CA2153583A1 - Process for the preparation of polyketone fibres - Google Patents
Process for the preparation of polyketone fibresInfo
- Publication number
- CA2153583A1 CA2153583A1 CA002153583A CA2153583A CA2153583A1 CA 2153583 A1 CA2153583 A1 CA 2153583A1 CA 002153583 A CA002153583 A CA 002153583A CA 2153583 A CA2153583 A CA 2153583A CA 2153583 A1 CA2153583 A1 CA 2153583A1
- Authority
- CA
- Canada
- Prior art keywords
- polymer
- solvent
- process according
- temperature
- solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/28—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from copolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds
- D01F6/30—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from copolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds comprising olefins as the major constituent
Abstract
It has been found that fibres can be spun in a simple manner from polyketone polymer solutions by making a thermoreversible gel from a solution of polyketone and a solvent for the polymer having a boiling temperature above 443 K, a melting temperature below 373 K and a polymer dissolving temperature above 443 K. The thermoreversible gel forms as the solution is cooled. Because of the specific properties of the solvent in combination with the concentration of the polymer and its intrinsic viscosity, a permanently orientable thermoreversible gel is formed by cooling. The polymer crystallises on being cooled, optionally while still in the presence of the solvent.
Preferably, so much polymer is dissolved as will give a product of the polymer concentration and [n]0,5 (wherein [n] represents the intrinsic viscosity of the polymer) of higher than 0,35 (dl/g)0,5.
Preferably, so much polymer is dissolved as will give a product of the polymer concentration and [n]0,5 (wherein [n] represents the intrinsic viscosity of the polymer) of higher than 0,35 (dl/g)0,5.
Description
21~3583 AFP 2330 R
PROCESS FOR THE PREPARATION OF POLYKETONE FIBRES
The invention relates to a process for the preparation of fibres of a linear polymer of alternating ethylene and carbon monoxide units, in which process the polymer is dissolved in an appropriate solvent having a boiling temperature above 443 K (170C), a melting tem-perature below 373 K (100C), and a polymer dissolving temperature above 443 K (170C), the polymer solution, after being moulded, is converted to a thermoreversible gel by cooling, and the solvent is removed from the obtained product.
Such a process is known from International Patent Application WO
92/10524, which describes intermixing an ethylene/carbon monoxide copolymer with a second component to produce polymer compositions suitable for making gel-based articles, amongst others components capable of dissolving the polymer and spinning it into fibres, and components which cause the polymer to swell and are not considered suitable~for fibre pr~duction.
According to this very general descripti~n,~it fs possible ta prepare a thread-like, thermoreversible gel using the aforementioned polymer dissolving means, but none of said substances has proved easily suited to practical use. For instance, many of the solvents and swelling agents mentioned have a low boiling point, which results in slow crystallisation of the polymer in the solution on cooling. Also described are solvents which in practice were found to dissolve the polyketone less readily if higher concentrations are employed. Not a single practical example of good quality fibres being prepared from such solvents is provided. The only example in which a highly concentrated solutiQn is prepared uses ~benzoic acid as a solvent, but this solvent was found to be unsuitable for the preparation of good quality fibres because of interference between the solvent and polymer crystallisation as the solution cools, which has an adverse effect on the mechanical properties of the products to be obtained. It was further found that benzoic acid breaks down the polyketone polymer.
~JIENIY~O S~EE~
- 215~S83 A process has now been found which is free of these drawbacks. This - process of the type mentioned in the opening paragraph provides a highly economical method of preparing polyketone fibres of favourable - mechanical properties, and is characterised in that a permanently orientable thermoreversible gel is formed.
Use is made in this process of a comparatively poor polymer solvent, with such a high polymer concentration in the solvent being selected as will give sufficient and homogeneous intermingling of the polymer's molecular chains. The polymer crystallises on cooling, without the solvent needing to have been removed. Thus, a thermoreversible gel of such properties is formed by cooling as will permit drawing of the gel without removal of the solvent. The drawing process serves to permanently orient the polymer's molecular chains.
According to the novel process, it is possible to obtain at a high rate and in large quantities a fibre having favourable mechanical pru~,l-ies an~ fro~ w~ch the- sol:vent - c~n be rem~ued~ compar~tively easily.
In general, so much polymer is dissolved in order to prepare a permanently orientable thermoreversible gel that the product of the polymer concentration and [~]o~S is higher than 0,35 (dl/g)o~S. [~] in this process was measured in an m-cresol solution at 298 K (25C).
Although the fact that W0 92/10524 describes, in a very general way, the possibility of preparing highly concentrated solutions, the statement that a minute portion of the mentioned means forms solvents for the polymer from which permanently orientable fibres can be made, has not b~een substantiated, nor has been- indicated~when ~and/or how these can be obtained.
The process now found comprises the following components:
- polyketone polymer of the proper intrinsic viscosity, a mediocre or even poor solvent in which the polymer takes up a comparatively small hydrodynamic volume, and A~AENDED SHE~T
21~35~3 a device for thoroughly intermixing the polymer and the solvent at a relatively high temperature and with forceful mechanical agitation.
Hydrodynamic volume is defined as the product of the intrinsic viscosity of the polyketone polymer in a particular solvent at the processing temperature and the average molecular weight.
According to the process found, these components are utilised such that:
a homogeneous solution is formed in such a concentration as will have overlapping of the molecular chains, which overlapping is preserved after cooling to below the crystallisation temperature of the solution, the homogeneous solution is extruded, and the resulting extrudate rapidly gels as it is cooled on account of the formation of crystalline nuclei, causing a thermoreversible gel to be formed which is drawable to a draw ratio ~A) of at least 6 and by being drawn to a draw ratio between 6 and 13 produces ~n ortented fib`-re with an initial modulus equal to or higher than 10/9-A-2,5 (N/tex).
Preferably, an oriented fibre with an initial modulus higher than 1O/9 A-1~75 (N/tex) is obtained. In a further preferred embodiment, the initial modulus is at least 1O/9 A-1 (N/tex), but will be less than 10/9-A+4 (N/tex). The optimal oriented fibre will have an initial modulus which at least fulfills the equation:
O~259+1~752.A-O~114.A2+O~OO625.A3-O~OOOO9.A4.
Thus, in the present invention, a permanently orientable thermoreversible gel is formed if said gel is drawable to a draw ratio of at least 6 and if from said gel an oriented fibre can be obtained which has an initial modulus in the range of 10/9~ 275 (N/tex) to 10/9-A+4 (N/tex) for a draw ratio between 6 and 13.
The process now found is so exceptional in particular because it is not subject to the drawbacks of traditional gel spinning and comes AMENDED SHEET
- 2153~83 very close to the meltspinning process which is so economically advantageous. This is advantageous in particular for some types of ethylene and carbon monoxide units containing polymers which are not melt processable on account of their degradation at the temperature required for polymer melt processing.
The solvents used are those which are generally considered to be so-called poor solvents for the polymer. The boiling point of these solvents is above 443 K (170C), more particularly above 453 K
(180C), and in a most preferred embodiment above 477 K (204C). These solvents will not dissolve the polymer in its entirety except with heating to a temperature above 443 K (170C),preferably to above 453 K
(180C), and most preferably to above 477 K (204C). In most cases, the temperature at which there is virtually complete polymer dissolution lies below the boiling point of the solvent, so that the dissolving process can easily be carried out under atmospheric pressure. In the case of a number of solvents, a suitable process for preparing a polymer solution lies in selecting a dissolving temperature equal to or higher than the boiling point of the solvent.
Such a process may be carried out with advantage when, e.g., benzyl alcohol is used as solvent. At temperatures which do not exceed the boiling temperature by more than 5 K (5C), operating under a pressure above 100 kPa will not be required in every case. At higher temperatures, however, this requirement will always be there.
The dissolving temperature of polyketone in a particular solvent is defined as the temperature at which virtually complete dissolution of 5-10 wt.% of polyketone having an intrinsic viscosity of about 7 is observed in that particular solvent.
Selecting the polymer concentration such that the product of the polymer concentration and [~]o.S is higher than 0,35 (dl/g)o~S will give a solution in which the molecular chains of the polymer are sufficiently intermingled to form the desired thermoreversible gel upon crystallisation. [~] is measured in an m-cresol solution at a AMENDED SHEET
- 21~3!;8~
temperature of 298 K (25C).In this formula the polymer concentration is expressed as the fraction by weight of polymer in the solution. A
very satisfactory process consists in so selecting the polymer concentration that the solution's crystallisation temperature lies between 398 K (125C) and the boiling point of the solvent.
It has been found that while using a solvent which satisfies the above-mentioned characteristics at lower polymer concentrations will allow a homogeneous solution to be obtained, such a low-concentration solution of a solvent according to the invention will lead to phase separation upon cooling. In the case of such cooled solutions it is no longer possible to speak of a permanently orientable thermoreversible gel. The products obtained from such low-concentration solutions have mechanical properties which are inadequate for use. This was earlier described in EP 456 306.
In the preparation of a solution to form a thermoreversible gel the cohesion between the chains, and thus the gelling, may be enhanced by so selecting the cancr-ntratiQn of a polymer having ,a given intrinsic viscosity that~the product of the~po,lymer cQncentrati~ and [~o~S is higher than 0,4 (dl/g)o~s. More favourable results still are attained if the product of the polymer concentration and [~]o~ is higher than 0,5 (dl/g)o. 5 .
Not only are the properties of the end products manufactured from such solutions enhanced, using high polymer concentrations also has advantages as regards the amount of polymer processed per unit of time and the rate at which the solvent can be removed from the product.
