where m = 7 and p = 3;
the case where m = 5 and p = 4; and the case where m = 7 and p = 4.
When the found zero-shear viscosity mentioned abo-ve is within the range of from the minimum of the calculated four values of the zero-shear viscosity to the maximum of the four values, this means that the cellulose dope exhibits a zero-shear viscosity (~o) which satisfies formula (1) above.
In the cellulose dope of the present invention, it is preferred that the viscosity average degree of po-lymerization (DPc) of the cellulose is from 350 to 1,200 and that the cellulose content (Cc) is from 5 to 10 ~ by weight. Further, it is preferred that m and p in formula (1) above are, respectively, from 6.3 to 6.5 and from 3.2 to 3.5. The narrowness of the ranges of m and p in formula (1) above means that the cellulose in the cellulose dope of the present invention is highly solubilized.
Conventionally, it was very difficult to produce a cellulose dope having a high content of cellulose hav-ing a high degree of polymerization. Further, it was conventionally considered that the higher the cellulose content and the polymerization degree of the cellulose, the more unstable and susceptible to gelation the cel-lulose dope becomes. However, surprisingly, the cellu-lose dope of the present invention is stable and free from gelation even when it has a high content of cellu-lose having a high polymerization degree.
Hereinbelow, for illustratively showing the essen-tial features of the present invention, the technical features of the present invention are explained by re-viewing how the present invention has been completed.
In the explanation made below, the six carbon atoms of the glucose unit of cellulose are abbreviated as fol-lows:
1-position carbon atom of the glucose unit: C1 2-position carbon atom of the glucose unit: C2 3-position carbon atom of the glucose unit: C3 4-position carbon atom of the glucose unit: C4 5-position carbon atom of the glucose unit: C5 6-position carbon atom of the glucose unit: C6 As mentioned above, cellulose is a polysaccharide having a linear chain comprising a number of D-glucose (D-glucopyranose) units, wherein the mutually adjacent units are bonded to each other through ~-1,4-bond.
Therefore, a cellulose molecule contains a number of hydroxyl groups which are hydrophilic groups and, hence, it is expected that cellulose is highly hydrophilic.
However, actually, cellulose is completely insoluble in water. The reason for this is considered as follows.
In general, when a compound is in a solid state, the distance between mutually adjacent molecules of the compound is small. Therefore, the conformation of the molecules is fixed by the interactions between the molecules, such as intermolecular hydrogen bonds.
However, when the compound is dissolved in a sol-vent, each of the molecules of the compound is sur-rounded by the molecules of the solvent, so that the above-mentioned interactions between the molecules of the compound are eliminated. As a result, the degree of freedom of the conformation of the molecules of the compound is greatly increased. This means that, when a compound in a solid state is dissolved in a solvent to obtain a solution, the entropy of the system comprising the compound and the solvent becomes high, as compared to the entropy of the compound in a solid state.
In other words, when the entropy of the system comprising the compound and the solvent, which is ob-tained by contacting a compound in a solid state with a solvent, becomes not higher than the entropy of the compound in a solid state, it follows that the compound is insoluble in the solvent. In general, the reason 5 for the insolubility of a compound in a solvent is that the affinity between the compound and the solvent is not so high as to eliminate the above-mentioned inter-actions between the molecules of the compound.
However, in the case of cellulose, as mentioned 10 above, cellulose is completely insoluble in water de-spite that a cellulose molecule contains many hydroxyl groups which are hydrophilic groups and, hence, it is expected that cellulose is highly hydrophilic. The reason for this is considered as follows.
15 In cellulose, an intramolecular hydrogen bond is present between two mutually adjacent glucose units of cellulose (i.e., two glucose units of cellulose which are bonded to each other through ~-1,4-bond). Specifi-cally, the intramolecular hydrogen bond is present be-20 tween the hydroxyl group bonded to C3 of one of the above two glucose units and the oxygen atom (which is a ring-forming atom of the 6-membered ring of the glucose unit) bonded to C5 of another one of the above two glu-cose units. As a result, the positional relationship 25 between the two adjacent glucose units is substantially ffixed.
Such intramolecular hydrogen bonds are present in nearly throughout the cellulose molecular chain, so that substantially the whole of the cellulose molecule becomes a rigid, linear molecular chain having a very low degree of freedom of conformation.
In general, the intermolecular hydrogen bonds are easily broken by water. Also in the case of cellulose, hydrogen bonds between molecules of cellulose are easi-1y broken by water, so that the cellulose is swelled with water. On the other hand, in general, the in-tramolecular hydrogen bonds are not broken by water.
Also in the case of cellulose, when cellulose is con tacted with water, the intramolecular hydrogen bonds in the cellulose are not broken and, hence, the cellulose molecule continues to be in the form of a rigid, linear molecular chain, which means that the degree of freedom of the conformation of the cellulose molecule remains low. Therefore, when cellulose in a solid state is contacted with water, the entropy of the system com-prising the cellulose and the water is not higher than that of the cellulose in a solid state. Accordingly, the cellulose is swelled with water but is insoluble in water.
As can be seen from the above, for dissolving cel-lulose in a solvent to obtain a cellulose dope, it is necessary to increase the degree of freedom of the con-formation of the molecule of the cellulose by breaking the above-mentioned intramolecular hydrogen bonds in the cellulose.
It should be noted that, when the degree of break-down of the intramolecular hydrogen bonds in the cellu-lose is unsatisfactory, cellulose (in the solution) having a high degree of freedom of the conformation im-mediately reverts to insoluble cellulose having a low degree of freedom of the conformation, so that the cel-lulose dope becomes unstable and susceptible to gela-tion. Therefore, for producing a cellulose dope which is stable and free from gelation, it is necessary to break the intramolecular hydrogen bonds in the cellu-lose as much as possible, and it is preferred to break all of the intramolecular hydrogen bonds in the cellu-lose.
It should also be noted that the higher the degree of breakdown of the intramolecular hydrogen bonds in the cellulose, the lower the viscosity of the produced cellulose dope becomes. Therefore, also from a view-point of producing a cellulose dope having a high proc-essability, it is necessary to break the intramolecular hydrogen bonds in the cellulose as much as possible, and it is preferred to break all of the intramolecular hydrogen bonds in the cellulose.
As a representative example of methods for break-ing the intramolecular hydrogen bonds in the cellulose, there can be mentioned a chemical modification method in which the cellulose is subjected to chemical modifi-cation to thereby prevent the formation of intramolecu-lar hydrogen bonds in the cellulose. Since, as men-tinned above, the hydroxyl group bonded to C3 is di-rectly involved in the formation of the intramolecular hydrogen bonds in the cellulose, the formation of in-tramolecular hydrogen bonds in the cellulose can be prevented by modifying the above-mentioned hydroxyl group. Further, by modifying the hydroxyl group bonded to C2, the formation of the intramolecular hydrogen bonds in the cellulose can be indirectly prevented.
As specific examples of this chemical modification method, there can be mentioned the above-mentioned vis-cose process and the above-mentioned cuprammonium proc-ess, both of which are the methods for producing regen-erated cellulose shaped articles which are commercially important.
In the case of the cuprammonium process, cellulose is bonded to the copper in a cuprammonium solution to form a complex. In this case, both of the hydroxyl group bonded to C3 and the hydroxyl group bonded to C2 are involved in the formation of the complex, so that the intramolecular hydrogen bonds in the cellulose are broken.
It is considered that, in a cellulose dope which is actually used in the cuprammonium process, substan-tially all of the intramolecular hydrogen bonds in the cellulose are broken, so that the stability and proc-essability of the cellulose dope are very high. Spe-cifically, it is considered that, when kept in a closed vessel, the cellulose dope remains stable for several years. The cellulose dope also has a low viscosity and a very high fluidity, so that the cellulose dope has a very high stringiness.
On the other hand, in the viscose process, which is more frequently employed on a commercial scale than the cuprammonium process, the intramolecular hydrogen bonds in the cellulose are broken by reacting the hy-droxyl group in the cellulose with carbon disulfide to form a xanthogenic acid ester.
However, in a cellulose dope (viscose) which is actually used in the viscose process, only 30 ~ by weight or less of the sum of the hydroxyl groups bonded to C3 atoms in the cellulose and the hydroxyl groups bonded to C2 atoms in the cellulose are esterified to form a xanthogenic acid ester. Therefore, a substan-tial amount of the intramvlecular hydrogen bonds remain in the cellulose molecules dissolved in the cellulose dope and, hence, the stability and processability of 5 the cellulose dope are low. Specifically, the cellu-lose dope is gelled within a few days after the produc-tion thereof.
Taking into consideration the above-mentioned con-ventional knowledge about the solubilization of cellu-10 lose, the present inventors have made extensive and in-tensive studies with a view toward developing a cellu-lose dope which not only has a high content of cellu-lose having a high degree of polymerization, but also is stable and free from gelation. As a result, it has 15 been found that, when a cellulose dope comprising an aqueous sodium hydroxide solution and cellulose dis-solved in the solution exhibits a zero-shear viscosity which satisfies the above-mentioned formula (1), the cellulose dope is stable and free from gelation 20 even if the cellulose dope has a high content of cellu-lose having a high degree of polymerization.
In the present invention, it is preferred that, in the NMR analysis of the cellulose dope, the 6-position carbon atoms (C6) of the glucose units of the cellulose 25 exhibit a longitudinal relaxation time (ic) of from 10 to 400 ms, more advantageously from 10 to 200 ms. It is also preferred that, in the NMR analysis of the cel-lulose dope, the 1-position carbon atoms (C1) of the glucose units of the cellulose exhibit a longitudinal relaxation time (ic) of from 200 to 10,000 ms.
The longitudinal relaxation time (ic) of a carbon atom in the cellulose dope is an index of the degree of the vigorousness of the movement of the carbon atom.
More specifically, a carbon atom which moves vigorously has a large is value; and a carbon atom which moves slightly or exhibits substantially no movement has a small is value.
It is possible that the movement of a carbon atom in the cellulose dope is impeded by various factors, such as the intramolecular and/or intermolecular hydro-gen bonds in the cellulose. In this case, the longitu-dinal relaxation time (ic) of the carbon atom becomes short. Therefore, the higher the degree of breakdown of the intramolecular and/or intermolecular hydrogen bonds and the higher the degree of freedom of the con-formation of the cellulose molecule (in other words, the higher the solubility of the cellulose and the more stable and susceptible to gelation the cellulose dope), the larger the is values of the carbon atoms of the glucose units of the cellulose become.

When the degree of breakdown of the above-mentioned intramolecular hydrogen bonds in the cellu-lose is high and the cellulose molecule has a high de-gree of freedom of the conformation, the entire cellu-lose molecule becomes highly flexible and able to move relatively freely as in the case of a general linear polymer. Therefore, when the degree of breakdown of the above-mentioned intramolecular hydrogen bonds in the cellulose is high and the cellulose molecule has a high degree of freedom of the conformation, C1 present in the main chain of the cellulose has a large zc value.
By contrast, the higher the solubilization of the cellulose, the smaller the is value of C6 becomes. The reason for this is considered as follows.
With respect to the position of C6 in the struc-ture of cellulose, C6 is present in a side chain bonded to a molecular chain comprising C1 to C5 and oxygen atoms. Therefore, even if cellulose as a whole has a relatively low degree of freedom of the conformation, the degree of freedom of the conformation of C6 is re-latively high. On the other hand, when cellulose is highly solubilized, C6 is surrounded by a large number of the molecules of a solvent (water) due to the solva-tion, so that the movement of C6 is impeded (that is, the degree of freedom of the conformation of C6 becomes low). As a result, the is value of the C6 becomes s-mall.
With respect to the gelation of a cellulose dope, this phenomenon can be understood as a phase separation (precipitation of cellulose) occurring at a microscopic level. The above phase separation means the separation (by precipitation) of cellulose from the system com-prising the independent microphases of cellulose which are separated from each other through water and the like. When the gelation occurs, the molecules of water surrounding the cellulose are separated from the cellu-lose, so that the above-mentioned intramolecular and intermolecular hydrogen bonds in the cellulose are re-formed. As a result, the degree of freedom of the conformation of cellulose as a whole is lowered. How-ever, in the case of C6, the movement of C6 is no lon-ger impeded by the molecules of water surrounding the cellulose, so that the degree of freedom of the confor-mation of C6 becomes high.
As can be seen from the above, the cellulose dope of the.present invention has a characteristic that the higher the solubilization of the cellulose in the cel-lulose dope, the more vigorous the movement of C1 be-comes and the less vigorous the movement of C6 becomes.
The cellulose dope of the present invention can be produced by a method comprising the following steps (1) to (3):
(1) providing a cellulose slurry comprising an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average parti-cle diameter of 30 ~.m or less, the cellulose slurry having a sodium hydroxide concentration of from 0.5 to less than 6.5 ~ by weight and a cellulose content of 5 ~ by weight or more, (2) adjusting the sodium hydroxide concentration of the cellulose slurry to 6.5 to 11 ~ by weight, and (3) stirring the cellulose slurry at 10 °C or less by means of a stirrer under stirring conditions satis-fying at least one requirement selected from the group consisting of the requirement that the stirring is per-formed at a shear rate of 9,000/sec or less and the re-quirement that the stirring is performed at a stirring speed of 500 m/min or less in terms of the speed at which the outer end of an agitating element of the stirrer is rotated, the steps (2) and (3) being conducted in the order of step (2) and step (3) or simultaneously, thereby causing the particulate cellulose to be dissolved in the cellulose slurry to the extent that the cellulose has a dissolution ratio of 99.0 ~ by weight or more, to obtain a cellulose dope, wherein the cellulose slurry satisfies the follow-ing formula (2):
cT - KlexP (klCNa) (2) 5 wherein:
aT represents the yield stress (Pa) of the slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and 10 CNa is the sodium hydroxide concentration (~ by weight) of the slurry, and wherein, in the solid state NMR analysis of the slurry, the cellulose in the slurry exhibits a non-crystallinity (xam) of 0.5 or more, the non-15 crystallinity being defined by the following formula (3):
xam - Ihigh ~ ( Ihigh + Ilow) ( wherein:
xam is the non-crystallinity of the cellulose 20 in the slurry, and Ihigh and IloW respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of the slurry, wherein the peaks are, respectively, ascribed to the higher magnetic 25 field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in the slurry, and wherein separation between the peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of the peaks is approximated to the Gaussian dis-tribution function.
First, an explanation is made with respect to the above-mentioned step (1).
In the step (1) is provided a cellulose slurry which comprises an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average particle diameter of 30 Eun or less and which has a sodium hydroxide concentration of from 0.5 to less than 6.5 ~ by weight and a cellulose content of 5 ~ by weight or more.
Examples of celluloses used for preparing the cel-lulose slurry include natural cellulose, such as pulp, cotton and cotton linter; and regenerated cellulose ob-tained from a cellulose solution, such as viscose or a cupurammonium solution of cellulose. These celluloses can be used individually or in combination.
When it is intended to use the slurry of natural cellulose for producing a cellulose dope containing highly solubilized cellulose, it is preferred to use, as the natural cellulose, a sulfite process dissolving pulp obtained by pulping by the sulfite process. When natural cellulose (such as a kraft process dissolving pulp) obtained by another method is used in the cellu-lose slurry, it is likely to become difficult to satis-factorily solubilize the cellulose. The reason for this is considered as follows. As mentioned above, the higher the degree of breakdown of the intramolecular hydrogen bonds in cellulose, the higher the solubiliza-tion of the cellulose becomes. Therefore, it is con-sidered that the high solubility of the sulfite process dissolving pulp is caused by the high degree of break-down of the intramolecular hydrogen bonds in the pulp.
In fact, with respect to the degree of breakdown of the intramolecular hydrogen bonds, a sulfite process dis-solving pulp has a higher degree than that of a kraft process dissolving pulp.
The viscosity average degree of polymerization (DPc) of cellulose is an important parameter for con-trolling the solubility of the cellulose. Examples of methods for adjusting the DPc value of cellulose in-elude a steam explosion method, an acid hydrolysis, an alkali hydrolysis, an electron ray irradiation method, a y-ray irradiation method and a mechanical pulveriza-tion (including a wet pulverization). However, in the alkali hydrolysis, when cellulose is contacted with an aqueous alkali solution having a high alkali concentra-tion, there is a danger that the cellulose cannot be highly solubilized due to the formation of an insoluble substance. For example, in the alkali hydrolysis using an aqueous sodium hydroxide solution, when the alkali concentration of the aqueous sodium hydroxide solution is 10 ~ by weight or more, a part of the cellulose is converted to an alkali cellulose. The alkali cellulose is insoluble in the aqueous sodium hydroxide solution, so that it becomes difficult to solubilize the cellu-lose highly.
When the viscosity average degree of polymeriza-tion (DPc) of cellulose is adjusted by the steam explo-sion method, it is possible to obtain cellulose having a high degree of breakdown of the intramolecular hydro-gen bonds, as compared to that of a kraft process dis-solving pulp.
When a sulfite process dissolving pulp or regener-ated cellulose is used in the cellulose slurry, in many cases, the adjustment of the DPc value of the material cellulose is not necessary.
The viscosity average degree of polymerization (DPc) of cellulose in the cellulose slurry varies de-pending on various factors, such as the desired proper-ties of a cellulose shaped article to be produced, and the desired degree of the stability of the cellulose dope during the course of the production. It is preferred that the viscosity average degree of polym-erization (DPc) is from 350 to 1,200, more advanta-geously from 400 to 1,000. When the viscosity average degree of polymerization (DPc) is less than 350, the mechanical strength of a cellulose shaped article pro-duced becomes low.
The above-mentioned cellulose is dispersed in an aqueous sodium hydroxide solution so as to obtain a cellulose slurry which contains particulate cellulose having an average particle diameter of 30 ~.m or less, preferably 20 Eun or less, and which has a sodium hy-droxide concentration of from 0.5 to less than 6.5 $ by weight and a cellulose content of 5 ~ by weight or more.
The above-mentioned operation for dispersing the cellulose in the aqueous sodium hydroxide solution is conducted so as to increase the surface area of the cellulose, thereby increasing the rate of dissolution of the cellulose. On this point, an explanation is made below. The rate of dissolution of cellulose into an aqueous alkali solution is markedly low, as compared to the rate of dissolution of cellulose into an aqueous cuprammonium solution or an aqueous Cadoxen solution.
Therefore, when cellulose is added to an aqueous alkali solution and the resultant mixture is allowed to stand, 5 the dissolution of the cellulose apparently stops.
Therefore, it is necessary to promote the dissolution of the cellulose by stirring. However, for the reason mentioned below, it is not preferred to stir at a high speed in the step for dissolving the cellulose into the 10 aqueous alkali solution. In the present invention, the surface area of the cellulose is increased so as to en-able the dissolution of the cellulose into the aqueous alkali solution by stirring at a low speed.
When the particulate cellulose has an average par-15 ticle diameter of more than 30 Vim, not only is the dis-solution ratio (Sc) of the cellulose low, but also the cellulose dope has low stability and is susceptible to gelation.
As a method for obtaining the cellulose slurry, 20 there can be mentioned wet pulverization. With respect to the wet pulverization, an explanation is made below.
The wet pulverization is a method in which cellu-lose is subjected to pulverization in an aqueous medium, thereby obtaining a slurry comprising particulate cel-25 lulose having a desired particle size dispersed in the aqueous medium.
Examples of aqueous media include water and an aqueous sodium hydroxide solution having a sodium hy-droxide concentration of less than 6.5 ~ by weight, preferably from 2 to 5 ~ by weight. When the wet pul-verization of cellulose is conducted in an aqueous so-dium hydroxide solution having a sodium hydroxide con-centration of 6.5 $ by weight or more, the cellulose is partially and heterogeneously dissolved in the solution, so that the dissolution ratio (Sc) of the cellulose in the cellulose dope is markedly low.
As specific methods for performing the wet pul-verization for increasing the surface area of the cel-lulose, there can be mentioned a method in which cellu-lose is pulverized into particles and a method in which cellulose is pulverized into microfibrils by the use of a stone mill type wet pulverizer or the like. Of these two methods, the former is employed in the present in-vention.
The slurry obtained by the former has a low vis-cosity. Therefore, it is easy to conduct a homogeneous and efficient stirring in the step for dissolving the cellulose in the slurry.
On the other hand, when the latter is employed, a slurry containing microfibrillated cellulose is ob-tained. Such a slurry has a very high viscosity and exhibits gelation even when the slurry has a low con-tent of cellulose solids. Therefore, the slurry is disadvantageous in that it is difficult to stir the slurry in the step for dissolving the cellulose in the slurry.
With respect to the apparatus used for the wet pulverization, there is no particular limitation as long as the apparatus is capable of pulverizing cellu-lose to the extent that the average particle diameter of the cellulose becomes 30 ~n or less, preferably 20 ~.m or less. Preferred examples of such apparatuses in-clude a stirred medium wet grinding apparatus described in Unexamined Japanese Patent Application Laid-Open Specification No. 3-163135.
With respect to the amounts of the cellulose and the aqueous medium used in the wet pulverization, there is no particular limitation. However, when the slurry obtained by the wet pulverization has a cellulose con-tent of more than 15 ~ by weight, it is likely that the viscosity of the slurry becomes markedly high, so that the handling of the slurry becomes difficult. There-fore, generally, the amounts of the cellulose and the aqueous medium are adjusted so that the slurry has a cellulose content of 15 ~ by weight or less.

When the thus obtained slurry has a sodium hydrox-ide concentration of from 0.5 to less than 6.5 ~ by weight, the obtained slurry as such can be used as the cellulose slurry in the steps (2) and (3) (which are mentioned above and explained below in detail). If de-sired, prior to the steps (2) and (3), the sodium hy-droxide concentration of the slurry may be further ad-justed within the above-mentioned range. On the other hand, when the obtained slurry has a sodium hydroxide concentration of less than 0.5 ~ by weight, a high con-centration aqueous sodium hydroxide solution or solid sodium hydroxide is added to the slurry so as to adjust the sodium hydroxide concentration to be in the range of from 0.5 to less than 6.5 ~, and the resultant slur-ry is used as the cellulose slurry in the steps (2) and (3).
With respect to the cellulose content of the cel-lulose slurry, the content needs to be adjusted to 5 ~
by weight or more. When the content is less than 5 ~
by weight, the cellulose dope obtained has a disadvan-tageously low cellulose content (Cc), so that it be-comes difficult to produce from the cellulose dope a cellulose shaped article having a strength sufficient for practical use.
It is required that the above-mentioned cellulose slurry satisfy the following formula (2):
QT - KlexP (klCNa) (2) wherein:
~T represents the yield stress (Pa) of the slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and CNa is the sodium hydroxide concentration (~ by weight) of the slurry.
The above-mentioned formula (2) means that, when the natural logarithmic values of the yield stresses (~T) of the slurry are plotted against the sodium hy-droxide concentration (CNa) values of the slurry, a straight line having a gradient of 0 or less is ob-tained. The formula (2} also shows that, when the so-dium hydroxide concentration (CNa} of the slurry in-creases, the yield stress (oT) of the slurry decreases or does not change and, hence, the viscosity of the slurry decreases or does not change. This feature is one of the essential features of the present invention and, as explained below, is quite unexpected.
In general, in a conventional slurry obtained by dispersing a substance in a particulate form in a solu-tion, the viscosity of the slurry increases as the con-centration of the solution increases. Therefore, the above-mentioned slurry satisfying the above-mentioned formula (2) has a quite unexpected property, completely differing from the case of the conventional slurry.
By virtue of this property, in the method of the 5 present invention, vigorous stirring is not necessary in the step for dissolving the cellulose in the slurry This is considered to contributes to the establishment of the effect of the method of the present invention, i.e., the effect that it is possible to produce a cel-10 lulose dope which has a high content of cellulose hav-ing a high degree of polymerization and which is stable and free from gelation .

The determination as to whether or not a cellulose slurry satisfies formula (2) above can be easily con-ducted by the following method.
First, the weight of the cellulose slurry and the yield stress of the cellulose slurry are measured. The found value of the yield stress is denoted as "QT1".
Next, a portion of the slurry is weighed and then, subjected to an appropriate analysis, such as neutrali-zation titration, to determine the sodium hydroxide concentration of the slurry. The found value of the sodium hydroxide concentration is denoted as "CNal".
Further, another portion of the slurry is taken, and an appropriate amount of sodium hydroxide is added to the taken slurry, thereby obtaining an additional sodium hydroxide-containing slurry. The sodium hydrox-ide concentration of the additional sodium hydroxide-containing slurry is denoted as "CNa2". This can be easily calculated from the above-mentioned CNal.
Then, the yield stress of the additional sodium hydroxide-containing slurry is measured. The found value of the yield stress of the additional sodium hy-droxide-containing slurry is denoted as "QT2".
Based on the thus obtained values QT1, aT2, CNal and CNa2, the natural logarithmic values of the yield stresses of the slurry (i.e., the natural logarithmic values of aTl and QT2) are plotted against the sodium hydroxide concentrations (not logarithmic values) (i.e., CNal and CNa2) to obtain a straight line. When the gradient of the straight line is 0 or less, it follows that the cellulose slurry satisfies formula (2) above.
Usually, the cellulose slurry obtained by the above-mentioned wet pulverization satisfies formula (2) above.
Further, in the solid state NMR analysis of the above-mentioned cellulose slurry used in the present invention, the cellulose in the slurry exhibits a non-crystallinity (xam) of 0.5 or more, wherein the non-crystallinity is defined by the following formula (3):
Ihigh ~ ( Ihigh + Ilow) ( 3 ) wherein:
xam is the non-crystallinity of the cellulose in the slurry, and Ihigh and Ilow respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of the slurry, wherein the peaks are, respectively, ascribed to the higher magnetic field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in the slurry, and wherein separation between the peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of the peaks is approximated to the Gaussian dis-tribution function.
The non-crystallinity xam of the cellulose in the slurry corresponds to the ratio of a specific region in the cellulose wherein the specific region indicates a portion in which the conformation of the cellulose mo-lecules has a high degree of freedom.
As mentioned above, the degree of freedom of con-formation of cellulose molecules is extremely low, but the degree of freedom is not zero. That is, the cellu-lose molecules have regions having a high degree of freedom of conformation as well as regions having a low degree of freedom of conformation. Needless to say, the solubilization of cellulose is achieved by increas-ing the ratio of the regions having a high degree of freedom of conformation.
The ratio of the regions having a high degree of freedom of conformation and the regions having a low degree of freedom of conformation can be determined from the areas of peaks observed in a solid state 13C-NMR spectrum of the above-mentioned slurry, which peaks are ascribed to the 4-position carbon atoms (C4) of the glucose units of the cellulose in the slurry.
Usually, in the above-mentioned solid state NMR
spectrum of the slurry, two peaks are observed in the range of from 85 to 95 ppm. Of these two peaks, the peak observed in the higher magnetic field is ascribed to the 4-position carbon atoms (C4 atoms) of the gluco-se units present in the regions having a high degree of freedom of conformation (such carbon atoms are collec-tively referred to as the "higher magnetic field compo-nent"). On the other hand, the peak observed in the lower magnetic field is ascribed to the 4-position car-bon atoms (C4 atoms) of the glucose units present in the regions having a low degree of freedom of conforma-tion (such carbon atoms are collectively referred to as the "lower magnetic field component"). Generally, the area of a peak observed in an NMR spectrum is propor-tional to the number of atoms (carbon atoms in the case of the above solid state 13C-NMR spectrum) to which the peak is ascribed. Therefore, the ratio between the re-gions having a high degree of freedom of conformation and the regions having a low degree of freedom of con-formation is approximately the same as the ratio be-tween the area of the peak observed in the higher mag-netic field and the area of the peak observed in the lower magnetic field. For this reason, the non-crystallinity Xam of the cellulose in the slurry can be used as an index of the degree of freedom of conforma-tion of cellulose molecules.
5 However, usually, the above-mentioned two peaks (respectively ascribed to the higher magnetic field component and the lower magnetic field component) in the solid state NMR spectrum overlap, so that the cor-rect ratio between the peak areas cannot be directly 10 obtained from the solid state NMR spectrum. For this reason, separation between the two peaks is made using a method in which each of the peaks is approximated to the Gaussian distribution function. Such a method for separation is an established method in this field and 15 can be easily conducted by computer processing of the data of the above-mentioned solid state NMR spectrum.
With respect to the above-mentioned slurry used in the present invention, the above-mentioned non-crystallinity Xam of the cellulose is as high as 0.5 or 20 more.
For example, when the cellulose slurry used in the present invention is prepared by using an aqueous sodi-um hydroxide solution having a sodium hydroxide concen-tration of 2 ~ by weight, the non-crystallinity xam of 25 the cellulose in the resultant slurry is as high as 0.6.

On the other hand, when a cellulose slurry is prepared by using water instead of the aqueous sodium hydroxide solution, the non-crystallinity Xam of the cellulose in the resultant slurry is as low as about 0.45. This clearly shows that the cellulose in the slurry produced by using an aqueous sodium hydroxide solution has a very high degree of freedom of conformation, as com-pared to that of the cellulose in the slurry produced by using water instead of the aqueous sodium hydroxide solution.
It is considered that this high non-crystallinity xam of the cellulose contributes to the establishment of the above-mentioned unique relationship between the yield stress ~T of the slurry and the sodium hydroxide concentration CNa of the slurry.
Usually, in the solid state NMR analysis of the cellulose slurry obtained by the above-mentioned wet pulverization, the cellulose in the slurry exhibits a non-crystallinity xam of 0.5 or more.
In the present invention, it is preferred that the above-mentioned cellulose slurry satisfies the follow-ing formula (4):
QT = K2 + k2DPc (4) wherein:
6T represents the yield stress (Pa) of the slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in the slurry.
Formula (4) above means that, when the values of yield stresses (aT) are plotted against the values of viscosity average degrees (DPc) of polymerization of the cellulose, a straight line having a slope of 0 or less is obtained. In other words, formula (4) above means that, when the viscosity average degree DPc of polymerization of the cellulose increases, the yield stress (QT) of the cellulose slurry does not change or decrease and, accordingly, the viscosity of the cellu-lose slurry does not change or decrease. As explained below, it is surprising that the above-mentioned cellu-lose slurry exhibits such a unique characteristic.
In general, in a conventional slurry obtained by dispersing particulate polymer, the viscosity of the slurry increases as the molecular weight (or degree of polymerization) of the polymer increases. Therefore, the above-mentioned cellulose slurry satisfying formula (4) above has a quite unexpected characteristic, which is completely different from that of the conventional cellulose slurry.
The determination as to whether or not a cellulose slurry satisfies formula (4) above can be easily con-ducted by the following method.
First, the weight of the cellulose slurry and the yield stress of the cellulose slurry are measured. The found value of the yield stress is defined as "QT3".
Next, a portion of the slurry is weighed and then, subjected to an appropriate analysis, such as neutrali-zation titration, to determine the sodium hydroxide concentration of the slurry. The found value of the sodium hydroxide concentration is denoted as "CNa3".
Further, another portion of the slurry is taken and subjected to vacuum drying. The weight of the re-sultant residue (containing particulate cellulose and sodium hydroxide) is measured, and the cellulose con-tent of the slurry is calculated from the weight of this residue and the above-mentioned CNa3. The ob-tamed value of the cellulose content is denoted as "Ccs3".
Next, using the above-obtained residue, the vis-cosity average degree of polymerization of the particu-late cellulose in the cellulose slurry is measured.
The found value of the viscosity average degree of polymerization is denoted as "DPcl".