In the aforesaid equation [~] represents the intrinsic viscosity of the palymer and is deter,mined as follo,ws: , [~] = lim ~pr-r = lim t - tn c~O c c~O to . C
so having the meaning of the ratio between the flow times t and to~
with to and t representing the flow time of the solvent and the AMENDED SHEET
2i535~ AFP 2330 R
polymer-containing solution, respectively, in a capillary viscometer at 298 K (25C). c in this equation has the meaning of the polymer con-centration in m-cresol, expressed in grams per deciliter.
The intrinsic viscosity of the polyketone used generally is in the range of 0,5 to 10 dl/g but may be higher. Polyketone highly suited to be used in the process now found has an intrinsic viscosity in the range of 1,2 - 8 dl/g, in particular in the range of 1,2 - 4,5 dl/g.
Very suitable polyketone for use in the present invention has an intrinsic viscosity in the range of 1,2 - 2,5 dl/g. The relation between the estimated molecular weight (Mw) (in grams per mole) and the intrinsic viscosity as utilised here can be established with the aid of the following formula:
[~] = 1,0 x 10-4 x MW0,85 The pnlyketone~ poly~me-r is prim~riily~ composed of alternating carbon monoxide~and~ethyle~e units according to the formula:
[- CH2 - CH2 - C - ]
In addition to carbon monoxide and ethylene units, this polymer may contain a small amount of other units, for instance propylene groups.
Also, other substances may be admixed, e.g., to improve the thermal and/or oxidative properties and/or other polymer and/or fibre properties. For the preparation of polyketone polymers reference is made to the following European Patent Specifications: 121 965;
222 454~; 227 135; 228 733~ 229~408~;~ 2~35 865; 235 86~; 239 145;~
245 893; 246 674; 246 683i 248 483; 253 416; 254 343; 257 663;
259 914; 262 745; 263 564; 264 159; 272 728; and 277 695.
It is not possible to prepare the desired thermoreversible gel which can be permanently oriented without the solvent having to be removed ENl~E~
- 21~3~83 if solvents are used of which the polymer dissolving temperature is lower than that mentioned in the claims. Using such solvents will result in thermoreversible gels which are far closer in character to gels prepared with a satisfactory solvent, which means, int. al., that the solvent cannot be removed from the obtained products without extraction, and the polymer concentration in the solutions obtained cannot be as high as presently found.
The process now found has the significant advantage of the polymer being crystallised by cooling under normal spinning operation conditions, such as normal cooling speed, while the processes hitherto known always required that an extracting agent be employed to carry out the desired polymer crystallisation. In a highly preferred embodiment of the present invention, the polymer is crystallised by cooling to room temperature under normal spinning conditions. Since the polymer is crystallised by cooling of the extrudate, it is possible to directly orient the molecular chains, e.g., by drawing the forme~- thermoreversible ge;l. Using the~ soTvents accordi~g to the present invention in a great many cases renders solvent extraction with the aid of an extracting agent unnecessary. Thus, it was found that the formed thermoreversible gel may be drawn directly on exiting from the extruder, optionally after first being passed, under low tension or virtually tensionless, along a source of heat. A preferred embodiment consequently is found in a process according to said invention in which at least 50% of the solvent is removed from the extruded product by a means other than extraction.
The solvents to be employed according to the present invention have a~
melting point be}ow 3J3 K ~100C)~.lf the melting point is comparatively high, the solvent and polymer crystallisations will be ~ 30 subject to interference upon cooling. This brings about substantial deterioration of the mechanical properties of the fibres to be obtained. Accordingly, the melting point of an appropriate solvent according to the present invention will be less than 373 K
AMENDED SHEE~
21~3~3 (100C),more particularly less than 318 K (45C).The properties of the obtained fibres were found to have improved with the lowering of the solvent melting point.
Considered to be highly suitable are solvents containing at least one component from the group made up of:
PROCESS FOR THE PREPARATION OF POLYKETONE FIBRES
The invention relates to a process for the preparation of fibres of a linear polymer of alternating ethylene and carbon monoxide units, in which process the polymer is dissolved in an appropriate solvent having a boiling temperature above 443 K (170C), a melting tem-perature below 373 K (100C), and a polymer dissolving temperature above 443 K (170C), the polymer solution, after being moulded, is converted to a thermoreversible gel by cooling, and the solvent is removed from the obtained product.
Such a process is known from International Patent Application WO
92/10524, which describes intermixing an ethylene/carbon monoxide copolymer with a second component to produce polymer compositions suitable for making gel-based articles, amongst others components capable of dissolving the polymer and spinning it into fibres, and components which cause the polymer to swell and are not considered suitable~for fibre pr~duction.
According to this very general descripti~n,~it fs possible ta prepare a thread-like, thermoreversible gel using the aforementioned polymer dissolving means, but none of said substances has proved easily suited to practical use. For instance, many of the solvents and swelling agents mentioned have a low boiling point, which results in slow crystallisation of the polymer in the solution on cooling. Also described are solvents which in practice were found to dissolve the polyketone less readily if higher concentrations are employed. Not a single practical example of good quality fibres being prepared from such solvents is provided. The only example in which a highly concentrated solutiQn is prepared uses ~benzoic acid as a solvent, but this solvent was found to be unsuitable for the preparation of good quality fibres because of interference between the solvent and polymer crystallisation as the solution cools, which has an adverse effect on the mechanical properties of the products to be obtained. It was further found that benzoic acid breaks down the polyketone polymer.
~JIENIY~O S~EE~
- 215~S83 A process has now been found which is free of these drawbacks. This - process of the type mentioned in the opening paragraph provides a highly economical method of preparing polyketone fibres of favourable - mechanical properties, and is characterised in that a permanently orientable thermoreversible gel is formed.
Use is made in this process of a comparatively poor polymer solvent, with such a high polymer concentration in the solvent being selected as will give sufficient and homogeneous intermingling of the polymer's molecular chains. The polymer crystallises on cooling, without the solvent needing to have been removed. Thus, a thermoreversible gel of such properties is formed by cooling as will permit drawing of the gel without removal of the solvent. The drawing process serves to permanently orient the polymer's molecular chains.
According to the novel process, it is possible to obtain at a high rate and in large quantities a fibre having favourable mechanical pru~,l-ies an~ fro~ w~ch the- sol:vent - c~n be rem~ued~ compar~tively easily.
In general, so much polymer is dissolved in order to prepare a permanently orientable thermoreversible gel that the product of the polymer concentration and [~]o~S is higher than 0,35 (dl/g)o~S. [~] in this process was measured in an m-cresol solution at 298 K (25C).
Although the fact that W0 92/10524 describes, in a very general way, the possibility of preparing highly concentrated solutions, the statement that a minute portion of the mentioned means forms solvents for the polymer from which permanently orientable fibres can be made, has not b~een substantiated, nor has been- indicated~when ~and/or how these can be obtained.
The process now found comprises the following components:
- polyketone polymer of the proper intrinsic viscosity, a mediocre or even poor solvent in which the polymer takes up a comparatively small hydrodynamic volume, and A~AENDED SHE~T
21~35~3 a device for thoroughly intermixing the polymer and the solvent at a relatively high temperature and with forceful mechanical agitation.
Hydrodynamic volume is defined as the product of the intrinsic viscosity of the polyketone polymer in a particular solvent at the processing temperature and the average molecular weight.
According to the process found, these components are utilised such that:
a homogeneous solution is formed in such a concentration as will have overlapping of the molecular chains, which overlapping is preserved after cooling to below the crystallisation temperature of the solution, the homogeneous solution is extruded, and the resulting extrudate rapidly gels as it is cooled on account of the formation of crystalline nuclei, causing a thermoreversible gel to be formed which is drawable to a draw ratio ~A) of at least 6 and by being drawn to a draw ratio between 6 and 13 produces ~n ortented fib`-re with an initial modulus equal to or higher than 10/9-A-2,5 (N/tex).
Preferably, an oriented fibre with an initial modulus higher than 1O/9 A-1~75 (N/tex) is obtained. In a further preferred embodiment, the initial modulus is at least 1O/9 A-1 (N/tex), but will be less than 10/9-A+4 (N/tex). The optimal oriented fibre will have an initial modulus which at least fulfills the equation:
O~259+1~752.A-O~114.A2+O~OO625.A3-O~OOOO9.A4.
Thus, in the present invention, a permanently orientable thermoreversible gel is formed if said gel is drawable to a draw ratio of at least 6 and if from said gel an oriented fibre can be obtained which has an initial modulus in the range of 10/9~ 275 (N/tex) to 10/9-A+4 (N/tex) for a draw ratio between 6 and 13.
The process now found is so exceptional in particular because it is not subject to the drawbacks of traditional gel spinning and comes AMENDED SHEET
- 2153~83 very close to the meltspinning process which is so economically advantageous. This is advantageous in particular for some types of ethylene and carbon monoxide units containing polymers which are not melt processable on account of their degradation at the temperature required for polymer melt processing.
The solvents used are those which are generally considered to be so-called poor solvents for the polymer. The boiling point of these solvents is above 443 K (170C), more particularly above 453 K
(180C), and in a most preferred embodiment above 477 K (204C). These solvents will not dissolve the polymer in its entirety except with heating to a temperature above 443 K (170C),preferably to above 453 K
(180C), and most preferably to above 477 K (204C). In most cases, the temperature at which there is virtually complete polymer dissolution lies below the boiling point of the solvent, so that the dissolving process can easily be carried out under atmospheric pressure. In the case of a number of solvents, a suitable process for preparing a polymer solution lies in selecting a dissolving temperature equal to or higher than the boiling point of the solvent.
Such a process may be carried out with advantage when, e.g., benzyl alcohol is used as solvent. At temperatures which do not exceed the boiling temperature by more than 5 K (5C), operating under a pressure above 100 kPa will not be required in every case. At higher temperatures, however, this requirement will always be there.