Further, using particulate cellulose having a vis-cosity average degree DPc2 (x DPcl) of polymerization, a cellulose slurry having a cellulose content of Ccs3 and a sodium hydroxide concentration of CNa3 is pre-y pared by the above-mentioned wet pulverization, and the yield stress of the resultant slurry is measured. The found value of the yield stress is denoted as "~T4".
The above-obtained values of yield stresses of the slurry (i.e., QT3 and aT4) are plotted against the above-obtained values of viscosity average degrees of polymerization (i.e., DPcl and DPc2), so as to obtain a straight line. When the gradient of the straight line is 0 or less, it follows that the cellulose slurry sat-isfies formula ( 4 ) above.
In many cases, the cellulose slurry obtained by the above-mentioned wet pulverization satisfies formula (4) above.
With respect to the cellulose molecules in the cellulose slurry obtained by the above-mentioned method, the degree of breakdown of the intramolecular hydrogen bonds is considerably high, so that the cellulose in the slurry has a high degree of freedom of conformation.
As a result, the solubility of cellulose (present in the cellulose slurry) in an aqueous sodium hydroxide solution becomes relatively high, so that the cellulose slurry can be used for producing a cellulose dope which has dissolved therein, in a high concentration, a cel-lulose having a high degree of polymerization, and which cellulose dope is stable and free from gelation.
5 The reason for this high degree of breakdown of the intramolecular hydrogen bonds in the cellulose mo-lecules present in the cellulose slurry obtained by the above-mentioned method has not yet been elucidated.
However, it is possible that the above-mentioned high 10 degree of breakdown of the intramolecular hydrogen bonds has a correlation with the observation results of the Raman spectrum of an aqueous sodium hydroxide solu-tion and the NMR spectrum of a conventional cellulose dope, which observation results are reported in the 15 documents described below.
The positions of peaks (representing the stretch-ing vibration of an O-H group and the deformation vi-bration of an O-H group) observed in the Raman spectrum of an aqueous sodium hydroxide solution having a sodium 20 hydroxide concentration in the range of from 2 to 5 ~
by weight are slightly different from those of peaks observed in the Raman spectrum of an aqueous sodium hy-droxide solution having a sodium hydroxide concentra-tion outside the above-mentioned range (Polymer Journal, 25 20, 447 (1988)). The reason for this is presumed as fO110WS.
Generally, in an aqueous sodium hydroxide solution having a sodium hydroxide concentration of 6 ~ by weight or less, each sodium ion is hydrated with 4 mo-les or more of water molecules by coordination. When the sodium hydroxide concentration is in the range of from 2 to 5 ~ by weight, energy exchange occurs between water molecules coordinated to sodium ions (coordinated water) and water molecules not coordinated to sodium ions (free water), which energy exchange causes the change in the positions of peaks observed in a Raman spectrum.
Further, the NMR spectrum of a conventional cellu-lose dope suggests that the electron densities around the atomic nuclei of C2 and C3 change due to the presence of sodium ions positioned close to the hy-droxyl group bonded to C2 (Polymer Journal, 17, 707(1985)).
Next, an explanation is made with respect to the above-mentioned steps (2) and (3) of the method of the present. invention.
In the above-mentioned step (2), the sodium hy-droxide concentration of the cellulose slurry provided in the above-mentioned step (1) is adjusted to 6.5 to 11 ~ by weight.

In the above-mentioned step (3), the cellulose slurry is stirred at 10 °C or less by means of a stir-rer under stirring conditions satisfying at least one requirement selected from the group consisting of the requirement that the stirring is performed at a shear rate of 9,000/sec or less and the requirement that the stirring is performed at a stirring speed of 500 m/min or less in terms of the speed at which an outer end of an agitating element of the stirrer is rotated, thereby causing the particulate cellulose to be dissolved in the cellulose slurry to the extent that the cellulose has a dissolution ratio of 99.0 ~ by weight or more, to obtain a cellulose dope.
The above-mentioned steps (2) and (3) can be con-ducted in the order of step (2) and step (3) or simul-taneously.
In step (2) of the method of the present invention, it is preferred that the sodium hydroxide concentration of the cellulose slurry is adjusted by the following method.
First, the cellulose slurry provided in the above-mentioned step (1) is cooled to 10 °C or less, usually to a temperature in the range of from 0 to -3 °C. Sub-sequently, to the resultant cellulose slurry is added an aqueous sodium hydroxide solution which has been cooled to 10 °C or less, usually to a temperature in the range of from -10 to -18 °C, so as to adjust the sodium hydroxide concentration of the cooled cellulose slurry to 6.5 to 11 ~ by weight, preferably 7 to 10 ~
by weight.
The sodium hydroxide concentration of the above-mentioned aqueous sodium hydroxide solution is appro-priately selected so as to obtain a cellulose dope hav-ing a desired sodium hydroxide concentration. However, it is generally in the range of from 10 to 45 ~ by weight.
It is especially preferred that the aqueous sodium hydroxide solution is cooled to a temperature as low as possible, as long as the aqueous sodium hydroxide solu-tion does not freeze. However, generally, the solution is cooled to a temperature in the range of from -10 to -18 °C, and it is not necessary to cool the solution to a temperature lower than this range. The cooling of the solution to the above-mentioned temperature range can be easily conducted by cooling the aqueous sodium hydroxide solution by means of a conventional freezer.
When the above-mentioned aqueous sodium hydroxide solution is cooled (by means of a freezer) to a tem-perature in the range of from -10 to -18 °C, the solu-tion may freeze depending on the sodium hydroxide con-centration of the solution. In such a case, the solu-tion is cooled to a temperature as low as possible within the range of from less than 10 °C to -10 °C, at which the solution does not freeze.
After the sodium hydroxide concentration of the cellulose slurry is adjusted by the above-mentioned method, the cellulose slurry is stirred by means of a stirrer, thereby causing the particulate cellulose to be dissolved in the cellulose slurry, to obtain a cel-lulose dope.
This operation must be conducted at a temperature of 10 °C or less. When this operation is conducted at a temperature of more than 10 °C, the particulate cel-lulose is not satisfactorily solubilized, so that the resultant cellulose dope becomes unstable and suscep-tible to gelation.
Further, the stirring of the cellulose slurry by means of a stirrer is conducted under stirring condi-tions satisfying at least one requirement selected from the group consisting of the requirement that the stir-ring is performed at a shear rate of 9,000/sec or less and the requirement that the stirring is performed at a stirring speed of 500 m/min or less in terms of the speed at which the outer end of an agitating element of the stirrer is rotated.

The speed at which the outer end of an agitating element of the stirrer is rotated can be obtained by the following formula:
5 Speed at which the outer end of an agitating element of the stirrer is rotated (m/min) - revolution rate (rpm) of the agitating element of the stirrer diameter (m) of the agitating element of the stirrer 3.14 The above-mentioned shear rate corresponds to the value obtained by dividing the above-mentioned speed (at which the outer end of an agitating element of the stirrer is rotated) by the distance between the outer end of an agitating element of the stirrer and the in-ner wall of an agitating vessel (in which the cellulose slurry is stirred) equipped with the stirrer.
The rate of dissolution of cellulose into an aque-ous alkali solution is markedly lower than the rate of dissolution of cellulose into an aqueous cuprammonium solution or an aqueous Cadoxen solution. Therefore, when cellulose is added to an aqueous alkali solution and the resultant mixture is allowed to stand without stirring, the dissolution of the cellulose apparently stops, so that the dissolution ratio (Sc) of the cellu-lose becomes only less than 50 ~. Therefore, it is ne-cessary to promote the dissolution of the cellulose by stirring.
In general, if the stirring is performed by means of a mixer or the like capable of stirring at a high speed, the dissolution rate can be increased. However, when a high speed stirring is performed, even if the average temperature of the whole system is kept at 10 °C or less, a local heat generation occurs, so that the stability of the resultant cellulose dope is lowered and gelation is likely to occur. Further, with respect to the solubility of the cellulose in an aqueous alkali solution, the higher the temperature of the cellulose, the lower the solubility of the cellulose becomes.
Therefore, it is not preferred that the temperature of a cellulose slurry is elevated due to a local heat gen-eration accompanying a high speed stirring.
For these reasons, in the present invention, it is required that the stirring of a cellulose slurry be performed at a low speed.
The above-mentioned cellulose slurry satisfies formula (2) above and, preferably, both of formula (2) above and formula (4) above. This means that, the above-mentioned cellulose slurry has a characteristic that, even if the sodium hydroxide concentration (CNa) of the slurry is increased, the viscosity of the slurry does not increase, and that it is preferred that, in addition to the above characteristic, the above-mentioned cellulose slurry has a characteristic that, even if the viscosity average degree of polymerization (DPc) of the cellulose is increased, the viscosity of the slurry does not increase. Accordingly, by using the above-mentioned cellulose slurry, a cellulose dope which is stable and unlikely to exhibit gelation can be obtained.
In the present invention, there is no particular limitation with respect to the stirrer for conducting the above-mentioned stirring, as long as the stirrer is capable of stirring the cellulose slurry under the above-mentioned stirring conditions. Examples of stir-rers which can be used in the present invention include a single-screw kneader and a twin-screw kneader. The above-mentioned stirring can be conducted either in a batchwise manner or in a continuous manner.
For easy understanding of the importance of the above-described stirring conditions, an illustrative explanation is made below with respect to the relation-ship between the stirring conditions for dissolving the cellulose in a cellulose slurry and the stability of the resultant cellulose dope.
Taken as an example is the preparation of a cellu-lose dope which contains cellulose having a viscosity average degree of polymerization (DPc) of 450 and which has a cellulose content (Cc) of 5 ~ by weight. In this case, when a cellulose slurry is subjected to a high speed stirring by using a stirrer under stirring condi-tions wherein the stirring is performed at a shear rate of 17,000/sec and a stirring speed of 1,020 m/min in terms of the speed at which the outer end of an agitat-ing element of the stirrer is rotated (wherein as a stirrer, T. K. HOMO-MIXER, manufactured and sold by TO-KUSHU KIKA KOGYO Co., Ltd., Japan, is used under condi-tions that the revolution rate of the agitating element thereof is set at 12,000 rpm), or when a cellulose slurry is subjected to a high speed stirring by using a stirrer under stirring conditions wherein the stirring is performed at a shear rate of 9,400/sec and a stir-ring speed of 570 m/min in terms of the speed at which the outer end of an agitating element of the stirrer is rotated (wherein as a stirrer, S-1 Mixer SMJ-40 (equipped with a stirring vessel having an internal volume of 64 ml), manufactured and sold by SAKURA SEI-SAKUSHO Ltd., Japan, is used under conditions that the revolution rate of the agitating element thereof is set at 4,500 rpm), even if the average temperature of the slurry is kept at -2 °C or less during the stirring for dissolving the cellulose, gelation proceeds immediately after the dissolution of the cellulose (i.e., prepara-tion of a cellulose dope) and, hence, the desired cel-lulose dope cannot be obtained.
On the other hand, when the same procedure as de-scribed above for preparing the above-mentioned cellu-lose dope is performed except that the cellulose slurry is subjected to a low speed stirring under stirring conditions wherein the stirring is performed at a shear rate of 2,000/sec and a stirring speed of 120 m/min in terms of the speed at which the outer end of an agitat-ing element of the stirrer is rotated, the resultant cellulose dope is stable for one week or more and free from gelation, and the dissolution ratio (Sc) of the cellulose in the cellulose dope is 99.0 ~ by weight or more.
Further, when a cellulose slurry is subjected to a low speed stirring in the same manner as mentioned above, even if the cellulose in the slurry has a vis-cosity average degree of polymerization (DPc) as high as 800, the resultant cellulose dope is also stable for one week or more and free from gelation, and the disso-lution ratio (Sc) of the cellulose in the cellulose do-pe is 99.0 ~ by weight or more.
In the above-mentioned step (3), the particulate cellulose is dissolved to the extent that the cellulose has a dissolution ratio (Sc) of 99.0 ~ by weight or 5 more. When the Sc is lower than 99.0 ~ by weight, as mentioned above, the filter (for removing the cellulose remaining undissolved in the cellulose dope) is fre-quently clogged, so that a commercial scale production of a fiber, a film or the like becomes practically im-10 possible.
The cellulose dope of the present invention, which is obtained by the above-mentioned method, is stable and free from gelation even when the cellulose dope has a high content of cellulose having a high degree of po-15 lymerization. Therefore, from the cellulose dope of the present invention, a cellulose shaped article (such as a fiber, a film, a particle, a sponge or the like) having high mechanical strength can be stably and effi-ciently produced by a commercially acceptable coagula-20 tion method without using a special molding apparatus.
From the viewpoint of reducing the cost for pro-ducing the cellulose shaped article, it is preferred that the cellulose content (Cc) of the cellulose dope is increased, while keeping the dissolution ratio (Sc) 25 of the cellulose in the cellulose dope at 99.0 ~ by weight or more. For attaining this objective, it is very effective to partially modify the hydroxyl groups of the cellulose in the cellulose slurry by reaction with a reagent which is reactive with a hydroxyl group in the presence of an alkali. Examples of such rea-gents include a vinyl compound, an etherification agent and a xanthation agent. When such a reagent is not used, the cellulose content (Cc) of the cellulose dope of the present invention is usually in the range of from 6 to 7 ~ by weight. On the other hand, by employ-ing the above-mentioned modification of the hydroxyl groups of the cellulose, the cellulose content (Cc) of the cellulose dope can usually be increased to the range of from 8 to 9 ~ by weight. This cellulose con-tent is about the same as the cellulose content (8.5 ~
by weight) of the cellulose dope (viscose).used in the conventional viscose process.
In the present invention, it is preferred that the above-mentioned reagent is selected from the group con sisting of an etherification agent and a xanthation agent.
Generally, when cellulose is reacted with the above-mentioned reagent in order to render the cellu-lose water-soluble, it is considered appropriate to use the reagent in an amount of from 0.3 to 1.2 mole per mole of glucose units in the cellulose. However, with respect to the cellulose dope of the present invention, when the amount of the reagent is in the above-mentioned range, it is possible that the mechanical strength of the cellulose shaped article (especially the mechanical strength exhibited when the article is in a wet state) is greatly lowered. Therefore, in the present invention, it is preferred that the amount of the reagent is 0.1 mole or less per mole of glucose units in the cellulose in the cellulose dope. When this amount of the reagent is used, the cellulose con-tent (Cc) of the cellulose dope can be increased to a satisfactorily high level while keeping the dissolution ratio (Sc) of the cellulose in the cellulose dope at 99.0 ~ by weight or more. Further, this amount of the reagent is considerably lower than the amount of the reagent used in the conventional viscose process.
Addition of the reagent can be conducted in an ap-propriate stage in the process for producing the cellu-lose dope of the present invention. In the present in-vention, it is preferred that the reagent is added to the cellulose slurry at a point in time which is after step (1) and before the end of step (3).
The cellulose dope obtained in this manner (where-in the hydroxyl groups of the cellulose are partially modified) also exhibits a zero-shear viscosity which satisfies the above-mentioned formula (1). Fur-ther, usually, in the NMR analysis of such cellulose dope, the 6-position carbon atoms of the glucose units of the cellulose exhibit a longitudinal relaxation time (ic) of from 10 to 400 ms, and the 1-position carbon atoms of the glucose units of the cellulose exhibit a longitudinal relaxation time (ic) of from 200 to 10,000 ms.
By subjecting the cellulose dope of the present invention to an appropriate coagulation treatment, a cellulose shaped article can be obtained. Examples of cellulose shaped articles include a fibrous body, a flat film, a tubular film, a hollow fiber, a particle, a sponge body and a coating.
In the present invention, it is preferred that the coagulation treatment is selected from the group con-sisting of drying coagulation, gelation coagulation and neutralization coagulation. Hereinbelow, an explana-tion is made with respect to these coagulation treat-ments.
<Drying coagulation>
Drying coagulation is a method for coagulating a cellulose dope to obtain a cellulose shaped article, which comprises drying a cellulose dope so as to pre-cipitate the cellulose in the cellulose dope. Drying coagulation is advantageous in that the cellulose shaped article obtained by drying coagulation has very high structural density and very high mechanical strength, as compared to those properties of the shaped articles obtained by other coagulation methods. Fur-ther, the shaped article obtained by drying coagulation has an extremely low permeability with respect to vari-ous substances, such as water.
For example, with respect to a film obtained by subjecting the above-mentioned cellulose dope to drying coagulation, the water permeability of the film is about 0.1 liter/(m2~hr~kg/cm2). This water permeabil-ity of the film is considerably smaller than the water permeability (about 1 to 5 liters/(m2~hr~kg/cm2)) of a commercially available reverse osmosis membrane. This means that the above-mentioned film exhibits a substan-tially complete water barrier property.
Also, the above-mentioned film exhibits an oxygen permeability of about 50 cc/m2/24 hr/atm, as measured at 23 °C and a relative humidity of 65 ~. That is, the above-mentioned film exhibits an extremely low gas per-meability (i.e., excellent gas barrier property).
Further, the above-mentioned shaped article (film) exhibits an extremely low oil permeability. For exam-ple, with respect to a cellulose-coated article ob-tained by a method in which the above-mentioned cellu-lose dope is coated on the surface of a paper sheet and 5 the resultant dope film is subjected to drying coagula-tion to thereby form a cellulose coating, when the oil resistance of the cellulose coating is measured in ac-cordance with the TAPPI RC-338 method, the cellulose coating exhibits a Kit value of 12 or more. (The "Kit 10 value" is an index of the oil resistance of an oil re-sistant paper. The higher the Kit value, the higher the oil resistance. With respect to the Kit value, see item (11) of the section below which explains the meas-uring methods used in the below-described Examples and 15 Comparative Examples.) The Kit value of 12 or more is far higher than the Kit value of a commercially avail-able oil resistant paper. The surface of the cellulose coating exhibits a slight hydrophobicity, and exhibits a contact angle of 50° or more with water.
20 The mechanical strength of the cellulose shaped article obtained by subjecting the above-mentioned cel-lulose dope to drying coagulation is very high, as com-pared to that of a cellulose shaped article obtained by subjecting to drying coagulation the conventional cel-25 lulose dope (i.e., a cellulose dope in which the cellu-lose content (Cc) is less than 4 ~ by weight and the viscosity average degree of polymerization (DPc) of the cellulose is less than 350).
<Gelation coagulation>
Cellulose can be dissolved only in an aqueous so-dium hydroxide solution having a specific sodium hy-droxide concentration (CNa), i.e., a sodium hydroxide concentration of from 6.5 to 11 ~ by weight. In other words, when a solution obtained by dissolving cellulose in an aqueous sodium hydroxide solution (i.e., a cellu-lose dope) is contacted with a liquid other than an aqueous sodium hydroxide solution having a sodium hy-droxide concentration of from 6.5 to 11 ~ by weight, gelation occurs. Therefore, a liquid other than an aqueous sodium hydroxide solution having a sodium hy-droxide concentration of from 6.5 to 11 ~ by weight can be used as a gelling agent for the above-mentioned cel-lulose dope.
With respect to the liquid used as a gelling agent, water and aqueous solutions can be preferably used.
When an aqueous solution of a salt is used as a gelling agent, the higher the concentration of the salt in the solution and the lower the gelation temperature, the higher the structural density and the mechanical strength of the obtained cellulose shaped article.
On the other hand, a cellulose shaped article ob-tained by subjecting a dope to gelation coagulation us-ing hot water as a gelling agent exhibits a lowest structural density and lowest mechanical strength.
However, the mechanical strength of such a cellulose shaped article is satisfactorily high, as compared to that of a cellulose shaped article obtained by subject-ing to gelation coagulation the conventional cellulose dope (i.e., a cellulose dope in which the cellulose content (Cc) is less than 4 % by weight and the viscos-ity average degree of polymerization (DPc) of the cel-lulose is less than 350).
<Neutralization coagulation>
In the case of the neutralization coagulation, the structure and mechanical properties of the obtained cellulose shaped article are largely affected by the concentration and temperature of the aqueous acidic so-lution used for neutralization. The higher the concen-tration of the aqueous acidic solution and the lower the temperature of the aqueous acidic solution, the higher the structural density and the mechanical strength of the obtained cellulose shaped article.
Therefore, the concentration and temperature of the aqueous acidic solution are appropriately selected in accordance with the structural density and mechanical properties desired for the cellulose shaped article.
A cellulose shaped article obtained by subjecting a dope to neutralization coagulation using a hot aque-ous acidic solution exhibits a low mechanical strength.
However, the mechanical strength of such a cellulose shaped article is satisfactorily high, as compared to that of a cellulose shaped article obtained by subject-ing to neutralization coagulation the conventional cel-lulose dope (i.e., a cellulose dope in which the cellu-lose content (Cc) is less than 4 ~ by weight and the viscosity average degree of polymerization (DPc) of the cellulose is less than 350).
Examples of aqueous acidic solutions which can be used in the present invention include aqueous solutions of acids, such as sulfuric acid, acetic acid, thiosul-furic acid, sulfurous acid, hydrochloric acid, hydro-bromic acid, hydrofluoric acid, nitric acid, phosphoric acid, pyrophosphoric acid, metaphosphoric acid, poly-phosphoric acid, hypophosphorous acid, trifluoroacetic acid, thiocyanic acid and the like; and aqueous solu-tions of salts of the above-mentioned acids. These aqueous acidic solutions can be used individually or in combination.

As described above, the structural density and mechanical properties of the cellulose shaped article can be greatly controlled by appropriately selecting the type of coagulation treatment and controlling the conditions for the coagulation treatment.
Further, in any case, since the cellulose shaped article of the present invention is produced from the above-mentioned cellulose dope in which the cellulose content (Cc) is 4 ~ by weight or more and the viscosity average degree of polymerization (DPc) of the cellulose is 350 or more), the mechanical strength of the cellu-lose shaped article of the present invention is satis-factorily high, as compared to that of a cellulose shaped article obtained by coagulating the conventional cellulose dope (i.e., a cellulose dope in which the cellulose content (Cc) is less than 4 ~ by weight and the viscosity average degree of polymerization (DPc) of the cellulose is less than 350).
The cellulose dope of the present invention can be produced without using a poisonous substance. There-fore, the cellulose dope of the present invention is suitable for producing an edible shaped article con-taining cellulose as a substrate (edible cellulose ar-ticle).
An edible cellulose article can be obtained by subjecting to the above-mentioned coagulation treatment a cellulose dope containing at least one additive se-lected from the group consisting of a polysaccharide, a polypeptide and a natural resin.
5 In the production of the edible cellulose article, the above-mentioned reagent may be used. In the case where the reagent is used, it is preferred that the reagent is a compound which has been approved as a rea-gent for use in food, such as monochloroacetic acid.
10 Examples of methods for producing the above-mentioned cellulose dope containing an additive in-clude:
i) a method in which the additive is dispersed or dissolved in an aqueous sodium hydroxide solution hav-15 ing a sodium hydroxide concentration of 6.5 to 11 ~ by weight, preferably 7 to 10 ~ by weight, and the resul-tant dispersion or solution is mixed with the above-mentioned cellulose dope; and ii) a method in which the additive is added to the 20 above-mentioned cellulose slurry to thereby obtain a mixture, and a cellulose dope is produced in substan-tially the same manner as mentioned above, except that the above-obtained mixture is used in place of the above-mentioned cellulose slurry.
25 Examples of polysaccharides which can be used as the above-obtained additive include gum arabic, arabi-nogalactan, alginic acid, gum ghatti, carrageenan, gum karaya, xanthan gum, guar gum, konjak starch powder, tamarind, tara gum, gum tragacanth, furcellaran, pullu-lan, pectin, chitin, locust been gum, xylan, mannan, starches, and Na, K and Ca salts thereof.
Examples of polypeptides which can be used as the above-obtained additive include natural proteins, such as soybean protein, casein, albumin, globulin, gelatin and hydrolysates of these proteins, Na, K and Ca salts of these proteins, and Na, K and Ca salts of the above-mentioned hydrolysates.
Examples of natural resins which can be used as the above-obtained additive include shellac resin.
These additives can be used individually or in combination.
As apparent from the above, the cellulose dope of the present invention is stable and free from gelation even when the cellulose dope has a high content of cel-lulose having a high degree of polymerization. By the use of the cellulose dope of the present invention, it becomes possible to produce, without using a large amount of a poisonous substance, a regenerated cellulo-se shaped article (such as a fiber or a film) which has a mechanical strength sufficient for practical use.

Therefore, the cellulose dope of the present invention is commercially very advantageous.

BEST MODE FOR CARRYING OUT THE INVENTION
Hereinbelow, the present invention will be de-scribed in more detail with reference to Examples and Comparative Examples, which should not be construed as limiting the scope of the present invention.
The below-mentioned methods were used for the measurement of the following properties: the dissolu-tion ratio (Sc) of cellulose, the viscosity average de-gree of polymerization (DPc), the average particle diameter of particulate cellulose (gym), the viscosity characteristics of a cellulose slurry, the zero-shear viscosity (~o) of a cellulose dope (mPa~s), the solid state NMR, the NMR longitudinal relaxation time (ms), the strength and elongation of a fiber, the water per-meability, the oxygen permeability, the oil resistance and the contact angle with water.
(1) Dissolution ratio (Sc) of cellulose The dissolution ratio of cellulose was obtained by a method in which the amount of cellulose (Rc) remain-ing undissolved in a cellulose/sodium hydroxide aqueous solution (cellulose dope) is measured in the below-described manner, and, then, a calculation is conducted using the below-mentioned formula (6). The measurement of the amount of cellulose (Rc) remaining undissolved was performed as follows. The cellulose/sodium hydrox-ide aqueous solution (cellulose dope) was diluted 80-fold with an aqueous 8 ~ by weight sodium hydroxide so-y lution to thereby obtain a diluted cellulose/sodium hy-droxide aqueous solution, and the number of the undis-solved cellulose particles present in 2 ml of the ob-tained diluted cellulose/sodium hydroxide aqueous solu-tion was counted by means of a Coulter counter (Coulter Counter ZM80, manufactured and sold by Coulter Elec-tronic Inc., U.S.A.). The counting was conducted with respect to cellulose particles having a particle diame-ter of from 3 dun to 100 ~zn, wherein the particle diame-ter range of from 3 ~.m to 100 ~.m was divided into a plurality of segments as shown in the below-mentioned formula (5). From the number obtained by the counting, the volume (Rc)(ml) of the undissolved matter present in 20 liters of the cellulose/sodium hydroxide aqueous solution was obtained using the following formula (5).
Formula (5) Rc = {N3 to N10 x (4/3)~'t(6.5 x 10-4/2)3 + Nlp to N20 x (4/3)n(15 x 10-4/2)3 + N20 to N30 x (4/3)n(25 x 10-4/2)3 ~...... + N90 to N100 x (4/3)n(95 x 10-4/2)3}
x 80 x (20 x 103/2) (wherein Nx to Ny represents the number of parti-cles each having a particle diameter of from x (dun) to y (Eun), which are contained in 2 ml of the 80-fold di-luted cellulose dope, wherein the number is counted by 5 a Coulter counter.) Formula (6) Sc = (1 - Rc x S1/(S2 x 20'103 x Cc/100)) x 100 (wherein S1 represents the specific gravity of the 10 cellulose (1.4 g/cm3);
S2 represents the specific gravity of the cellu-lose/sodium hydroxide aqueous solution (1.1 g/cm3); and Cc represents the cellulose content (~ by weight) of the cellulose/sodium hydroxide aqueous solution.) (2) Viscosity average degree of polymerization (DPc) The viscosity average degree of polymerization of cellulose was obtained by the following method. The [r~] value of a cellulose/Cadoxen solution was obtained, and the obtained [~] value was substituted for the [r~]
in the below-mentioned viscosity formula of Brown and Wikstrom (described in Euro. Polym. J, 1 ,1 (1966)) to thereby obtain a viscosity average molecular weight (Mw). The obtained viscosity average molecular weight (Mw) was divided by 162, and the value obtained by the division was defined as the viscosity average degree of polymerization (DPc). The method for preparing Cadoxen is described in the above-mentioned Euro. Polym, J, 1, 1 (1966).
I~l - 3.85 x 10-2 x Mw0.76 (3) Average particle diameter (dun) of particulate cel-lulose First, a cellulose slurry was diluted with dis-tilled water so that the cellulose content of the slur-ry became 0.1 ~ by weight and, then, the cellulose par-ticles were dispersed by ultrasonication. Subsequently, the particle size distribution of the dispersed cellu-lose particles was measured by means of a laser dif-fraction type particle size distribution measuring equipment (SALD-1100, manufactured and sold by Shimadzu Corporation, Japan). From the particle size distribu-tion, the total volume of the cellulose particles was obtained, based on the assumption that the cellulose particles are spherical. Then, a graph showing the re-lationship between the particle diameters of the cellu-lose particles and the sum of the volumes of cellulose particles having a given particle diameter or less was obtained. In the above-mentioned graph, a specific particle diameter was obtained at which the sum of the volumes of the particles having the specific particle diameter or less is 50 ~ of the total volume of the particles. The obtained specific particle diameter was taken as the average particle diameter of the particu-late cellulose. (This method is described in detail in Unexamined Japanese Patent Application Laid-Open Speci-fication No. 3-163135.) (4) Viscosity characteristics of a cellulose slurry The measurement was performed using HAAKE viscome-ter RheoStress RS 100 Model as a measuring apparatus (cone/plate sensor system, angle: 4°, diameter: 35 mm).
The measurement mode employed was stress ramp mode, and the stress range was 1 to 450 Pa, the measurement time was 300 sec, and the measurement temperature was 20 °C.
Based on the results of the measurement, a viscosity (~s)-stress (as) curve was obtained. The stress at which the viscosity sharply decreases (as shown in Fig.
1) was obtained in this curve and defined as the yield stress (aT).
(5) Zero-shear viscosity (~o) of a cellulose dope The measurement was performed using HAAKE viscome ter RV-12 Model as a measuring apparatus (double cylin der type, rotor: MV-I). The measurement temperature was 10 °C and the viscosity was measured at various shear rates. The ~o value was obtained by a method in which the shear rates are extrapolated to 0/sec.
(6) Solid state NMR of a cellulose slurry Solid state 13C-NMR measurement of a cellulose slurry was conducted by the CP/MAS method using an NMR
spectrometer (DSX400, manufactured and sold by Bruker Instruments Inc., U.S.A.) under the following measuring conditions: contact time: 1 ms; pulse intervals: 5 s;
90° pulse: 4.8 ~s; number of accumulations: 3000; and rotation rate: 4000 Hz.
Separation was made between the peaks respectively ascribed to the higher magnetic field component and the lower magnetic field component of the 4-position carbon atoms (C4) of the glucose units of the cellulose in the slurry, using a method in which each of the peaks is approximated to the Gaussian distribution function by using a curve fitting program "Win Fit", which is at-tacked to the above-mentioned spectrometer.
(7) NMR longitudinal relaxation time With respect to a cellulose dope, the measurement of NMR longitudinal relaxation time (zc) was conducted using an NMR spectrometer (JNM-LA400, manufactured and sold by JEOL Ltd., Japan) under the following measuring conditions: observation frequency: 400 MHz; number of accumulations: 500; and temparature: 10 °C. In the measurement, D20 and the cellulose dope were, respec-tively, placed in the inner tube and the outer tube of a double tube, and the proton decoupling method was used.
(8) Strength and elongation of a fiber The strength and elongation of a fiber were meas-ured in accordance with JIS L 1013-1981.
(9) Water permeability of a cellulose-coated paper The water permeability of a cellulose-coated paper was measured by a method in which a cellulose-coated paper sheet having an area of 20 cm2 is placed under a pressure of 1 atm at 25 °C, and water is applied onto the cellulose-coated paper sheet, and the volume of wa-ter which has passed through the cellulose-coated paper sheet during a predetermined period of time is measured.
(10) Oxygen permeability of a cellulose-coated paper The oxygen permeability of a cellulose-coated pa-per was measured with respect to a measuring area of 4 cm2 in accordance with JIS K7126 (MOCON method).