The dissolving temperature of polyketone in a particular solvent is defined as the temperature at which virtually complete dissolution of 5-10 wt.% of polyketone having an intrinsic viscosity of about 7 is observed in that particular solvent.
Selecting the polymer concentration such that the product of the polymer concentration and [~]o.S is higher than 0,35 (dl/g)o~S will give a solution in which the molecular chains of the polymer are sufficiently intermingled to form the desired thermoreversible gel upon crystallisation. [~] is measured in an m-cresol solution at a AMENDED SHEET
- 21~3!;8~
temperature of 298 K (25C).In this formula the polymer concentration is expressed as the fraction by weight of polymer in the solution. A
very satisfactory process consists in so selecting the polymer concentration that the solution's crystallisation temperature lies between 398 K (125C) and the boiling point of the solvent.
It has been found that while using a solvent which satisfies the above-mentioned characteristics at lower polymer concentrations will allow a homogeneous solution to be obtained, such a low-concentration solution of a solvent according to the invention will lead to phase separation upon cooling. In the case of such cooled solutions it is no longer possible to speak of a permanently orientable thermoreversible gel. The products obtained from such low-concentration solutions have mechanical properties which are inadequate for use. This was earlier described in EP 456 306.
In the preparation of a solution to form a thermoreversible gel the cohesion between the chains, and thus the gelling, may be enhanced by so selecting the cancr-ntratiQn of a polymer having ,a given intrinsic viscosity that~the product of the~po,lymer cQncentrati~ and [~o~S is higher than 0,4 (dl/g)o~s. More favourable results still are attained if the product of the polymer concentration and [~]o~ is higher than 0,5 (dl/g)o. 5 .
Not only are the properties of the end products manufactured from such solutions enhanced, using high polymer concentrations also has advantages as regards the amount of polymer processed per unit of time and the rate at which the solvent can be removed from the product.
In the aforesaid equation [~] represents the intrinsic viscosity of the palymer and is deter,mined as follo,ws: , [~] = lim ~pr-r = lim t - tn c~O c c~O to . C
so having the meaning of the ratio between the flow times t and to~
with to and t representing the flow time of the solvent and the AMENDED SHEET
2i535~ AFP 2330 R
polymer-containing solution, respectively, in a capillary viscometer at 298 K (25C). c in this equation has the meaning of the polymer con-centration in m-cresol, expressed in grams per deciliter.
The intrinsic viscosity of the polyketone used generally is in the range of 0,5 to 10 dl/g but may be higher. Polyketone highly suited to be used in the process now found has an intrinsic viscosity in the range of 1,2 - 8 dl/g, in particular in the range of 1,2 - 4,5 dl/g.
Very suitable polyketone for use in the present invention has an intrinsic viscosity in the range of 1,2 - 2,5 dl/g. The relation between the estimated molecular weight (Mw) (in grams per mole) and the intrinsic viscosity as utilised here can be established with the aid of the following formula:
[~] = 1,0 x 10-4 x MW0,85 The pnlyketone~ poly~me-r is prim~riily~ composed of alternating carbon monoxide~and~ethyle~e units according to the formula:
[- CH2 - CH2 - C - ]
In addition to carbon monoxide and ethylene units, this polymer may contain a small amount of other units, for instance propylene groups.
Also, other substances may be admixed, e.g., to improve the thermal and/or oxidative properties and/or other polymer and/or fibre properties. For the preparation of polyketone polymers reference is made to the following European Patent Specifications: 121 965;
222 454~; 227 135; 228 733~ 229~408~;~ 2~35 865; 235 86~; 239 145;~
245 893; 246 674; 246 683i 248 483; 253 416; 254 343; 257 663;
259 914; 262 745; 263 564; 264 159; 272 728; and 277 695.
It is not possible to prepare the desired thermoreversible gel which can be permanently oriented without the solvent having to be removed ENl~E~
- 21~3~83 if solvents are used of which the polymer dissolving temperature is lower than that mentioned in the claims. Using such solvents will result in thermoreversible gels which are far closer in character to gels prepared with a satisfactory solvent, which means, int. al., that the solvent cannot be removed from the obtained products without extraction, and the polymer concentration in the solutions obtained cannot be as high as presently found.
The process now found has the significant advantage of the polymer being crystallised by cooling under normal spinning operation conditions, such as normal cooling speed, while the processes hitherto known always required that an extracting agent be employed to carry out the desired polymer crystallisation. In a highly preferred embodiment of the present invention, the polymer is crystallised by cooling to room temperature under normal spinning conditions. Since the polymer is crystallised by cooling of the extrudate, it is possible to directly orient the molecular chains, e.g., by drawing the forme~- thermoreversible ge;l. Using the~ soTvents accordi~g to the present invention in a great many cases renders solvent extraction with the aid of an extracting agent unnecessary. Thus, it was found that the formed thermoreversible gel may be drawn directly on exiting from the extruder, optionally after first being passed, under low tension or virtually tensionless, along a source of heat. A preferred embodiment consequently is found in a process according to said invention in which at least 50% of the solvent is removed from the extruded product by a means other than extraction.
The solvents to be employed according to the present invention have a~
melting point be}ow 3J3 K ~100C)~.lf the melting point is comparatively high, the solvent and polymer crystallisations will be ~ 30 subject to interference upon cooling. This brings about substantial deterioration of the mechanical properties of the fibres to be obtained. Accordingly, the melting point of an appropriate solvent according to the present invention will be less than 373 K
AMENDED SHEE~
21~3~3 (100C),more particularly less than 318 K (45C).The properties of the obtained fibres were found to have improved with the lowering of the solvent melting point.
Considered to be highly suitable are solvents containing at least one component from the group made up of:
2-methoxy phenol, 2-hydroxypropionphenone, diethylene glycol, dipropylene glycol, triethylene glycol, anhydroerythritol, thiodiethylene glycol, 5-methyl-2-pyrrolidinone, N-methyl-2-oxazolidinone, N-formyl piperidine, dimethyl phthalate, benzyl alcohol, y-butyrolactone, ~-caprolactam, dimethyl sulphoxide, ethylene carbonate, and propylene carbonate. These solvents are held to be suitable in particular because they have no or only very low toxicity and do not cause polymer degradation, and because the temperature at which the polymer dissolves is in a favourable range.
Particularly significant in this connection are those solvents which conta~in at least one component from the group made up of:
ethylcne ~ca.rbonate,- propylene carbonate~ be~zyl alcohoT, y-butyrolactone, ~-caprolactam, dimethyl phthalate, and dipropylene glycol. Notably ethylene carbonate, propylene carbonate, and benzyl alcohol, in combination or not with one or more other substances, were found to be highly suitable solvents. Thus, the solvents to be used may be made up of one or more of the aforementioned components, but also contain other components. The important thing is that the mixture continues to satisfy the criteria for the solvent as given in the claims.
In actual practice, a number of solvents proved to be less suitable for use~. The criteria which are considered relevant with regard to the practical use of such materials are listed below.
Thus, solvents which are deemed suitable should be of low toxicity and/or cause little or no irritation, so that their handling does not call for any additional measures. For that reason, solvents containing a substantial amount of phenol are not suitable for use according to AMENDED SHEE~
the present invention.
Also, for economic reasons, the solvents should be comparatively inexpensive. In addition, they should be chemically inert with regard to the polymer. For instance, it was found that, at elevated temperature, benzoic acid and aniline break down the polyketone polymer. Furthermore, solutions prepared with the aid of the solvent will have to be reproducible in order to facilitate continuous spinning operations.
The solution according to the present process may be prepared in the aforementioned concentration by intimate mixing of the solvent and the polymer with increasing temperature, followed by extrusion moulding of the solution. Thus, the preparation of the solution may take the form of feeding the polymer and the solvent to a kneading apparatus, and then using a spinning pump to press the mixture through an extrusion plate at elevated temperature. The temperature at which the solution is extruded preferably is a~Qve 453 K (180C),but lower than the polymer degra~ation temperature. The polymer and the soTvent may be mixed either in the kneading apparatus itself or intermixed in advance, with the resulting mixture, the suspension, subsequently being passed to the kneading apparatus. The solution is obtained by heating the mixture to or above the temperature at which the polymer dissolves. This temperature should be lower than the temperature at which there is substantial thermal decomposition of the polymer. A
process suited to practical use is found by selecting the temperature lower than the solvent's boiling point at the prevailing operating pressure in the kneading apparatus, and higher than the polymer's dissolving point in the solvent at this operating pressure. More particularly, a temperature in the range of about 453 to 513 K (18Q to 240C) is employed, depending on the solvent used.
According to one process very suited to practical use for preparing solutions containing polymer concentrations of over 70 wt.%, up to even 95 wt.~, based on the weight of the solution, the polymer and the ~ E~ SH~ET
- ~535~3 solvent are fed to a kneading apparatus equipped with one or more screws in order to subject the mixture to mixing and kneading at high mechanical shear rates. More particularly, the kneading apparatus used is a twin-screw extruder, although also a single-screw extruder or another high shear kneader can very well be applied. In particular, the use of a twin-screw extruder is consider advantageous, since in such a mixing means the mixture is mixed and heated as well as transported. The construction of the screw is such as to give a short stay and low dispersion during that stay, which serves to counter polymer degradation and will benefit the constant quality of the solution to be obtained. In the kneading extruder the polymer's stay and temperature can be set in relation to the concentration and the solvent employed. For instance, it has been found that a stay in the range of about 1 to 5 minutes was very suitable for heating the mixture sufficiently for both dissolving and extruding purposes. Using such a twin-screw extruder makes it possible to obtain solutions with a very hi~h polymer concen~ration. In addition, it is possible to operate under a pres,sure tn excess of`l~0 kPa if s~ desired, withaut this giving any problems.
According to a very favourable method, the kneading extruder is connected to a spinning unit, and the resulting solution is fed directly to the spinning pump. After extrusion the solvent can be removed by evaporation, e.g., by passing the solution through a heated tube, along a hotplate, or by a flow of hot air.
The polymer will be crystallised by cooling. Cooling may take the form of air cooling, water cooling, water vapour cooling, passing over cooled rollers or through a bath containing a cooling liquid, or of a combtnation of cooling techniques.
~ 30 Alternatively, the extruded product may be drawn following its extrusion at elevated temperature or not, with the solvent being removed from the product either by the drawing process itself or by the heat applied during the drawing.
A~AENDED SHE~r 21~35~
Figure 1 shows the process according to a preferred embodiment of the present invention, which does without an extracting agent to remove the solvent. At (1) the polymer is charged and at (2) the solvent, whereupon both are heated in the twin-screw extruder (3) to the desired temperature, which will be above 443 K (170C). (4) represents the spinning pump and (5) the filter through which the solution is pressed. The solution is pressed through the spinneret, referred to here as the extrusion plate (6), and the obtained extrudates are guided through a heated tube (7), after which, via a separator roll (8) and with the aid of a winder (9), the resulting fibres are wound onto a bobbin.
The mechanical properties of the fibres are measured.on filaments that have been conditioned at 21C and 65% relative humidity for at least 16 hours. The breaking tenacity (BT), elongation at break (EAB), initial modulus (~M), and final modulus (FM) are obtained by breaking a single~: filament.in ~ tensil.e te~ster. The gauge.length for the filaments is 100 mm. The samples are elon~ated at a constant extension rate of 10 mm/min.
The breaking tenacity and the elongation at break are obtained from the stress-strain curve as defined in ASTM D 2256-88. The initial and final moduli are obtained from the first derivative of the stress-strain curve (the modulus-strain curve) as the maximum moduli for a strain smaller than 0.2% and a strain larger than 2%, respectively.
The linear density of the filaments (LD, expressed in dtex) is calculated on the basis of the functional resonance frequency as defined in ASTM D 1577-66, or by weighing of the filaments.
EXAMP~E I
Several substances were tested for their serviceability as solvents for the process according to the present invention. To this end polyketone polymer having an intrinsic viscosity as indicated below was added to a quantity of the substance mentioned below and slowly AMENDED SHEET
2 15 ~ ~ 8 3 AFP 2330 R
heated in an atmosphere of nitrogen. After complete dissolving of the polymer or the attaining of a temperature of 523 K (250C), the obtained substance was left to slowly cool.
The following substances were employed:
benzoic acid: boiling point 522 K (249C), melting temperature 396 K
(123C) benzyl alcohol: boiling point 483 K (210C), melting temperature 258 K
(-15C) ~-caprolactam: boiling point 543 K (270C), melting temperature 343 K
(70C~
N-methyl-2-pyrrolidone: boiling point 475 K (202C), melting temperature 249 K (-24C).
I a (Comparative example) Prepared was a 2%-solution of polyketone ([~] 9,8) and benzoic acid by heating in an atmosphere of nitrogen. At 396 K (123C) the benzoic acid meltedi. At 468 K (195C) the~ polymer had dissolved completely, the solutton bein~ faintly yel-low in col`our. On bef~g caaled, the solution first became cloudy `and then finally crystallised at a temperature of 433 K (160C), with phase separation of the benzoic acid and the polymer being observed.
I b Prepared was a 4%-solution of polyketone ([~] 9,8) and benzyl alcohol.
The benzyl alcohol wets the polymer straightaway. At 443 K (170C) the polymer had dissolved completely, and a clear solution was obtained.
On preparing a 30%-solution of polyketone ([~] 1,3) and benzyl alcohol the polymer was found to have dissolved completely at a temperature of 472 K (199C). The polymer crystallised at 418 K (145C).
~ 30 I c Prepared was a 4%-solution of polyketone ([~] 9,8) and ~-caprolactam.
The caprolactam melted at 353 K (80C) and at 413 K (140C) caused the polymer to swell. At 503 K (230C) the polymer had dissolved A~ENDED SHEEt ~ 1 ~ 3 5 8 ~ AFP 2330 R
completely, and a clear solution was obtained. On being cooled, the solution crystallised at a temperature of 438 K (165C).
I d (Comparative example) Prepared were two 30%-solutions of polyketone ([~] 1,3) from the same production batch and N-methyl-2-pyrrolidone.
In a manner known in itself thermal analyses were carried out by repeatedly heating and cooling the contents of the closed vessel. The identically prepared solutions were found to have different temperatures for complete polymer dissolution. Heating the solutions a second time produced lower temperatures, which is indicative of polymer degradation. The temperatures found for the first and second heatings were 491 K (218C) and 483 K (210C) and 476 K (203C) and 473 K (200C), respectively. Repeating this test with polyketone of a different intrinsic viscosity ([~]= 8,4) showed a similar range at other temperatures. These results are so far apart that the preparation of polymer solutions of N-methyl-2-pyrrolidone and ; polyketone of sufficiently reproducible ~ua~ity does not appear~ very feasible.
These examples already show that benzoic acid is not a suitable solvent for the preparation of fibres according to the present process. The use of N-methyl-2-pyrrolidone is likewise attended with drawbacks which render it unsuitable for use in actual practice. By contrast, very satisfactory solutions highly suited to practical use can be prepared using the solvents mentioned in Examples I b and I c.
EXAMPLE II
Solutions were prepared from polyketone having a molecular weight and ~ 30 an intrinsic viscosity [~] as listed in the table. The polyketone was composed of carbon monoxide and ethylene units and contained neither stabilisers nor any other additives.
The polymer, in the powdered form, was charged to a twin-screw AMENDED SHEET
extruder, where it was slowly heated to 353 K (80C). To the polymer of this temperature (353 K [80C]) the solvent was added, after which the mixture was dissolved by the kneading action of the extruder and - the appropriate temperature settings to above the temperature at which the polymer dissolves. This temperature was 493 K (220C) for the propylene carbonate solutions, 458 K (185C) for benzyl alcohol, and 453 K (180C) for the propylene carbonate/resorcinol mixtures. At the extruder's head there was a spinneret plate with two round orifices of 4 mm in diameter. The moulded strands were immediately cooled over three water-cooled rollers and then chopped up into pellets of about 3 mm.
Rapid cooling caused the solvent to be retained in the solution, as a result of which solid solutions in the shape of pel]ets were obtained.
In this manner the following solutions were prepared:
TABLE I
solvent set c~ncen- Mw ~ [~] c.~o,~
tration [kg/kmole] rdl/g~ ~dl/g]~ 5 1 prop. carbonate 0,25 561 000 7,7 0,6937 2 prop. carbonate 0,17 561 000 7,7 0,4717 3 prop. carbonate 0,33 `485 000 6,8 0,8605 4 resorcinol/prop.
carbonate 35/65 0,25 468 000 6,6 0,6422 -"- 0,275 561 000 7,7 0,763 6 -"- 0,30 561 000 7,7 0,8324 7 prop. carbonate 0, 25 561 000 7,7 0,6937 8 benzyl alcohol 0,20 410 000 5,9 0,4858 9 benzyl alcohol/prop.
carbonate 75/25 0,18 561 000 7,7 0,4994 EXAMPLE I I I
The pellets made from solutions 1 and 8 i n Example II were fed to a 30 si ngle-screw extruder with at its mouth a spinneret provided with a spinneret plate having 26 round orifices, each of 250 ~m in diameter.
The solutions were extruded and the formed extrudates crystallised by being cooled in air. The obtained solid filaments were washed out with P~ANDED SHEET
2~535~3 water and subsequently drawn over a matt chromed pin heated at 509 K
(236C) and two or three 34 cm long heated plates. The draw ratios of the spun fibres, the temperatures of the heated plates, and the mechanical properties found for the fibres are given in Tables II and III .
TABLE II
no. draw plate LD BT EAB IM FM
sol ratio temp. [K(C)] [dtex] [mN/tex] [%] [N/tex] [N/tex]
1 13,0 518/522(245/249) 15,6 950 5,3 16 22 1 13,0 518/522(245/249) 16,8 1000 5,9 15 22 1 13,0 518/522(245/249) 15,3 1100 5,6 18 24 1 11,1 518/522'245/249) 17,7 1280 7,7 14 20 1 11,1 518/522:245l249) 18,4 1210 7,2 .14 21 1 11,1 518/522;245l249) 15,6 1320 7,3 15 22 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
The measured concentration of solution 1 was 0,34. The product of the c~ncentr~tion.~a~ ~}~Q~`S thu~ was~ 0:~.9.4~5~dl/g~.,.S
TABLE III
no. draw plate LD BT EAB IM FM
sol ratio temp[K(C)] [dtex] [mN/tex] [%] [N/tex] [N/tex]
8 10,2 519 22,6 870 7,6 9,6 14 8 11,2 519/526 17,9 880 6,4 12 17 (246/253) 8 13,0 519/529 14,8 1230 5,6 18 26 (246/256) 8 13,0 519/529 18,7 980 5,7 15 21 (246/256) 8 14,6 519/526/528 19,0 1000 4,9 17 24 (2461253/255) 8 14,6 519152fil528 15,7 960 5,1: 16 22 (246l253/255) LD: linear density, BT: breaking tenacity, EAB: elongation at break -~
- 30 IM: initial modulus, FM: final modulus.
The measured concentration of solution 8 was 0,29. The product of the concentration and [~]o~S was 0,7 (dl/g)o~S.