(11) Oil resistance The measurement was performed by the TAPPI RC338 method. This method is a method in which oils respec-tively having predetermined different compositions are individually dropped on a coated paper sheet and wheth-er or not the oils permeate into the coated paper sheet is visually examined. 12 types of oils having differ-ent permeation abilities are used. 12 numbers (1 to 12) are, respectively, assigned to the 12 types of oils in the order from the oil having the lowest permeation ability to the oil having the highest permeation abil-ity. The 12 types of oils are individually dropped on the coated paper sheet in the order from the oil having the lowest permeation ability. The oils which have been found to be unable to permeate into the coated pa-per sheet are selected. From among the selected oils, the oil assigned the largest number (i.e., the oil hav-ing the highest permeation ability) is selected, and the number assigned to this oil is taken as the Kit value, which is used as an index of oil resistance.
(12) Contact angle with water The measurement was performed by means of a CBVP-A-3 type tension meter (KYOWA KAIMEN KAGAKU CO., LTD., Japan). A specimen was horizontally held, and 2 mm3 of water at 25 °C was put on the specimen by means of a micropipet which is attached to the tension meter, and the contact angle of the drop of water with the speci-men was measured.
Examples 1 to 4 and Comparative Examples 1 to 4 In each of Examples 1 to 4, the relationship be tween the yield stress (aT) of a cellulose slurry and the DPc of the cellulose in the slurry is examined and shown.
A sulfite process dissolving pulp (manufactured and sold by Nippon Paper Industries Co., Ltd., Japan) was hydrolyzed by the steam explosion method, thereby obtaining three types of celluloses having varied vis-cosity average degrees of polymerization (DPc). The obtained celluloses and the same dissolving pulp as mentioned above (without being subjected to the steam explosion) were individually mixed with sodium hydrox-ide so that each of the resultant four aqueous mixtures had a cellulose solids content of 8.5 ~ by weight and a sodium hydroxide concentration of 2 ~ by weight. The obtained four aqueous mixtures were individually sub-jected to wet pulverization by using a stirred medium wet grinding apparatus (PEARL Mill RL5-VS, manufactured and sold by ASHIZAWA, Ltd., Japan) for 8 minutes, thereby obtaining alkali/cellulose slurries each con-taining particulate cellulose having an average parti-cle diameter of 10 to 13 Eun. The obtained al-kali/cellulose slurries respectively had DPc values of 350, 450, 540 and 720, and these were, respectively, identified as the slurries of Examples 1 to 4. As Com-parative Examples, substantially the same procedure as described above was conducted, except that sodium hy-droxide was not used (i.e., an aqueous medium contain-ing no sodium hydroxide was used). The resultant aque-ous cellulose slurries (water/cellulose slurries) re-spectively containing particulate celluloses having DPc values of 350, 450, 540 and 720 were, respectively, identified as the slurries of Comparative Examples 1 to 4.
In each of Examples 1 to 4, k2 of the above-mentioned formula (4) was -0.05, i.e., a negative value.
This means that the higher the DPc, the lower the yield stress (aT) of the slurry becomes (wherein the yield stress is the stress at which the viscosity of the slurry exhibits a sharp decrease). A cellulose slurry having such a property is extremely advantageous in that the cellulose contained therein can be homogene-ously dissolved by gently stirring while suppressing a ' 103 temperature increase. This property is especially ad-vantageous for the dissolution of a cellulose of a high DPc. Further, in each of Examples 1 to 4, the cellu-lose in the slurry exhibited a non-crystallinity (xam) of 0.6, wherein the non-crystallinity is defined by the formula : xam = Ihigh / ( Ihigh + I low ) ' The non-crystallinity Xam is an index of the de-gree of breakdown of the intramolecular hydrogen bonds of the cellulose. The fact that in each of Examples 1 to 4 the non-crystallinity xam is more than 0.5 shows that the degree of breakdown of the intramolecular hy-drogen bonds in the cellulose in the alkali/cellulose slurry of each of Examples 1 to 4 is high and, hence, the conformation of the cellulose molecule has a high degree of freedom. This has a relationship to the fact that, as mentioned above, in each of Examples 1 to 4, k2 of formula (4) is a negative value. It is consid-ered that when cellulose in such a state is dissolved, the entropy of the system becomes satisfactorily high, so that the cellulose in the cellulose slurry of each of Examples 1 to 4 can be easily dissolved.
As mentioned above, the rate of dissolution of cellulose into an aqueous alkali solution is markedly lower than the rate of dissolution of cellulose into an aqueous cuprammonium solution or an aqueous Cadoxen so-lution. Therefore, when cellulose is added to an aque-ous alkali solution and the resultant mixture is al-lowed to stand still without stirring, the dissolution of the cellulose apparently stops, so that the dissolu-tion ratio (Sc) of the cellulose becomes only less than 50 ~. Therefore, it is necessary to promote the disso-lution of the cellulose by stirring. In general, if the stirring is performed by means of a mixer or the like capable of stirring at a high speed, the dissolu-tion rate can be increased. However, when a high speed stirring is performed, even if the average temperature of the whole system is kept at 10 °C or less, a local heat generation occurs, so that the stability of the resultant cellulose dope is decreased and gelation is likely to occur. Further, with respect to the cellu-lose in an aqueous alkali solution, the higher the tem-perature of the cellulose, the lower the solubility of the cellulose becomes. Therefore, it is not preferred that the temperature of a cellulose slurry is elevated due to a local heat generation accompanying a high speed stirring. For these reasons, in the present in-vention, it is required that the stirring of a cellulo-se slurry be performed at a low speed.
The cellulose slurries of Examples 1 to 4 satisfy the above-mentioned formula (4). This means that, with respect to the cellulose slurries of Examples 1 to 4, even if the viscosity average degree of polymerization (DPc) of the cellulose is increased, the viscosity of the slurry does not increase. Accordingly, by using any of the cellulose slurries of Examples 1 to 4, a cellulose dope which is stable and unlikely to exhibit gelation can be obtained.
On the other hand, in each of Comparative Examples 1 to 4 (in each of which a water/cellulose slurry was obtained by subjecting to wet pulverization the cellu-lose dispersed in an aqueous medium containing no sodi-um hydroxide), k2 of the above-mentioned formula (4) was 0.8, i.e., a positive value. This means that a ho-mogeneous dissolution of the cellulose of the slurry is difficult. Therefore, the dissolution ratio (Sc) of the cellulose in the resultant cellulose/sodium hydrox-ide aqueous solution (cellulose dope) is poor. This poor property becomes marked especially in the case of the dissolution of cellulose having a high DPc. Fur-ther, in each of Comparative Examples 1 to 4, the cel-lulose in the slurry exhibited a non-crystallinity (xam) of 0.45, suggesting that the movement of the cel-lulose molecular skeleton itself is restricted. For easy reference, the formula (4) is shown below again:
QT = K2 + k2DPc (4) wherein:
QT represents the yield stress (Pa) of the slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in the slurry.
Examples 5 to 8 and Comparative Example 5 In each of Examples 5 to 8, with respect to each cellulose slurry, the relationship between the yield stress (QT) and the sodium hydroxide concentration (CNa) is examined and shown.
A sulfite process dissolving pulp (manufactured and sold by Nippon Paper Industries Co., Ltd., Japan) was hydrolyzed by means of an aqueous sulfuric acid so-lution, thereby obtaining cellulose having a DPc value of 600. The obtained cellulose was mixed with sodium hydroxide so that four aqueous mixtures were obtained each of which had a cellulose solids content of 10.5 ~
by weight and which respectively had sodium hydroxide concentration (CNa) values of 0.5 ~ by weight, 2 ~ by weight, 3 ~ by weight and 5 ~ by weight. The obtained four aqueous mixtures were individually subjected to wet pulverization by using a stirred medium wet grind-ing apparatus (APEX MILL AM-1, manufactured and sold by KOTOBUKI Engineering and Manufacturing Co., Ltd., Ja-pan) for 6 minutes, thereby obtaining alkali/cellulose slurries each containing particulate cellulose having an average particle diameter of 10 to 13 ~,m. The ob-tained alkali/cellulose slurries had CNa values of 0.5 ~ by weight, 2 ~ by weight, 3 $ by weight and 5 by weight, and these were, respectively, identified as the slurries of Examples 5 to 8.
The relationship between the yield stress (aT) and the sodium hydroxide concentration (CNa) of each of the obtained alkali/cellulose slurries was examined. It was found that k1 of the above-mentioned formula (2) was -0.16, i.e., a negative value. Further, with re-spect to the non-crystallinity xam represented by the above-mentioned formula (3), which is an index of the freedom of the movement of the cellulose molecular skeleton, the celluloses in the slurries of Examples 5 to 8 respectively had non-crystallinity (Xam) values of 0.54, 0.59, 0.61 and 0.62, i.e., values which are each more than 0.5. As shown in Examples 1 to 4, the fact that the non-crystallinity xam is more than 0.5 and k1 of the formula (2) is a negative value shows that the cellulose molecular skeleton is easily movable. When the configuration entropies before and after the disso-lution are also taken into consideration, it is be-lieved that the above fact suggests that the celluloses in these slurries can be easily dissolved.
As Comparative Example 5, the following experiment was conducted. In substantially the same manner as in Examples 5 to 8, a sulfite process dissolving pulp (manufactured and sold by Nippon Paper Industries Co., Ltd., Japan) was hydrolyzed by means of an aqueous sul-furic acid solution, thereby obtaining cellulose having a DPc value of 600. The obtained cellulose was mixed with sodium hydroxide so that four aqueous mixtures were obtained each of which had a cellulose solids con-tent of 10.5 ~ by weight and which respectively had so-dium hydroxide concentrations of 0.5 ~ by weight, 2 by weight, 3 ~ by weight and 5 ~ by weight. The ob-tained four aqueous mixtures were individually stirred using a stirrer (T. K. HOMO-MIXER, manufactured and sold by TOKUSHU KIKA KOGYO Co., Ltd., Japan), thereby obtaining alkali/cellulose slurries having the same compositions as the cellulose slurries of Examples 5 to 8. The relationship between the yield stress (oT) and the sodium hydroxide concentration (CNa) of each of the obtained alkali/cellulose slurries was examined. It was found that k1 of the formula (2) was 0.11, i.e., a positive value. Further, with respect to each of the obtained alkali/cellulose slurries, it was found that the non-crystallinity xam of the cellulose was less than 0.5 and, hence, the movement of the cellulose mo-lecular skeleton was restricted, suggesting that the dissolution performance was poor.
Comparative Example 6 A sulfite process dissolving pulp (ALAPUL-T, manu factured and sold by ALASKA PULP Co., Ltd., U.S.A.) was mixed with sodium hydroxide so that two aqueous mix tures were obtained each of which had a cellulose solids content of 3 ~ by weight and which respectively had sodium hydroxide concentration (CNa) values of 2 ~
by weight and 4 ~ by weight. The obtained two aqueous mixtures were individually subjected to pulverization by using a grinder (SUPER-GRINDEL, manufactured and sold by MASUKO SANGYO Co., Ltd., Japan) under grinding conditions wherein the rotor revolution rate is 1,500 rpm, the clearance between the grindstones is 40 Eun and the grinding operation is conducted 5 times, thereby obtaining alkali/cellulose slurries. The obtained al-kali/cellulose slurries were individually concentrated by using a centrifugal dehydrator until the cellulose solids content of each slurry became 8.5 ~ by weight.
Then, it was attempted to measure the yield stress (aT) 11~
of each of the resultant concentrated slurries. How-ever, any of these concentrated slurries was a solid-like product exhibiting almost no fluidity. Therefore, it was impossible to measure their viscosities. It is considered that the reason why these concentrated slur-ries exhibited a solid-like state is because microfi-brils formed a network structure, thereby markedly in-creasing the viscosity. As mentioned above, the pul-verization of cellulose is classified into a pulveriza-tion wherein cellulose fibers are cut into particles (as conducted in the present invention) and a pulveri-zation wherein cellulose fibers are caused to undergo fibrillation (as conducted in this Comparative Example 6). In the case of the fibrillation, the fibrils form a network structure, so that the resultant suspension has markedly high viscosity and, hence, exhibits a gel state even when the solids content is low. When it is attempted to dissolve the cellulose contained in such a high viscosity cellulose suspension, it is difficult to mix such a high viscosity cellulose suspension with an aqueous sodium hydroxide solution as a solvent. There-fore, such a high viscosity cellulose suspension is un-suitable for use as a cellulose slurry for the prepara-tion of a cellulose dope.
To the above-obtained concentrated slurries (cel-lulose slurries which had been individually concentrat-ed to a cellulose solids content of 8.5 ~ by weight) was added an aqueous sodium hydroxide solution, thereby adjusting the compositions of the cellulose slurries so that each slurry had a cellulose content (Cc) of 5 ~ by weight and a CNa (sodium hydroxide concentration) value of 7.6 ~ by weight, wherein this operation was conduct-ed in the same manner as in Example 15 described below.
The resultant mixtures were individually subjected to dissolution operation for the cellulose (preparation of a dope) in the same manner as in Example 15 described below, thereby obtaining cellulose/sodium hydroxide aqueous solutions (cellulose dopes). However, the dis-solution ratios (Sc) of the celluloses in the obtained cellulose dopes were only 96 ~ or less and, hence, the dissolution performance was markedly poor. With re-spect to the zero-shear viscosities (~o) of these cel-lulose/sodium hydroxide aqueous solutions (dopes), one dope (prepared by the method in which the aqueous mix-ture subjected to the pulverization had a sodium hy-droxide concentration (CNa).of 2 ~ by weight) exhibited a zero-shear viscosity (~o) of 52,000 mPa~s, and the other dope (prepared by the method in which the aqueous mixture subjected to the pulverization had a sodium hy-droxide concentration (CNa) of 4 ~ by weight) exhibited a zero-shear viscosity (~o) of 44,000 mPa~s. Therefore, these dopes exhibited high viscosities which do not satisfy the above formula (1).
Examples 9 to 15 and Comparative Examples 7 to 18 In substantially the same manner as in Examples 1 to 4, cellulose slurries which respectively had DPc values of 350, 450, 540, 640 and 720 (and each of which had a sodium hydroxide concentration of 2 ~ by weight) were obtained. These cellulose slurries were cooled to 0 °C. To the~cooled cellulose slurries respectively having DPc values of 350, 450, 540, 640 and 720 was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 15.6 ~ by weight and which had been kept at -10 °C, thereby adjusting the compositions of the slurries so that each slurry had a cellulose content (Cc) of 5 ~ by weight and a CNa (so-dium hydroxide concentration) value of 7.6 ~ by weight.
To the same cellulose slurries respectively having DPc values of 350 and 540 as employed above was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 33.7 ~ by weight and which had been kept at -10 °C, thereby adjusting the composi-tions of the slurries so that each slurry had a cellu-lose content (Cc) of 7 ~ by weight and a CNa (sodium hydroxide concentration) value of 7.6 ~ by weight.
Then, these 7 cellulose slurries were individually stirred using a low speed stirring type kneader (twin-screw kneader) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 500/sec and a stirring speed of 15 m/min in terms of the speed at which the outer end of an agitat-ing element of the stirrer is rotated, thereby obtain-ing 7 cellulose dopes including:
5 cellulose dopes each of which had a cellulose content (Cc) value of 5 ~ by weight, a sodium hydroxide concentration (CNa) value of 7.6 ~ by weight and which respectively had DPc values of 350, 450, 540, 640 and 720 (respectively as Examples 9, 11, 12, 14 and 15; see Table 2); and 2 cellulose dopes each of which had a cellulose content (Cc) value of 7 ~ by weight, a sodium hydroxide concentration (CNa) value of 7.6 ~ by weight and which respectively had DPc values of 350 and 540 (respec-tively as Examples 10 and 13; see Table 3).
With respect to the cellulose dopes having DPc values of 450, 640 and 720, experiments in which the Cc value is adjusted to 7 ~ by weight were not carried out. The dissolution ratio (Sc) of the cellulose in each of the obtained cellulose dopes was 99.0 ~ by weight or more and, hence, the dissolution performance was good. The results are shown in Tables 2 and 3. These cellulose dopes of Examples 9 to 15 each exhibited a zero-shear viscosity (~o) which satisfies the formula (1). As an example, the relationship between the DPc and ~~p of the cellulose dopes having a cellulose content (Cc) of 5 ~
by weight is shown in Fig. 3. In Fig. 3, the region surrounded by solid lines corresponds to the range which satisfies the formula (1). As shown in Fig. 3, any of the ~o values of the cellulose dopes of Examples 9, 11, 12, 14 and 15 falls inside of the region sur-rounded by the solid lines. In addition, when these cellulose dopes were allowed to stand still at 10 °C, their zero-shear viscosities (gyp) did not change for one week or more and hence these dopes were stable.
As Comparative Examples 7 to 9, the cellulose slurries obtained in Examples 1, 3 and 4, which respec-tively had DPc values of 350, 540 and 720, were sub-jected to the dissolution of the cellulose (preparation of a dope) in substantially the same manner as de-scribed in connection with production of the dopes of Examples 9 to 15, except that the Cc (cellulose con-tent) of the dope was changed to 3 ~ by weight. With respect to each of the obtained cellulose dopes of Com-parative Examples 7 to 9, the zero-shear viscosity (~o) was measured. As shown in Table 1 (see the column for Comparative Examples 7 to 9 in Table 1), the zero-shear viscosities (~o) of these cellulose dopes did not sat isfy the formula (1). For easy reference, the formula (1) is shown below again:
kCcm x DPcp ( 1 ) wherein:
~o represents the zero-shear viscosity (mPa~s) of the cellulose dope, Cc represents the cellulose content (~ by weight) of the cellulose dope, DPc represents the viscosity average degree of polymerization of the cellulose in the cellu-lose dope, k = 3.9 x 10-11, m is a number of from 5 to 7, and p is a number of from 3 to 4.
Further, in the NMR analysis of the cellulose dope having a DPc value of 350 and a Cc value of 5 ~ by weight (Example 9), the cellulose dope having a DPc value of 540 and a Cc value of 5 ~ by weight (Example 12) and the cellulose dope having a DPc value of 720 and a Cc value of 5 ~ by weight (Example 15), the 6-position carbon atoms (C6) of the glucose units of the celluloses respectively exhibited longitudinal relaxa-tion time (ic6) values of 140, 150 and 190 ms, and the 1-position carbon atoms (C1) of the glucose units of the celluloses respectively exhibited longitudinal re-laxation time (zcl) values of 300, 300 and 520 ms.
In Comparative Examples 10 to 17, the cellulose slurries obtained in Comparative Examples 1, 3 and 4 (water/cellulose slurries obtained by effecting wet pulverization of cellulose in an aqueous medium con-taining no sodium hydroxide) (wherein the cellulose slurries respectively had DPc values of 350, 540 and 720) were cooled to 0 °C. To the cooled cellulose slurries respectively having DPc values of 350, 540 and 720 was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 11.7 ~ by weight and which had been kept at -10 °C, thereby ad-justing the compositions of the slurries so that each slurry had a cellulose content (Cc) of 3 ~ by weight and a CNa (sodium hydroxide concentration) value of 7.6 ~ by weight. To the same cooled cellulose slurries respectively having DPc values of 350, 540 and 720 as employed above was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 18.5 ~ by weight and which had been kept at -10 °C, thereby adjusting the compositions of the slurries so that each slurry had a cellulose content (Cc) of 5 % by weight and a CNa (sodium hydroxide concentration) value of ?.6 % by weight. To the same cooled cellulose slur-ries respectively having DPc values of 350 and 540 as employed above was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 43.1 % by weight and which had been kept at -10 °C, thereby adjusting the compositions of the slurries so that each slurry had a cellulose content (Cc) of 7 % by weight and a CNa (sodium hydroxide concentration) value of 7.6 % by weight. Then, these 8 cellulose slurries were individually subjected to a high speed stirring under stirring conditions wherein the stirring is per-formed at a shear rate of 17,000/sec and a stirring speed of 1,020 m/min in terms of the speed at which the outer end of an agitating element of the stirrer is ro-tated, thereby obtaining 8 cellulose dopes (the cellu-lose dopes of Comparative Examples 10 to 17; see Tables 1 to 3). As shown in Tables 1 to 3 (see the columns for Comparative Examples 10 to 17 in Tables 1 to 3), the zero-shear viscosities (~o) of these cellulose do-pes did not satisfy the formula (1). Of these cellu-lose dopes, any one which had a DPc value of 350 or more and a cellulose content (Cc) of 5 % by weight or more exhibited a zero-shear viscosity (~o) which is higher than the range satisfying the formula (1), and this indicates that gelation proceeds immediately after the dissolution of the cellulose (preparation of a dope). For example, in the case of the cellulose dope having a DPc value of 540 and a Cc value of 7 ~ by weight (Comparative Example 15), the ~o value thereof immediately after the dissolution (preparation) was 49,000 mPa~s; however, gelation occurred one day after the dissolution (preparation), losing the solution state.
Further, in the NMR analysis of the cellulose dope having a DPc value of 720 and a cellulose content (Cc) value of 5 ~ by weight (Comparative Example 17), the 6-position carbon atoms (C6) of the glucose units of the cellulose exhibited a longitudinal relaxation time (ic6) of 410 ms, and the 1-position carbon atoms (C1) of the glucose units of the cellulose exhibited a lon-gitudinal relaxation time (icl) of 170 ms, suggesting that the movement of the main chain of the cellulose molecule is markedly restricted and, hence, the disso-lution performance is not good.
In addition, in Comparative Example 18, the fol-lowing experiment was conducted. A cellulose/sodium hydroxide suspension which had the same composition as the cellulose slurry used in Example 15, i.e., a cellu-lose slurry having a DPc value of 720 and a sodium hy-droxide concentration of 2 ~ by weight (containing par-ticulate cellulose having an average particle diameter of 45 ~zn) was prepared. The cellulose slurry was not subjected to wet pulverization. In an attempt to ob-tain a cellulose/sodium hydroxide aqueous solution (dope) having a cellulose content (Cc) of 5 ~ by weight, the cellulose slurry was subjected to a high speed stirring in the same manner as in Comparative Examples 10 to 17. However, a vigorous gelation occurred during the stirring and, hence, a cellulose/sodium hydroxide aqueous solution (dope) was not able to be obtained.

Table 1 Cc: 3 ~ by weight Range satisfyingDope prepared Dope prepared the formula from al- from wa-(1) (mPa~s) kali/celluloseter/cellulose slurry slurry (mPa~s) (mPa~s) DPc = 350 5 to 39 60 (x) 80 (x) (Comparative (Comparative Example 7) Example 10) DPc = 540 22 to 180 220 (x) 240 (x) (Comparative (Comparative Example 8) Example 13) DPc = 720 55 to 493 700 (x) 1300 (x) (Comparative (Comparative Example 9) Example 16) ( O : satisfying the formula ( 1 ) x: not satisfying the formula (1)) (A good shaped article cannot be obtained from a dope having a Cc value of less than 5 ~ by weight.) ' 121 Table 2 Cc: 5 ~ by weight Range satisfyingDope prepared Dope prepared the formula from al- from wa-(1) (mPa~s) kali/cellulose ter/cellulose slurry slurry r~o (mPa~s) (mPa~s) DPc = 350 137 to 1093 270 (O) 1520 (x) ( Example 9 ( Comparative ) Stable for Example 11) one week or relation oc-curred one week more after prepara-tion DPc = 450 305 to 2634 910 (O) (Example 11) .-Stable for one week or more DPc = 540 547 to 4986 920 (O) 5500 (x) ( Example 12 ( Comparative ) Stable f Or Example 14 ) one week or Gelation oc-curred one week more after prepara-tion DPc = 640 943 to 9036 2050 (O) (Example 14) Stable for one week or more DPc = 720 1374 to 13647 6500 (O) 50000 (x) (Example 15) (Comparative Stable for Example 1~ ) one week or Gelation oc-curred one week more after prepara-tion ( O : satisfying the formula ( 1 ) x: not satisfying the formula (1)) ' 122 Table 3 Cc: 7 ~ by weight Range satisfyingDope prepared Dope prepared the formula from al- from wa-(1) kali/ceiluloseter/cellulose (mPa~s) slurry slurry o (mPa~s) (mPa~s) DPc = 350 1138 to 9737 1500 (O) 18000 (x) ( Example 10 ( Comparative ) Stable for Example 12 ) one week or Gelation oc-curred one week more after prepara-tion DPc = 540 4559 to 44420 6750 (O) 49000 (x) ( Example 13 ( Comparative ) Stable for Example 15) one week Or Gelation oc-curred one day more after prepara-tion ( O : satisfying the formula ( 1 ) x: not satisfying the formula (1)) Examples 16 to 18 and Comparative Example 19 In Examples 16 to 18, the influence of CNa on the dissolution of cellulose is examined and shown.
The cellulose slurries obtained in Examples 5, 7 and 8, each of which has a cellulose solids content of 10.5 ~ by weight and which respectively have CNa values of 0.5 ~ by weight, 3 ~ by weight and 5 ~ by weight, were cooled to 0 °C. To these cooled cellulose slurri-es respectively having CNa values of 0.5 ~ by weight, 3 ~ by weight and 5 ~ by weight were, respectively, ' 123 added aqueous sodium hydroxide solutions which respec-tively had sodium hydroxide concentrations of 21.8 ~ by weight, 16.8 ~ by weight and 12.8 ~ by weight and which had been kept at -10 °C, thereby adjusting the composi-tions of the three cellulose slurries so that each slurry had a cellulose content of 7 ~ by weight and a CNa (sodium hydroxide concentration) value of 7.6 ~ by weight. Then, the cellulose slurries were individually subjected to a low speed stirring by using a stirrer (T:
K. HOMO-MIXER, manufactured and sold by TOKUSHU KIKA
KOGYO Co., Ltd., Japan) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 2,000/sec and a stirring speed of 120 m/min in terms of the speed at which the outer end of an agitating element of the stirrer is rotated, thereby obtaining three cellulose dopes. The cellulose dopes produced from the cellulose slurries respectively having CNa values of 0.5 ~ by weight, 3 ~ by weight and 5 ~ by weight were, respectively, identified as the cellulose dopes of Examples 16, 17 and 18.
The dissolution ratio (Sc) of the cellulose in each of the cellulose dopes of Examples 16, 17 and 18 was 99.0 ~ by weight or more and, hence, the dissolu-tion performance was good. These cellulose dopes each exhibited a zero-shear viscosity (gyp) which satisfies ' 124 the formula (1). These dopes were stable for one week or more. With respect to other indexes of the dissolu-tion performance, i.e.. the longitudinal relaxation time (ic6) exhibited by the 6-position carbon atoms (C6) of the glucose units of the cellulose and the lon-gitudinal relaxation time (icl) exhibited by the 1-position carbon atoms (C1) of the glucose units of the cellulose, the celluloses of the cellulose dopes exhib-ited favorable values.
In Comparative Example 19, a slurry having a CNa value of 6.5 ~ by weight was produced in the same man-ner as in the production of the cellulose slurries used in Examples 16 to 18. From the cellulose slurry, a cellulose dope having a cellulose content of 7 ~ by weight and a CNa value of 7.6 ~ by weight was prepared in substantially the same manner as in Examples 16 to 18.
The dope obtained in Comparative Example 19 exhib-ited a zero-shear viscosity (~o) which was higher than the range satisfying the formula (1), and this indi-Gates that the dope is likely to exhibit gelation. Ac-tually, the dope obtained in Comparative Example 19 was unstable, and gelation occurred only one day after the preparation of the dope. Further, both ic6 and icl values were unfavorable.