A~ENDED SHEE~
- 2153~83 EXAMPLE IV
The method as described in Example II was used to prepare fibres from Example II 's solution no. 9, except that this time the obtained filaments were not drawn over hotplates, but in a single step in a hot oven at a temperature of 498 K (225C). The properties of the resulting products are listed in Table IV.
TABLE IV
draw LD BT EAB IM FM
ratio[dtex] [mN/tex] [%] [N/tex] [N/tex]
14,4 15,3 760 5,6 12 16 14,4 15,3 680 4,6 13 17 9,3 29,6 550 5,6 10 11 18,3 12,5 750 4,5 16 19 13,3 15,2 770 5,3 14 17 13,3 15,4 710 4,5 15 18 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM- initia~ modu1us, F~^-final m~dulus.
EXAMPLE V
A solution of polyketone polymer and benzyl alcohol was prepared by charging powdered polyketone with an intrinsic viscosity of 2,93 and solvent to a twin-screw extruder. The temperature was 378 K (105C) in the first extruder zone and 453 K (180C) in the last one. The kneading action of the extruder and heating to 453 K (180C) caused the polymer to dissolve completely. The residence time of the polymer in the extruder was about 3 minutes. At the mouth of the extruder there was a spinneret with 10 orifices af 200 ym, through which the~
solution was passed. The temperature of the solution during the extrusion process was 458 K (185C), the pressure applied was 7200 ~ 30 kPa. The moulded extrudates were passed through a heated tube (T =
498 K [225C]) and along a number of guide bars and wound onto a bobbin. The fibres from this bobbin were not drawn over hotplates, but in one or two steps in a heated oven. At the end of the drawing set-up A~ENDED SHEET
~ 1 5 3 5 8 ~ AFP 2330 R
there was a bobbin onto which the formed fibres were wound.
The measured polyketone concentration in the solution was 0,50. The product of the concentration and [~]. 5 was 0,86 (dl/g)~ 5 .
The drawing conditions and the mechanical properties of the resulting products are listed in Table V
S
TABLE V
draw oven LD~) BT~) EAB~) IM~) FMl) ratiotemp[K(C)][dtex] [mN/tex] [%] [N/tex] [N/tex]
2373 (100) 372,0 68 31 0,8 0,5 4373 (100) 171,0 283 9,5 3,1 3,5 4373 (100) 138 350 9,3 4,3 4,9 4498 (225) 95 440 10,3 4,7 6,1 6473 (200) 100 430 6,1 6,7 9,2 6498 (225) 91,6 530 6,68 7,4 9,7 6523 (250) 93,5 737 8,14 7,9 11,8 8,1313/498 (40/225) 46,9 631 5,83 10,1 13,6 8,1523 (250) 74 910 6,81 11,7 17,0 10313/523 (40/225) 32 970 6,1 13,0 20,0 LD: linear density, BT: breaking tenacity, EAB: elongat~on at break IM: initial modulus, FM: final modulus.
l): The averaged value for 10 measurements is given.
Example VI
A mixture of fine solid polyketone powder with an intrinsic viscosity of 1,35 and propylene carbonate was prepared at room temperature using a Brabender blender. The blend, having a total weight of approximately 15 grams, was homogenised for at least 15 minutes at a screw speed of - 100 rpm.
Three grams of the so obtained samples were compression moulded into -.films between two aluminium carriers of 25 cm x 35 cm. During compression at elevated temperature a polymer solution was formed.
- After the compression moulding procedure was completed, the filmsample, including the aluminium carriers, was removed from the hot AMENDEp SHEEt ~1~3583 AFP 2330 R
surface of the press and the package was subsequently cooled by being pressed with a cold copper plate on a metal base for at least 20 seconds.
The resulting film was cut up into strands with a size of 0,08-0,1 mm (thickness) x 2 mm (width) x 30 mm (length). Some of the strands were washed with acetone before being drawn. The conditions for the preparation of the strands are listed in Table VI. The strands were drawn in a single step in a hot oven. The drawing conditions and the properties of the resulting products are listed in Table VII.
TABLE VI
strandPOK preload LoadLoading Temperature strand no. conc. (10 s.) time washed [kN] [kN] [s] [K(C)]
1 0,71 20 20 90 493 (220) no 2 0,71 20 20 90 493 (220) no 3 0,71 2a 20 9~; 4g~ ~22QI~ yes 4 0,71 20 20 90 493 (Z20) no 0,83 30 30 90 513 (240) yes DED S~E~
TABLE VII
- strand draw oven drawing BT IM FM
no. ratio temp speed [K(C)] [mm/sec] [mN/tex] [N/tex] [N/tex]
1 6 498(225) 10 460 6,1 8,0 2 7 498(225) 5 440 6,4 8,6 3 6 508(235) 10 200 4,4 6,0 4 6 508(235) 10 380 5,0 8,0 6 508(235) 20 230 4,8 7,1 BT: breaking tenacity, IM: initial modulus, FM: final modulus.
The product of the concentration and [~]0,5 thus was 0,82 (dl/g)0~5 for the blend with a polyketone concentration of 0,71 and 0,96 (dl/g)0~5 for the blend with a polyketone concentration of 0,83.
It is also possible to use the blends for the preparation of fibres.
Extruding these blends at elevated temperature, e.g., 513 K (240C), through cappilaries of approximately 1000 ~m, will produce fibres which after drawi~ng at - e}evated temperatur;e ~isplay mechanical properties similar to or even better than those of the drawn strands~.
Solutions were prepared from polyketone having a molecular weight of 310 000 g/mole and an intrinsic viscosity [~] of 4,66 using dry propylene carbonate as solvent. Polymer was added in such a quantity as to give a percentage by weight of the polymer in the solution of 15. The product of the polymer concentration and [~]o~S accordingly was 0,32 (dl/g)o~s.
The pGlyketone polymer was composed of carbon monoxide an-d ethylene units and contained neither stabilisers nor any other additives.
The solution was prepared by heating the solvent and the polymer in a stirred beaker under nitrogen to 493 K (220C). The time required for dissolution was 120 minutes. The formed solution was passed through six spinning orifices of a diameter of 300 ~m each in a spinning machine at 483 K (210C). 10 mm beneath the spinneret plate there was ~EN~ED SHEET
21~35~3 an extraction or coagulation bath filled with acetone of 250 K
(-23C), through which the moulded extrudates were passed. Next, free of solvent, the fibres were drawn by being passed over one or more hotplates under tension, and wound.
Measurement of the mechanical properties produced the following results, which are listed in Table A1.
draw plate LD BT EAB IM FM
ratio temp[K(C)] [dtex] [mN/tex] [~] [N/tex] [N/tex]
8 513 (215) 12,8 430 11,3 5 5 513 '215) 11,1 570 8,9 6 8 12 513 215) 8,7 730 7,2 9 13 14 513 215) 7,2 840 6,7 12 15 LD: linear dens ty, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
COMPARATIVE EXAM~LE Z
A solution was prepared of polyketone having a molecular weight of 640 000 g/mole and an intrinsic viscosity [~] of 8,62 using dry propylene carbonate as solvent. Polymer was added in such a quantity as to give a percentage by weight of the polymer in the solution of 8.
The product of the polymer concentration and [~]o~S accordingly was 0,08 x 2,93 = 0,23 (dl/g)o~s.
The solution was prepared by heating the solvent and the polymer to 493 K (220C) in a stirred closed dissolving vessel under nitrogen.
The time required for dissolution was 60 minutes. The formed solution was passed through a single spinning orifice of a diameter of 5Q0 ~m in a spinning machine at 483 K (210C). 10 mm beneath the spinneret - 30 plate there was an extraction or coagulation bath filled with acetone of 248 K (-25C), through which the formed extrudates were passed.
Next, free of solvent, the fibres were drawn by being passed over one or more hotplates under tension, and wound.
A ~ NDED SHEET
Measurement of the mechanical properties produced the following results, which are listed in Table A2.
draw plate LD BT EAB IM FM
ratio temp[K(C)][dtex] [mN/tex] [%] [N/tex] [N/tex]
8 473(200) 24,9 370 9,2 4 5 12 473/498(200/225)16,1 540 8,5 6 7 473/503(200/230) 9,9 770 7,2 10 13 18 473/503(200/230)12,5 610 7,8 8 10 473/503(200/230) 8,6 780 6,5 12 15 23 473/503(200/230) 8,6 880 6,7 12 16 26 473/508(200/235) 9,6 840 7,4 12 15 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
A~AEN~ED S~EET
Particularly significant in this connection are those solvents which conta~in at least one component from the group made up of:
ethylcne ~ca.rbonate,- propylene carbonate~ be~zyl alcohoT, y-butyrolactone, ~-caprolactam, dimethyl phthalate, and dipropylene glycol. Notably ethylene carbonate, propylene carbonate, and benzyl alcohol, in combination or not with one or more other substances, were found to be highly suitable solvents. Thus, the solvents to be used may be made up of one or more of the aforementioned components, but also contain other components. The important thing is that the mixture continues to satisfy the criteria for the solvent as given in the claims.
In actual practice, a number of solvents proved to be less suitable for use~. The criteria which are considered relevant with regard to the practical use of such materials are listed below.
Thus, solvents which are deemed suitable should be of low toxicity and/or cause little or no irritation, so that their handling does not call for any additional measures. For that reason, solvents containing a substantial amount of phenol are not suitable for use according to AMENDED SHEE~
the present invention.
Also, for economic reasons, the solvents should be comparatively inexpensive. In addition, they should be chemically inert with regard to the polymer. For instance, it was found that, at elevated temperature, benzoic acid and aniline break down the polyketone polymer. Furthermore, solutions prepared with the aid of the solvent will have to be reproducible in order to facilitate continuous spinning operations.