The data of Examples 16 to 18 and Comparative Ex-ample 19 are shown in Table 4.
Table 4 Longitudinal CN Stability of relaxation a ~o dope time ~ (ms) (~ by weight) s) (mPa ic6 icl 0.5 25000 Stable for 180 300 one (Example 16) week or more 3 11800 Stable for 140 450 one (Example 17) week or more 19500 Stable for 170 370 one (Example 18) week or more 6.5 Gelation occurred (Comparative 46000 one day after 560 190 Example 19) preparation Examples 19 to 22 In each of Examples 19 to 22, the influence of a reagent (additive) on the dissolution of cellulose is examined and shown.
A sulfite process dissolving pulp (manufactured and sold by Nippon Paper Industries Co., Ltd., Japan) was hydrolyzed by the steam explosion method, thereby obtaining cellulose. The obtained cellulose was mixed with sodium hydroxide so that the resultant aqueous mixture had a cellulose solids content of 10.5 ~ by ' 126 weight and a CNa (sodium hydroxide concentration) value of 4 ~ by weight. The obtained aqueous mixture was subjected to wet pulverization by using a stirred medi-um wet grinding apparatus (APEX MILL AM-1, manufactured and sold by KOTOBUKI Engineering and Manufacturing, Co., Ltd., Japan) for 6 minutes, thereby obtaining a cellu-lose slurry containing particulate cellulose having a DPc value of 540 and an average particle diameter of 12 Vim. 190.48 g of the obtained cellulose slurry was placed in a 300 ml beaker and cooled to 0 °C. To the cooled cellulose slurry was added 59.52 g of an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 19.12 ~ by weight and which contained the below-mentioned additive (the amount of additive:
O.l mole/mole of glucose units) and which had been kept at -10 °C, thereby adjusting the composition of the slurry so that the slurry had a weight of 250 g, a cel-lulose content of 8 ~ by weight and a CNa (sodium hy-droxide concentration) value of 7.6 ~ by weight and that the amount of the additive became 0.1 mole/mole of glucose units. Then, the cellulose slurry was subject-ed to a low speed stirring by using a stirrer (T. K.
HOMO-MIXER, manufactured and sold by TOKUSHU KIKA KOGYO
Co., Ltd., Japan) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 2,000/sec and a stirring speed of 120 m/min in terms of the speed at which the outer end of an agitat-ing element of the stirrer is rotated, thereby obtain-ing a cellulose dope. As the above-mentioned additive, acrylonitrile, acrylamide, carbon disulfide and propyl-ene oxide were individually employed, and the cellulose dopes containing them were, respectively, identified as Examples 19, 20, 21 and 22.
The results are shown in Table 5.
Table 5 Zero-shear Additive viscosity, Stability of dope 'YJ ( mP a ~ s ) le for one week or Acrylonitrile (Example 19) 2 50 0 0 mora le for one week or Acrylamide (Example 20) 3 0 0 0 0 mora stable for one week or Carbon disulfide (Exam 1e 12 0 0 0 more 21) p Stable for one week or Propylene oxide (Example 2 9 0 0 0 more 22) Range of the zero-shear viscosity (r~o) satisfying the formula (1) (mPa~s): 10573 to 105810 Examples 23 and 24 and Comparative Examples 20 and 21 An example of the production of a fiber as a cel-lulose shaped article is shown.
Sodium hydroxide was added to a sulfite process dissolving pulp (manufactured and sold by Nippon Paper Industries Co., Ltd., Japan) so that the resultant aqueous mixture had a cellulose solids content of 8.5 ~
by weight and a C~a (sodium hydroxide concentration) value of 4 ~ by weight. The obtained aqueous mixture was subjected to wet pulverization by using a stirred medium wet grinding apparatus (APEX MILL AM-1, manufac-tured and sold by KOTOBUKI Engineering and Manufactur-ing Co., Ltd., Japan) for 6 minutes, thereby obtaining a cellulose slurry containing particulate cellulose having a DPc value of 720 and an average particle diameter of 12 ~.m. The obtained cellulose slurry was cooled to 0 °C. To 10 parts by weight of the cooled cellulose slurry was added 7 parts by weight of an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 12.75 ~ by weight and which had been kept at -10 °C, thereby adjusting the composi-tion of the cellulose slurry so that the slurry had a cellulose content of 5 ~ by weight and a sodium hydrox-ide concentration of 7.6 ~ by weight. Then, the cellu-lose slurry was subjected to stirring by using a low speed stirring type kneader (twin-screw kneader) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 500/sec and a stirring speed of 15 m/min in terms of the speed at ' 129 which the outer end of an agitating element of the stirrer is rotated, thereby obtaining a cellulose dope having a cellulose content of 5 ~ by weight and a sodi-um hydroxide concentration of 7.6 ~ by weight.
The obtained cellulose/sodium hydroxide aqueous solution (dope) was subjected to deaeration under vac-uum, and then to spinning by the following method. The dope was discharged through a spinneret nozzle having 100 holes (each having 0.08 mm fb) into a 25 cm length bath containing an aqueous 25 ~ by weight sulfuric acid solution at -5 °C, at a discharge rate of 30.2 ml/min (a discharge speed of 60 m/min), thereby coagulating the dope in the aqueous sulfuric acid solution, while taking up the resultant fibrous body (fiber) at a take up speed of 60 m/min. The obtained fiber was subjected to water washing and then drying using a heat roll at 120 °C, and wound around a reel at a rate of 60 m/min.
This fiber was identified as the fiber of Example 23.
Substantially the same procedure as described above (Example 23) was repeated except that the discharge rate of the dope was.change to 50.3 ml/min (a discharge speed of 100 m/min), and the coagulation, water washing and drying were conducted while taking up the formed ffiber at a take up speed of 100 m/min. The obtained fiber was identified as the fiber of Example 24.

' 130 For comparison, the following experiments were conducted. A pulp was subjected to steam treatment for 4 minutes by using saturated steam at a pressure of 8.5 kg/cm2, thereby obtaining a hydrolyzed pulp. The hy-drolyzed pulp was subjected to wet pulverization under the same conditions as described above, thereby obtain-ing a cellulose slurry containing particulate cellulose having a DPc value of 310. Then, with respect to the obtained cellulose slurry, the dissolution of the cel-lulose (preparation of a dope) and the spinning of the dope were conducted in substantially the same manner as described in connection with production of the fibers of Examples 23 and 24 (i.e., substantially the same procedures as in Examples 23 and 24 were repeated ex-cept that the above-obtained cellulose slurry contain-ing particulate cellulose having a DPc value of 310 was employed). These comparative experiments respectively for comparison with Examples 23 and 24 were, respec-tively, identified as Comparative Examples 20 and 21.
The strengths and elongations of the obtained fi-bers are shown in Table 6.

Table 6 Example Example Comparative Comparative 23 24 Example 20 Example 21 Take up 60 m/min 100 m/min 60 m/min 100 m/min speed Spinning was Strength 1 impossible 2 . 6 . because of ( g/d) fiber breakage Spinning was Elonga-impossible tion 16.8 13.1 11.g because of fiber breakage The fibers of Examples 23 and 24, which were ob-tained from dopes having a high DPc value, exhibited strengths exceeding 2 g/d (denier). By contrast, the fiber of Comparative Example 20, which was obtained from a dope having a low DPc value, exhibited a low strength (1.5 g/d). This value (1.5 g/d) is lower than the strength of a regular viscose rayon.
In Comparative Example 21, the strength of the gel fiber being coagulated was too low, so that a spinning while taking up at a take up speed of 100 m/min was not able to be conducted. In the production of a regular viscose filament, the take up speed of 100 m/min is a lowest level of take up speed, and use of a take up speed lower than 100 m/min is impractical from the viewpoint of productivity.

Examples 25 to 27 and Comparative Examples 22 and 23 An example of the production of a flat film as a cellulose shaped article is shown.
In substantially the same manner as in Examples 9, 12 and 15, dopes which respectively had DPc values of 350, 540 and 720 and each of which had a cellulose con-tent of 5 ~ by weight and a sodium hydroxide concentra-tion of 7.6 ~ by weight were obtained. (These dopes were, respectively, identified as the dopes of Examples 25, 26 and 27.) For comparison, dopes respectively having DPc values of 200 and 310 were obtained in sub-stantially the same manner as mentioned above. (These dopes were, respectively, identified as the dopes of Comparative Examples of 22 and 23.) Each of the obtained dopes was individually sub-jected to deaeration under vacuum, and then individual-ly cast on a glass plate so that the resultant dope film had a thickness of 500 Nrn. The formed dope films were subjected to coagulation for 5 minutes by means of an aqueous 25 ~ by weight sulfuric acid solution at -5 °C and then fully washed with water to thereby ob-tain gel films. The strengths of the obtained gel films were measured. The results obtained with respect to Examples 25, 26 and 27 and Comparative Examples 22 and 23 are shown in Fig. 2. The films obtained from the dopes of Comparative Examples 22 and 23 (dopes re-spectively having DPc values of 200 and 310) both had strengths as low as 40 kg/cm2 or less. With respect to cellulose shaped articles having such a low level of gel strength, it is difficult to produce the shaped ar-ticles (such as fibers and films) in high productivity on a commercial scale. Further, in some cases, commer-cial-scale production of such low strength shaped arti-cles requires use of a special apparatus (as disclosed in Unexamined Japanese Patent Application Laid-Open Specification No. 7-278941) which enables a consider-able lowering of the tension sustained by cellulose shaped articles during the production process thereof.
As seen from Example 25, when the DPc value was in-creased to 350, the gel strength sharply increased to a level which is about 2 times the strength achieved at the DPc value of 310. Further, as seen from Example 27, the gel strength achieved at the DPc value of 720 was 4 times the strength achieved at the DPc value of 310.
The same dope as the dope of Example 27 (having a DPc value of 720) was subjected to deaeration under vacuum, and then cast on a glass plate so that the re-sultant dope film had a thickness of 500 ~zn. The dope film was subjected to drying by heating until the water content thereof became 5 ~ by weight or less to thereby coagulate the dope. The resultant was washed with water and dried to obtain a film. The strength of the obtained film was more than 1,800 kg/cm2, which is a value by far higher than the strength of a regular cel-lophane film.
Examples 28 to 30 An example of the production of a flat film from a dope containing incorporated therein a polysaccharide or a polypeptide is shown.
Sodium hydroxide was added to a sulfite process dissolving pulp (CELLUNIER-F, manufactured and sold by Rayonier, U.S.A.) so that the resultant aqueous mixture had a cellulose solids content of 8.5 ~ by weight and a CNa (sodium hydroxide concentration) value of 2 ~ by weight. The obtained aqueous mixture was subjected to wet pulverization by using a stirred medium wet grind-ing apparatus (APEX MILL AM-1, manufactured and sold by KOTOBUKI Engineering and Manufacturing Co., Ltd., Ja-pan) for 6 minutes, thereby obtaining a cellulose slur-ry containing particulate cellulose having a DPc value of 620 and an average particle diameter of 10 E,~m. To the obtained slurry were individually added starch, ca-sein and collagen to thereby obtain three types of mix-tures. The obtained three types of mixtures were cooled to 0 °C. To each of the cooled mixtures was added an aqueous sodium hydroxide solution which had a sodium hydroxide concentration of 30 ~ by weight and which had been kept at -10 °C, thereby adjusting the compositions of the mixtures so that the mixtures each had a cellulose content of 4 ~ by weight, a starch con-tent, casein content or collagen content of 4 ~ by weight and a sodium hydroxide concentration of 7.6 ~ by weight. Then, the mixtures were subjected to a low speed stirring by using a stirrer (T. K. HOMO-MIXER, manufactured and sold by TOKUSHU KIKA KOGYO Co., Ltd., Japan) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 2,000/sec and a stirring speed of 120 m/min in terms of the speed at which the outer end of an agitating ele-merit of the stirrer is rotated, thereby obtaining three types of dopes. The dopes respectively containing starch, casein and collagen were, respectively, identi-fied as the dopes of Examples 28, 29 and 30. Each of the obtained three types of dopes was individually sub-jetted to deaeration under vacuum, and then individual-ly cast on a glass plate so that the resultant dope film had a thickness of 500 Eun. The formed dope films were subjected to coagulation for 5 minutes by means of an aqueous 25 ~ by weight sulfuric acid solution at -5 °C, and then washed with water and dried to thereby obtain flat films. The film of Example 28 containing starch, the film of Example 29 containing casein and the film of Example 30 containing collagen respectively exhibited dry strengths of 1,100 kg/cm2, 770 kg/cm2 and 1,050 kg/cm2. All of the three films had excellent flexibility and excellent palatableness.
Example 31 and Comparative Example 24 An example of the production of a tubular film as a cellulose shaped article is shown.
Sodium hydroxide was added to a sulfite process dissolving pulp (DERIVAT LV-U, manufactured and sold by BORREGAARD, Norway) so that the resultant aqueous mix-ture had a cellulose solids content of 8.5 ~ by weight and a CNa (sodium hydroxide concentration) value of 4 by weight. The obtained aqueous mixture was subjected to wet pulverization by using a stirred medium wet grinding apparatus (APEX MILL AM-1, manufactured and sold by KOTOBUKI Engineering and Manufacturing Co., Ltd., Japan) for 6 minutes, thereby obtaining a cellu-lose slurry containing particulate cellulose having a DPc value of 660 and an average particle diameter of 11 Vim. The obtained cellulose slurry was cooled to 0 °C.