The solution according to the present process may be prepared in the aforementioned concentration by intimate mixing of the solvent and the polymer with increasing temperature, followed by extrusion moulding of the solution. Thus, the preparation of the solution may take the form of feeding the polymer and the solvent to a kneading apparatus, and then using a spinning pump to press the mixture through an extrusion plate at elevated temperature. The temperature at which the solution is extruded preferably is a~Qve 453 K (180C),but lower than the polymer degra~ation temperature. The polymer and the soTvent may be mixed either in the kneading apparatus itself or intermixed in advance, with the resulting mixture, the suspension, subsequently being passed to the kneading apparatus. The solution is obtained by heating the mixture to or above the temperature at which the polymer dissolves. This temperature should be lower than the temperature at which there is substantial thermal decomposition of the polymer. A
process suited to practical use is found by selecting the temperature lower than the solvent's boiling point at the prevailing operating pressure in the kneading apparatus, and higher than the polymer's dissolving point in the solvent at this operating pressure. More particularly, a temperature in the range of about 453 to 513 K (18Q to 240C) is employed, depending on the solvent used.
According to one process very suited to practical use for preparing solutions containing polymer concentrations of over 70 wt.%, up to even 95 wt.~, based on the weight of the solution, the polymer and the ~ E~ SH~ET
- ~535~3 solvent are fed to a kneading apparatus equipped with one or more screws in order to subject the mixture to mixing and kneading at high mechanical shear rates. More particularly, the kneading apparatus used is a twin-screw extruder, although also a single-screw extruder or another high shear kneader can very well be applied. In particular, the use of a twin-screw extruder is consider advantageous, since in such a mixing means the mixture is mixed and heated as well as transported. The construction of the screw is such as to give a short stay and low dispersion during that stay, which serves to counter polymer degradation and will benefit the constant quality of the solution to be obtained. In the kneading extruder the polymer's stay and temperature can be set in relation to the concentration and the solvent employed. For instance, it has been found that a stay in the range of about 1 to 5 minutes was very suitable for heating the mixture sufficiently for both dissolving and extruding purposes. Using such a twin-screw extruder makes it possible to obtain solutions with a very hi~h polymer concen~ration. In addition, it is possible to operate under a pres,sure tn excess of`l~0 kPa if s~ desired, withaut this giving any problems.
According to a very favourable method, the kneading extruder is connected to a spinning unit, and the resulting solution is fed directly to the spinning pump. After extrusion the solvent can be removed by evaporation, e.g., by passing the solution through a heated tube, along a hotplate, or by a flow of hot air.
The polymer will be crystallised by cooling. Cooling may take the form of air cooling, water cooling, water vapour cooling, passing over cooled rollers or through a bath containing a cooling liquid, or of a combtnation of cooling techniques.
~ 30 Alternatively, the extruded product may be drawn following its extrusion at elevated temperature or not, with the solvent being removed from the product either by the drawing process itself or by the heat applied during the drawing.
A~AENDED SHE~r 21~35~
Figure 1 shows the process according to a preferred embodiment of the present invention, which does without an extracting agent to remove the solvent. At (1) the polymer is charged and at (2) the solvent, whereupon both are heated in the twin-screw extruder (3) to the desired temperature, which will be above 443 K (170C). (4) represents the spinning pump and (5) the filter through which the solution is pressed. The solution is pressed through the spinneret, referred to here as the extrusion plate (6), and the obtained extrudates are guided through a heated tube (7), after which, via a separator roll (8) and with the aid of a winder (9), the resulting fibres are wound onto a bobbin.
The mechanical properties of the fibres are measured.on filaments that have been conditioned at 21C and 65% relative humidity for at least 16 hours. The breaking tenacity (BT), elongation at break (EAB), initial modulus (~M), and final modulus (FM) are obtained by breaking a single~: filament.in ~ tensil.e te~ster. The gauge.length for the filaments is 100 mm. The samples are elon~ated at a constant extension rate of 10 mm/min.
The breaking tenacity and the elongation at break are obtained from the stress-strain curve as defined in ASTM D 2256-88. The initial and final moduli are obtained from the first derivative of the stress-strain curve (the modulus-strain curve) as the maximum moduli for a strain smaller than 0.2% and a strain larger than 2%, respectively.
The linear density of the filaments (LD, expressed in dtex) is calculated on the basis of the functional resonance frequency as defined in ASTM D 1577-66, or by weighing of the filaments.
EXAMP~E I
Several substances were tested for their serviceability as solvents for the process according to the present invention. To this end polyketone polymer having an intrinsic viscosity as indicated below was added to a quantity of the substance mentioned below and slowly AMENDED SHEET
2 15 ~ ~ 8 3 AFP 2330 R
heated in an atmosphere of nitrogen. After complete dissolving of the polymer or the attaining of a temperature of 523 K (250C), the obtained substance was left to slowly cool.
The following substances were employed:
benzoic acid: boiling point 522 K (249C), melting temperature 396 K
(123C) benzyl alcohol: boiling point 483 K (210C), melting temperature 258 K
(-15C) ~-caprolactam: boiling point 543 K (270C), melting temperature 343 K
(70C~
N-methyl-2-pyrrolidone: boiling point 475 K (202C), melting temperature 249 K (-24C).
I a (Comparative example) Prepared was a 2%-solution of polyketone ([~] 9,8) and benzoic acid by heating in an atmosphere of nitrogen. At 396 K (123C) the benzoic acid meltedi. At 468 K (195C) the~ polymer had dissolved completely, the solutton bein~ faintly yel-low in col`our. On bef~g caaled, the solution first became cloudy `and then finally crystallised at a temperature of 433 K (160C), with phase separation of the benzoic acid and the polymer being observed.
I b Prepared was a 4%-solution of polyketone ([~] 9,8) and benzyl alcohol.
The benzyl alcohol wets the polymer straightaway. At 443 K (170C) the polymer had dissolved completely, and a clear solution was obtained.
On preparing a 30%-solution of polyketone ([~] 1,3) and benzyl alcohol the polymer was found to have dissolved completely at a temperature of 472 K (199C). The polymer crystallised at 418 K (145C).
~ 30 I c Prepared was a 4%-solution of polyketone ([~] 9,8) and ~-caprolactam.
The caprolactam melted at 353 K (80C) and at 413 K (140C) caused the polymer to swell. At 503 K (230C) the polymer had dissolved A~ENDED SHEEt ~ 1 ~ 3 5 8 ~ AFP 2330 R
completely, and a clear solution was obtained. On being cooled, the solution crystallised at a temperature of 438 K (165C).
I d (Comparative example) Prepared were two 30%-solutions of polyketone ([~] 1,3) from the same production batch and N-methyl-2-pyrrolidone.
In a manner known in itself thermal analyses were carried out by repeatedly heating and cooling the contents of the closed vessel. The identically prepared solutions were found to have different temperatures for complete polymer dissolution. Heating the solutions a second time produced lower temperatures, which is indicative of polymer degradation. The temperatures found for the first and second heatings were 491 K (218C) and 483 K (210C) and 476 K (203C) and 473 K (200C), respectively. Repeating this test with polyketone of a different intrinsic viscosity ([~]= 8,4) showed a similar range at other temperatures. These results are so far apart that the preparation of polymer solutions of N-methyl-2-pyrrolidone and ; polyketone of sufficiently reproducible ~ua~ity does not appear~ very feasible.
These examples already show that benzoic acid is not a suitable solvent for the preparation of fibres according to the present process. The use of N-methyl-2-pyrrolidone is likewise attended with drawbacks which render it unsuitable for use in actual practice. By contrast, very satisfactory solutions highly suited to practical use can be prepared using the solvents mentioned in Examples I b and I c.
EXAMPLE II
Solutions were prepared from polyketone having a molecular weight and ~ 30 an intrinsic viscosity [~] as listed in the table. The polyketone was composed of carbon monoxide and ethylene units and contained neither stabilisers nor any other additives.
The polymer, in the powdered form, was charged to a twin-screw AMENDED SHEET
extruder, where it was slowly heated to 353 K (80C). To the polymer of this temperature (353 K [80C]) the solvent was added, after which the mixture was dissolved by the kneading action of the extruder and - the appropriate temperature settings to above the temperature at which the polymer dissolves. This temperature was 493 K (220C) for the propylene carbonate solutions, 458 K (185C) for benzyl alcohol, and 453 K (180C) for the propylene carbonate/resorcinol mixtures. At the extruder's head there was a spinneret plate with two round orifices of 4 mm in diameter. The moulded strands were immediately cooled over three water-cooled rollers and then chopped up into pellets of about 3 mm.
Rapid cooling caused the solvent to be retained in the solution, as a result of which solid solutions in the shape of pel]ets were obtained.
In this manner the following solutions were prepared:
TABLE I
solvent set c~ncen- Mw ~ [~] c.~o,~
tration [kg/kmole] rdl/g~ ~dl/g]~ 5 1 prop. carbonate 0,25 561 000 7,7 0,6937 2 prop. carbonate 0,17 561 000 7,7 0,4717 3 prop. carbonate 0,33 `485 000 6,8 0,8605 4 resorcinol/prop.
carbonate 35/65 0,25 468 000 6,6 0,6422 -"- 0,275 561 000 7,7 0,763 6 -"- 0,30 561 000 7,7 0,8324 7 prop. carbonate 0, 25 561 000 7,7 0,6937 8 benzyl alcohol 0,20 410 000 5,9 0,4858 9 benzyl alcohol/prop.
carbonate 75/25 0,18 561 000 7,7 0,4994 EXAMPLE I I I
The pellets made from solutions 1 and 8 i n Example II were fed to a 30 si ngle-screw extruder with at its mouth a spinneret provided with a spinneret plate having 26 round orifices, each of 250 ~m in diameter.
The solutions were extruded and the formed extrudates crystallised by being cooled in air. The obtained solid filaments were washed out with P~ANDED SHEET
2~535~3 water and subsequently drawn over a matt chromed pin heated at 509 K
(236C) and two or three 34 cm long heated plates. The draw ratios of the spun fibres, the temperatures of the heated plates, and the mechanical properties found for the fibres are given in Tables II and III .
TABLE II
no. draw plate LD BT EAB IM FM
sol ratio temp. [K(C)] [dtex] [mN/tex] [%] [N/tex] [N/tex]
1 13,0 518/522(245/249) 15,6 950 5,3 16 22 1 13,0 518/522(245/249) 16,8 1000 5,9 15 22 1 13,0 518/522(245/249) 15,3 1100 5,6 18 24 1 11,1 518/522'245/249) 17,7 1280 7,7 14 20 1 11,1 518/522:245l249) 18,4 1210 7,2 .14 21 1 11,1 518/522;245l249) 15,6 1320 7,3 15 22 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
The measured concentration of solution 1 was 0,34. The product of the c~ncentr~tion.~a~ ~}~Q~`S thu~ was~ 0:~.9.4~5~dl/g~.,.S
TABLE III
no. draw plate LD BT EAB IM FM
sol ratio temp[K(C)] [dtex] [mN/tex] [%] [N/tex] [N/tex]
8 10,2 519 22,6 870 7,6 9,6 14 8 11,2 519/526 17,9 880 6,4 12 17 (246/253) 8 13,0 519/529 14,8 1230 5,6 18 26 (246/256) 8 13,0 519/529 18,7 980 5,7 15 21 (246/256) 8 14,6 519/526/528 19,0 1000 4,9 17 24 (2461253/255) 8 14,6 519152fil528 15,7 960 5,1: 16 22 (246l253/255) LD: linear density, BT: breaking tenacity, EAB: elongation at break -~
- 30 IM: initial modulus, FM: final modulus.
The measured concentration of solution 8 was 0,29. The product of the concentration and [~]o~S was 0,7 (dl/g)o~S.
A~ENDED SHEE~
- 2153~83 EXAMPLE IV
The method as described in Example II was used to prepare fibres from Example II 's solution no. 9, except that this time the obtained filaments were not drawn over hotplates, but in a single step in a hot oven at a temperature of 498 K (225C). The properties of the resulting products are listed in Table IV.
TABLE IV
draw LD BT EAB IM FM
ratio[dtex] [mN/tex] [%] [N/tex] [N/tex]
14,4 15,3 760 5,6 12 16 14,4 15,3 680 4,6 13 17 9,3 29,6 550 5,6 10 11 18,3 12,5 750 4,5 16 19 13,3 15,2 770 5,3 14 17 13,3 15,4 710 4,5 15 18 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM- initia~ modu1us, F~^-final m~dulus.
EXAMPLE V
A solution of polyketone polymer and benzyl alcohol was prepared by charging powdered polyketone with an intrinsic viscosity of 2,93 and solvent to a twin-screw extruder. The temperature was 378 K (105C) in the first extruder zone and 453 K (180C) in the last one. The kneading action of the extruder and heating to 453 K (180C) caused the polymer to dissolve completely. The residence time of the polymer in the extruder was about 3 minutes. At the mouth of the extruder there was a spinneret with 10 orifices af 200 ym, through which the~
solution was passed. The temperature of the solution during the extrusion process was 458 K (185C), the pressure applied was 7200 ~ 30 kPa. The moulded extrudates were passed through a heated tube (T =
498 K [225C]) and along a number of guide bars and wound onto a bobbin. The fibres from this bobbin were not drawn over hotplates, but in one or two steps in a heated oven. At the end of the drawing set-up A~ENDED SHEET
~ 1 5 3 5 8 ~ AFP 2330 R
there was a bobbin onto which the formed fibres were wound.
The measured polyketone concentration in the solution was 0,50. The product of the concentration and [~]. 5 was 0,86 (dl/g)~ 5 .
The drawing conditions and the mechanical properties of the resulting products are listed in Table V
S
TABLE V
draw oven LD~) BT~) EAB~) IM~) FMl) ratiotemp[K(C)][dtex] [mN/tex] [%] [N/tex] [N/tex]
2373 (100) 372,0 68 31 0,8 0,5 4373 (100) 171,0 283 9,5 3,1 3,5 4373 (100) 138 350 9,3 4,3 4,9 4498 (225) 95 440 10,3 4,7 6,1 6473 (200) 100 430 6,1 6,7 9,2 6498 (225) 91,6 530 6,68 7,4 9,7 6523 (250) 93,5 737 8,14 7,9 11,8 8,1313/498 (40/225) 46,9 631 5,83 10,1 13,6 8,1523 (250) 74 910 6,81 11,7 17,0 10313/523 (40/225) 32 970 6,1 13,0 20,0 LD: linear density, BT: breaking tenacity, EAB: elongat~on at break IM: initial modulus, FM: final modulus.
l): The averaged value for 10 measurements is given.
Example VI
A mixture of fine solid polyketone powder with an intrinsic viscosity of 1,35 and propylene carbonate was prepared at room temperature using a Brabender blender. The blend, having a total weight of approximately 15 grams, was homogenised for at least 15 minutes at a screw speed of - 100 rpm.
Three grams of the so obtained samples were compression moulded into -.films between two aluminium carriers of 25 cm x 35 cm. During compression at elevated temperature a polymer solution was formed.
- After the compression moulding procedure was completed, the filmsample, including the aluminium carriers, was removed from the hot AMENDEp SHEEt ~1~3583 AFP 2330 R
surface of the press and the package was subsequently cooled by being pressed with a cold copper plate on a metal base for at least 20 seconds.
The resulting film was cut up into strands with a size of 0,08-0,1 mm (thickness) x 2 mm (width) x 30 mm (length). Some of the strands were washed with acetone before being drawn. The conditions for the preparation of the strands are listed in Table VI. The strands were drawn in a single step in a hot oven. The drawing conditions and the properties of the resulting products are listed in Table VII.
TABLE VI
strandPOK preload LoadLoading Temperature strand no. conc. (10 s.) time washed [kN] [kN] [s] [K(C)]
1 0,71 20 20 90 493 (220) no 2 0,71 20 20 90 493 (220) no 3 0,71 2a 20 9~; 4g~ ~22QI~ yes 4 0,71 20 20 90 493 (Z20) no 0,83 30 30 90 513 (240) yes DED S~E~
TABLE VII
- strand draw oven drawing BT IM FM
no. ratio temp speed [K(C)] [mm/sec] [mN/tex] [N/tex] [N/tex]
1 6 498(225) 10 460 6,1 8,0 2 7 498(225) 5 440 6,4 8,6 3 6 508(235) 10 200 4,4 6,0 4 6 508(235) 10 380 5,0 8,0 6 508(235) 20 230 4,8 7,1 BT: breaking tenacity, IM: initial modulus, FM: final modulus.
The product of the concentration and [~]0,5 thus was 0,82 (dl/g)0~5 for the blend with a polyketone concentration of 0,71 and 0,96 (dl/g)0~5 for the blend with a polyketone concentration of 0,83.
It is also possible to use the blends for the preparation of fibres.
Extruding these blends at elevated temperature, e.g., 513 K (240C), through cappilaries of approximately 1000 ~m, will produce fibres which after drawi~ng at - e}evated temperatur;e ~isplay mechanical properties similar to or even better than those of the drawn strands~.
Solutions were prepared from polyketone having a molecular weight of 310 000 g/mole and an intrinsic viscosity [~] of 4,66 using dry propylene carbonate as solvent. Polymer was added in such a quantity as to give a percentage by weight of the polymer in the solution of 15. The product of the polymer concentration and [~]o~S accordingly was 0,32 (dl/g)o~s.
The pGlyketone polymer was composed of carbon monoxide an-d ethylene units and contained neither stabilisers nor any other additives.
The solution was prepared by heating the solvent and the polymer in a stirred beaker under nitrogen to 493 K (220C). The time required for dissolution was 120 minutes. The formed solution was passed through six spinning orifices of a diameter of 300 ~m each in a spinning machine at 483 K (210C). 10 mm beneath the spinneret plate there was ~EN~ED SHEET
21~35~3 an extraction or coagulation bath filled with acetone of 250 K
(-23C), through which the moulded extrudates were passed. Next, free of solvent, the fibres were drawn by being passed over one or more hotplates under tension, and wound.
Measurement of the mechanical properties produced the following results, which are listed in Table A1.
draw plate LD BT EAB IM FM
ratio temp[K(C)] [dtex] [mN/tex] [~] [N/tex] [N/tex]
8 513 (215) 12,8 430 11,3 5 5 513 '215) 11,1 570 8,9 6 8 12 513 215) 8,7 730 7,2 9 13 14 513 215) 7,2 840 6,7 12 15 LD: linear dens ty, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
COMPARATIVE EXAM~LE Z
A solution was prepared of polyketone having a molecular weight of 640 000 g/mole and an intrinsic viscosity [~] of 8,62 using dry propylene carbonate as solvent. Polymer was added in such a quantity as to give a percentage by weight of the polymer in the solution of 8.
The product of the polymer concentration and [~]o~S accordingly was 0,08 x 2,93 = 0,23 (dl/g)o~s.
The solution was prepared by heating the solvent and the polymer to 493 K (220C) in a stirred closed dissolving vessel under nitrogen.