To the cooled cellulose slurry was added an aqueous so-dium hydroxide solution which had a sodium hydroxide concentration of 16.2 % by weight and which had been kept at -10 °C, thereby adjusting the composition of the cellulose slurry so that the slurry had a cellulose content of 6 ~ by weight and a sodium hydroxide concen-tration of 7.6 ~ by weight. Then, the cellulose slurry was subjected to a low speed stirring by using a stir-rer (T. K. HOMO-MIXER, manufactured and sold by TOKUSHU
KIKA KOGYO Co., Ltd., Japan) under stirring conditions wherein the stirring is performed at -4 °C for 10 min at a shear rate of 2000/sec and a stirring speed of 120 m/min iri terms of the speed at which the outer end of an agitating element of the stirrer is rotated, thereby obtaining a dope. From the obtained dope, a tubular film was produced by the following method. The ob-tained dope was discharged through an annular slit noz-zle which was provided in a bath containing an outside coagulation liquid and which was directed toward the upside so that the dope was discharged vertically up-wardly into the outside coagulation liquid at a dis-charge linear velocity of 15 m/min, thereby coagulating the discharged dope in the bath, while taking up the resultant coagulated tubular film upwardly at a take up speed of 30 m/min. The diameter of the annular slit nozzle was 20 mm and the width of the slit was 500 ~.m.
The outside coagulation liquid was an aqueous 25 ~ by weight sulfuric acid solution kept at -5 °C. At the central portion of the annular slit nozzle was provided an internal pipe which extended upwardly up to a level which was a little higher than the liquid level of the outside coagulation liquid bath, wherein an inside co-agulation liquid was introduced from the downside into an annular space vertically extending between the outer wall of the internal pipe and the inner wall of the tu-bular film being coagulated, so that the outer and in-ner walls of the tubular film being formed are in con-tact with the outside and inside coagulation liquids, respectively. The inside coagulation liquid ascended up to the upper end of the internal pipe, and then overflowed into the inside of the internal pipe and was allowed to fall down to be discharged through the in-ternal pipe. Since the level of the upper end of the internal pipe is higher than the liquid level of the outside coagulation liquid bath (wherein the outside coagulation liquid is in contact with the outer wall of the tubular film being formed), the level of the inside coagulation liquid becomes higher than the liquid level of the outside coagulation liquid bath (wherein the outside coagulation liquid is in contact with the outer wall of the tubular film being formed). Consequently, at the upper portion of the tubular film which is posi-tinned at a level higher than the liquid level of the outside coagulation liquid bath, the tubular film being formed becomes a little expanded by the from-inside-toward-outside pressure which is exerted by the inside coagulation liquid on the inner wall of the tubular film being formed. By this method for the production of a film, it is possible to improve the isotropy of the molecular orientation of the cellulose of the film obtained. The tubular film which had been coagulated by neutralization was washed with water and then dried.
The drying step was conducted under conditions wherein pressurized air is kept in the inside of the tubular film. By this drying operation, a film having more im-proved isotropic molecular orientation can be obtained.
The obtained tubular film was identified as the tubular film of Example 31. The tubular film of Example 31 had a strength of 1,470 kg/cm2 in the direction of the film formation and a strength of 1,340 kg/cm2 in the direc-tion from the center to the circumference of the tubu-lar film. In Comparative Example 24, an attempt was made to produce a tubular film from a dope having a DPc value of 310. However, since the strength of the gel film during the coagulation step was low, the produc-tion of the film was not able to be stably conducted.
Examples 32 and 33 and Comparative Example 25 An example of the production of a sponge as a cel-lulose shaped article is shown.
A cellulose dope was produced in the same manner as in the above-mentioned example of the production of a tubular film. The temperature of 300 g of the ob-tained dope was adjusted to 10 °C, and thereto were added 4 g of polyester fibers having an average fiber length of 5 mm and a thickness of 1 denier and either 500 g of Glauber's salt having an average particle diameter of 3 mm (as Example 32) or 500 g of sodium me-tasilicate nonahydrate (Na2Si03~9H20) (as Example 33), followed by kneading. Each of the resultant kneaded mixtures was individually shaped into a block, and sub-jected to gelation at 90 °C, and then to neutralization with an aqueous sulfuric acid solution, followed by wa-ter washing and drying, thereby obtaining a sponge.
The obtained sponges were, respectively, identified as the sponges of Examples 32 and 33. As Comparative Ex-ample 25, a sponge was produced in substantially the same manner as described above except that a dope hav-ing a DPc value of 310 was used. The sponges of Exam-ples 32 and 33, having a high DPc value, exhibited sat-isfactory strength even in a wet state. By contrast, when the sponge of Comparative Example 25 was in a wet state, the sponge was easily torn and hence found to be unsuitable for practical use.
Examples 34 to 36 and Comparative Examples 26 and 27 An example of the production of a coating as a cellulose shaped article is shown.
A cellulose dope was produced in the same manner as in the above-described example of the production of a tubular film. The obtained dope was roll-coated on a high density paper sheet (substrate) having a density of 250 g/m2 so that the dope was coated in an amount of 5 ~ by weight in terms of the weight of the cellulose, based on the weight of the substrate paper. The resul-tant dope-coated high density paper sheet was subjected to drying by means of a heat roll at 90 °C to thereby coagulate the dope on the paper sheet, and then to neu-tralization with an aqueous 20 ~ by weight sulfuric ac-id solution at 20 °C, followed by water washing and then drying using a heat roll at 90 °C, thereby obtain-ing a cellulose-coated~paper sheet. This cellulose-coated paper sheet was identified as the cellulose-coated article of Example 34. The results of Example 34 are shown in Table 7.

The cellulose-coated article of Example 34 exhib-ited a water permeability which is only about 1/10,000 of the water permeability of the original non-coated high density paper sheet. That is, the cellulose coat-s ing greatly reduced the water permeability of the high density paper sheet. This water permeability of the cellulose-coated article is considerably smaller than the water permeability (about 1 to 5 liters/(m2~hr~kg/
cm2)) of a commercially available reverse osmosis mem-brane. This means that the cellulose-coated article of Example 34 exhibits a substantially complete water bar-rier property. This cellulose-coated article also ex-hibited an excellent gas barrier property. Specifi-cally, this cellulose-coated article exhibited an oxy-gen permeability of only 40 cc/m2/24 hr/atm, as meas-ured at 23 °C and a relative humidity of 65 ~. This cellulose-coated article also exhibited a very excel-lent oil resistance. Specifically, when the oil resis-tance of this cellulose-coated article was measured in accordance with the TAPPI RC-338 method, the article exhibited a Kit value of 12 or more, indicating that the article exhibits a highest level of oil resistance.
The surface of this cellulose-coated article exhibited a slight hydrophobicity, and exhibited a contact angle of 55° with water.

A paper cup was prepared from the cellulose-coated article of Example 34. Even when hot water was poured into the prepared paper cup, no bad smell was perceived.
Since this cellulose-coated article exhibited excellent properties in that the water permeability is low, the imperviousness to an oil (such as an edible oil) is high, the oxygen barrier property is high, and no bad smell is generated, the cellulose-coated article can be applied to in the food-related fields, such as food packaging materials and trays. As Comparative Example 26, substantially the same procedure as in Example 34 was repeated except that a cellulose/sodium hydroxide aqueous solution having a DPc value of 310 was used as a coating material. With respect to water impermeabil-ity, oil resistance and oxygen barrier property, the cellulose-coated article of Comparative Example 26 ex-hibited substantially the same properties as those of the cellulose-coated article of Example 34. However, since the cellulose used in Comparative Example 26 had a low DPc value, it exhibited low strength. Specifi-cally, when the cellulose-coated article of Comparative Example 26 was rubbed in water, the cellulose coating came off in the form of small flakes. Therefore, the cellulose-coated article of Comparative Example 26 can-not be practically used.

The same dope as used in Example 34 was coated on a kraft paper sheet having a density of 50 g/m2 by means of a gravure coater so that the dope was coated in an amount of 0.2 ~ by weight in terms of the weight of the cellulose, based on the weight of the substrate paper. The resultant dope-coated paper sheet was sub-jected to drying at 90 °C to thereby coagulate the dope on the paper sheet, and, then, the resultant was thor-oughly washed with water (as Example 35) or subjected to neutralization of the alkali values with an aqueous citric acid solution (as Example 36). Then, the resul-tant was again subjected to drying, to obtain a cellu-lose-coated article. In any of Example 35 and Example 36, the obtained cellulose-coated article exhibited a Kit value of 12 or more, indicating that the article exhibits a highest level of oil resistance. As shown in Examples 35 and 36, the amount of the coating on the article may be small. In addition, as shown in Example 36, water washing is not necessary. Therefore, there is an advantage in that the coating can be performed by means of an ordinary gravure coater. In Comparative Example 27, the oil resistance of an oil resistant pa-per (density: 54 g/m2) (manufactured and sold by Oji Paper Co., Ltd., Japan) was measured by the same method as mentioned above. The commercially available oil re-sistant paper was found to exhibit a Kit value of 9, showing that the oil resistance of the oil resistant paper is lower than the oil resistances of the cellu-lose-coated articles of Examples 35 and 36.
The data of Examples 34 to 36 and Comparative Ex-amples 26 and 27 are shown in Table 7.

Table 7 Amount Water per-Kit value Oxygen Abrasion of coating meability permeabil- resis-(% based (liter/ ity tance in on the atmm2hr) (ml/atmm2 water weigh of 24hr) substrate paper) High den- - 1360 1 or less - -sity paper Example 34 5 0.10 12 or more 40 Example 35 0.2 100 12 or more - 0 Example 36 0.2 125 12 or more -Comparative 5 0.16 12 or more 110 X

Example 26 Comparative Example 27 (oil resis-tant paper - _ 9 - -manufactured and sold by Oji Paper Co., Ltd.) INDUSTRIAL APPLICABILITY
The cellulose dope of the present invention is stable and free from gelation even when the cellulose dope has a high content of cellulose having a rela-tively high degree of polymerization (DPc). By the use of the cellulose dope of the present invention, a re-generated cellulose shaped article (such as a fibrous body, a flat film, a tubular film, a hollow fiber, a particle, a sponge body or a coating) which has a mechanical strength sufficient for practical use can be easily and stably produced without using a large amount of a poisonous substance (such as carbon disulfide or cuprammonium) and without using special molding appara-tus. Therefore, the cellulose dope of the present in-vention is commercially very advantageous.

Claims

1. A cellulose dope comprising an aqueous sodium hy-droxide solution and cellulose dissolved in said solu-tion, said cellulose dope having a sodium hydroxide con-centration (C Na) of from 6.5 to 11% by weight and a cellulose content (Cc) of from 4 to 12% by weight, wherein said cellulose dope exhibits a zero-shear viscosity (.eta.0) which satisfies the following formula (1):

.eta.0= kCc m x DPc p (1) wherein:

represents the zero-shear viscosity (mPa.multidot.s) of the cellulose dope, Cc represents the cellulose content (% by weight) of the cellulose dope, DPc represents the viscosity average degree of polymerization of the cellulose in the cellu-lose dope, k = 3.9 x 10-11, m is a number of from 5 to 7, and p is a number of from 3 to 4.

2. The cellulose dope according to claim 1, wherein the viscosity average degree of polymerization (DPc) of the cellulose is from 350 to 1,200, and the cellulose content (Cc) is from 5 to 10 % by weight, and wherein m and p are from 6.3 to 6.5 and from 3.2 to 3.5, respec-tively.

3. The cellulose dope according to claim 1 or 2, wherein, in the NMR analysis of the cellulose dope, the 6-position carbon atoms of the glucose units of the cellulose exhibit a longitudinal relaxation time (~c) of from 10 to 400 ms, and the 1-position carbon atoms of the glucose units of the cellulose exhibit a longi-tudinal relaxation time (~c) of from 200 to 10,000 ms.

4. The cellulose dope according to claim 3, wherein, in the NMR analysis of the cellulose dope, the 6-position carbon atoms of the glucose units of the cel-lulose exhibit a longitudinal relaxation time (~c) of from 10 to 200 ms.

5. The cellulose dope according to any one of claims 1 to 4, wherein the hydroxyl groups of the cellulose are partially modified by reaction with a reagent which is reactive with a hydroxyl group in the presence of an alkali.

6. The cellulose dope according to claim 5, wherein said reagent is selected from the group consisting of an etherification agent and a xanthation agent.

7. The cellulose dope according to claim 5 or 6, wherein said reagent is used in an amount of 0.1 mole or less per mole of glucose units in the cellulose.

8. A method for producing the cellulose dope of claim 1, which comprises:

(1) providing a cellulose slurry comprising an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average parti-cle diameter of 30µm or less, said cellulose slurry having a sodium hydroxide concentration of from 0.5 to less than 6.5% by weight and a cellulose content of 5% by weight or more, (2) adjusting the sodium hydroxide concentration of the cellulose slurry to 6.5 to 11% by weight, and (3) stirring the cellulose slurry at 10°C or less by means of a stirrer under stirring conditions satis-fying at least one requirement selected from the group consisting of the requirement that the stirring is per-formed at a shear rate of 9,000/sec or less and the re-quirement that the stirring is performed at a stirring speed of 500 m/min or less in terms of the speed at which the outer end of an agitating element of the stirrer is rotated, said steps (2) and (3) being conducted in the or-der of step (2) and step (3) or simultaneously, thereby causing the particulate cellulose to be dissolved in the cellulose slurry to the extent that the cellulose has a dissolution ratio of 99.0% by weight or more, to obtain a cellulose dope, wherein said cellulose slurry satisfies the fol-lowing formula (2):
.sigma.T = K1exP(k1C Na) (2) wherein:
.sigma.T represents the yield stress (Pa) of said slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and C Na is the sodium hydroxide concentration (% by weight) of said slurry, and wherein, in the solid state NMR analysis of said slurry, the cellulose in said slurry exhibits a non-crystallinity (~am) of 0.5 or more, said non-crystallinity being defined by the following formula (3):

~am = I high / (I high + I low) (3) wherein:

~am is the non-crystallinity of the cellulose in said slurry, and I high and I low respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of said slurry, wherein the peaks are, respectively, ascribed to the higher magnetic field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in said slurry, and wherein separation between said peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of said peaks is approximated to the Gaussian dis-tribution function.

9. The method according to claim 8, wherein said cel-lulose slurry satisfies the following formula (4):

.sigma.T = K2 + k2DPc wherein:

.sigma.T represents the yield stress (Pa) of said slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in said slurry.

10. The method according to claim 8 or 9, wherein said cellulose in said cellulose slurry has an average par-ticle diameter of 20 µm or less.

11. The method according to any one of claims 8 to 10, wherein said cellulose in said cellulose slurry has a viscosity average degree of polymerization (DPc) of from 350 to 1,200.

12. The method according to any one of claims 8 to 11, wherein the hydroxyl groups of said cellulose in said cellulose slurry are partially modified by reaction with a reagent which is reactive with a hydroxyl group in the presence of an alkali.

13. The method according to any one of claims 8 to 11, which further comprises, at a point in time which is after step (1) and before the end of step (3), adding to the cellulose slurry a reagent which is reactive with a hydroxyl group in the presence of an alkali.

14. The method according to claim 12 or 13, wherein said reagent is selected from the group consisting of an etherification agent and a xanthation agent.

15. The method according to any one of claims 12 to 14, wherein said reagent is used such that the amount of the reagent is 0.1 mole or less per mole of glucose units in the cellulose in said cellulose dope.

16. A cellulose shaped article obtained by subjecting the cellulose dope of any one of claims 1 to 7 to at least one coagulation treatment selected from the group consisting of drying coagulation, gelation coagulation and neutralization coagulation.

17. The cellulose shaped article according to claim 16, wherein the cellulose dope contains at least one addi-tive selected from the group consisting of a polysac-charade, a polypeptide and a natural resin.

18. The cellulose shaped article according to claim 16 or 17, which is a fibrous body, a flat film, a tubular film, a hollow fiber, a particle, a sponge body or a coating.

19. A cellulose slurry comprising an aqueous sodium hydroxide solution and, dispersed therein, particulate cellulose having an average particle diameter of 30 µm or less, said cellulose slurry having a sodium hydroxide concentration of from 0.5 to less than 6.5% by weight and a cellulose content of 5% by weight or more, wherein said cellulose slurry satisfies the fol-lowing formula (2):

.sigma.T = K1exp (k1C Na) (2) wherein:

.sigma.T represents the yield stress (Pa) of said slurry, K1 represents an arbitrary constant (Pa), k1 is 0 or less, and C Na is the sodium hydroxide concentration (% by weight) of said slurry, and wherein, in the solid state NMR analysis of said slurry, the cellulose in said slurry exhibits a non-crystallinity (~am) of 0.5 or more, said non-crystallinity being defined by the following formula (3):
~am = I high / (I high + I low) wherein:

~am is the non-crystallinity of the cellulose in said slurry, and I high and I low respectively represent the ratios of the areas of the peaks in a solid state NMR
spectrum of said slurry, wherein the peaks are, respectively, ascribed to the higher magnetic field component and lower magnetic field compo-nent of the 4-position carbon atoms of the glu-cose units of the cellulose in said slurry, and wherein separation between said peaks respec-tively ascribed to the higher magnetic field component and the lower magnetic field compo-nent is made using a method in which each of said peaks is approximated to the Gaussian dis-tribution function.

20. The cellulose slurry according to claim 19, which satisfies the following formula (4):

.sigma.T = K2 + k2DPc (4) wherein:

.sigma.T represents the yield stress (Pa) of said slurry, K2 represents an arbitrary constant (Pa), k2 is 0 or less (Pa), and DPc represents the viscosity average degree of polymerization of the cellulose in said slurry.

21. The cellulose slurry according to claim 19 or 20, wherein said cellulose has an average particle diameter of 20 µm or less.