The time required for dissolution was 60 minutes. The formed solution was passed through a single spinning orifice of a diameter of 5Q0 ~m in a spinning machine at 483 K (210C). 10 mm beneath the spinneret - 30 plate there was an extraction or coagulation bath filled with acetone of 248 K (-25C), through which the formed extrudates were passed.
Next, free of solvent, the fibres were drawn by being passed over one or more hotplates under tension, and wound.
A ~ NDED SHEET
Measurement of the mechanical properties produced the following results, which are listed in Table A2.
draw plate LD BT EAB IM FM
ratio temp[K(C)][dtex] [mN/tex] [%] [N/tex] [N/tex]
8 473(200) 24,9 370 9,2 4 5 12 473/498(200/225)16,1 540 8,5 6 7 473/503(200/230) 9,9 770 7,2 10 13 18 473/503(200/230)12,5 610 7,8 8 10 473/503(200/230) 8,6 780 6,5 12 15 23 473/503(200/230) 8,6 880 6,7 12 16 26 473/508(200/235) 9,6 840 7,4 12 15 LD: linear density, BT: breaking tenacity, EAB: elongation at break IM: initial modulus, FM: final modulus.
A~AEN~ED S~EET
Claims (12)
1. A process for the preparation of a fibre of a linear polymer composed of alternating ethylene and carbon monoxide units, in which process the polymer is dissolved in an appropriate solvent having a boiling temperature above 443 K (170°C), a melting temperature below 373 K (100°C), and a polymer dissolving temperature above 443 K (170°C), with the dissolving temperature in a particular solvent being defined as the temperature at which virtually complete dissolution of 5-10wt.% of polyketone having an intrinsic viscosity of about 7 is observed in that particular solvent, and the polymer solution after being moulded is converted to a thermoreversible gel by cooling, and the solvent is removed from the obtained product, characterised in that after the moulding a permanently orientable thermoreversible gel is formed.
2. A process according to claim 1, characterised in that so much polymer is dissolved that the product of the polymer concentration and [?]0,5, with the polymer concentration being expressed as the fraction by weigth of polymer in the solution and [?] being measured in an m-cresol solution at 298 K (25°C), is higher than 0,35 (dl/g)0,5.
3. A process according to claim 2, characterised in that the product of the polymer concentration and [?]0,5 is higher than 0,4 (dl/g)0,5.
4. A process according to claim 3, characterised in that so much polymer is dissolved that the product of the polymer concentration and [?]0,5 is higher than 0,5 (dl/g)0,5.
5. A process according to any one of the preceding claims, characterised in that the solvent contains at least one component from the group made up of:
2-methoxy phenol, 2-hydroxypropionphenone, diethylene glycol, benzyl alcohol, dipropylene glycol, triethylene glycol, anhydroerythritol, thiodiethylene glycol, 5-methyl-2-pyrrolidinone, N-methyl-2-oxazolidinone, N-formyl piperidine, dimethyl phthalate, .gamma.-butyrolactone, dimethyl sulphoxide, ethylene carbonate, propylene carbonate, and .epsilon.-caprolactam.
2-methoxy phenol, 2-hydroxypropionphenone, diethylene glycol, benzyl alcohol, dipropylene glycol, triethylene glycol, anhydroerythritol, thiodiethylene glycol, 5-methyl-2-pyrrolidinone, N-methyl-2-oxazolidinone, N-formyl piperidine, dimethyl phthalate, .gamma.-butyrolactone, dimethyl sulphoxide, ethylene carbonate, propylene carbonate, and .epsilon.-caprolactam.
6. A process according to claim 5, characterised in that the solvent contains at least one component from the group made up of:
ethylene carbonate, propylene carbonate, benzyl alcohol, .gamma.-butyrolactone, .epsilon.-caprolactam, dimethyl phthalate, and dipropylene glycol.
ethylene carbonate, propylene carbonate, benzyl alcohol, .gamma.-butyrolactone, .epsilon.-caprolactam, dimethyl phthalate, and dipropylene glycol.
7. A process according to claim 6, characterised in that the solvent contains at least one component from the group made up of:
propylene carbonate, ethylene carbonate, and benzyl alcohol.
propylene carbonate, ethylene carbonate, and benzyl alcohol.
8. A process according to any one of the preceding claims, characterised in that the boiling point of the solvent is above 477 K (204°C).
9. A process according to any one of the preceding claims, characterised in that the melting point of the solvent is below 318 K (45°C).
10. A process according to any one of the preceding claims, characterised in that the polymer dissolving temperature is in the range of 453 K (180°C) to 513 K (240°C).
11. A process according to any one of the preceding claims, characterised in that the polymer is dissolved at a temperature higher than or equal to the boiling point of the solvent.
12. A process according to any one of the preceding claims, characterised in that at least 50 wt.% of the solvent is removed from the extruded product by a means other than extraction.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL9300060 | 1993-01-13 | ||
| NL9300060 | 1993-01-13 | ||
| PCT/EP1994/000061 WO1994016127A1 (en) | 1993-01-13 | 1994-01-07 | Process for the preparation of polyketone fibres |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2153583A1 true CA2153583A1 (en) | 1994-07-21 |
Family
ID=19861906
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002153583A Abandoned CA2153583A1 (en) | 1993-01-13 | 1994-01-07 | Process for the preparation of polyketone fibres |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP0679201B1 (en) |
| JP (1) | JP3411279B2 (en) |
| CN (1) | CN1116435A (en) |
| AT (1) | ATE167534T1 (en) |
| BR (1) | BR9405807A (en) |
| CA (1) | CA2153583A1 (en) |
| DE (1) | DE69411146T2 (en) |
| ES (1) | ES2120008T3 (en) |
| RU (1) | RU2121017C1 (en) |
| UA (1) | UA42708C2 (en) |
| WO (1) | WO1994016127A1 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2733844B1 (en) * | 1995-05-03 | 1997-06-06 | Alcatel Cable | OPTICAL FIBER AND FIBER OPTIC TAPE, AND MANUFACTURING METHOD THEREOF |
| KR100445354B1 (en) | 1998-08-10 | 2004-08-21 | 아사히 가세이 가부시키가이샤 | Polyketone solution |
| US6818728B2 (en) | 2001-02-27 | 2004-11-16 | Asahi Kasei Kabushiki Kaisha | Polyketone fiber and process for producing the same |
| US7459516B2 (en) | 2002-08-29 | 2008-12-02 | Asahi Kasei Fibers Corporation | Polyketone fiber and process for producing the same |
| JP2007283896A (en) | 2006-04-17 | 2007-11-01 | Bridgestone Corp | Pneumatic tire |
| KR101373832B1 (en) * | 2012-03-23 | 2014-03-14 | 아주대학교산학협력단 | A precess for preparing polyketone using benzyl alcohol |
| CN111647960B (en) * | 2020-05-09 | 2021-06-11 | 中国水产科学研究院东海水产研究所 | Manufacturing method of loss-reducing and resistance-reducing wire for marine ranching |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8822349D0 (en) * | 1988-09-22 | 1988-10-26 | Shell Int Research | Process for preparation of thermoplastic fibres |
| NL8901253A (en) * | 1989-05-19 | 1990-12-17 | Stamicarbon | POLYMERIC FILAMENTS, TAPES AND FILMS WITH HIGH MODULUS, HIGH STRENGTH AND HIGH MELTING TEMPERATURE AND A METHOD FOR THE PRODUCTION THEREOF. |
| DE69115346T2 (en) * | 1990-05-09 | 1996-07-18 | Akzo Nobel Nv | Process for the production of polyketone fibers |
| NL9002666A (en) * | 1990-12-05 | 1992-07-01 | Stamicarbon | COMPOSITION OF AN ETHENE CARBON MONOXIDE COPOLYMER. |
-
1994
- 1994-01-07 ES ES94904651T patent/ES2120008T3/en not_active Expired - Lifetime
- 1994-01-07 CN CN94190937A patent/CN1116435A/en active Pending
- 1994-01-07 CA CA002153583A patent/CA2153583A1/en not_active Abandoned
- 1994-01-07 AT AT94904651T patent/ATE167534T1/en not_active IP Right Cessation
- 1994-01-07 EP EP94904651A patent/EP0679201B1/en not_active Expired - Lifetime
- 1994-01-07 UA UA95073315A patent/UA42708C2/en unknown
- 1994-01-07 WO PCT/EP1994/000061 patent/WO1994016127A1/en active IP Right Grant
- 1994-01-07 DE DE69411146T patent/DE69411146T2/en not_active Expired - Fee Related
- 1994-01-07 RU RU95116596A patent/RU2121017C1/en active
- 1994-01-07 BR BR9405807A patent/BR9405807A/en not_active IP Right Cessation
- 1994-01-07 JP JP50758194A patent/JP3411279B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| UA42708C2 (en) | 2001-11-15 |
| BR9405807A (en) | 1995-12-19 |
| EP0679201B1 (en) | 1998-06-17 |
| RU2121017C1 (en) | 1998-10-27 |
| EP0679201A1 (en) | 1995-11-02 |
| RU95116596A (en) | 1997-06-10 |
| WO1994016127A1 (en) | 1994-07-21 |
| JPH08507328A (en) | 1996-08-06 |
| ES2120008T3 (en) | 1998-10-16 |
| DE69411146T2 (en) | 1999-01-07 |
| CN1116435A (en) | 1996-02-07 |
| DE69411146D1 (en) | 1998-07-23 |
| JP3411279B2 (en) | 2003-05-26 |
| ATE167534T1 (en) | 1998-07-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US3369057A (en) | Polyamide-polyester dispersions wherein the polyamide is less than 40% amine terminated | |
| EP0456306A1 (en) | Process for making polyketone fibres | |
| CA2153583A1 (en) | Process for the preparation of polyketone fibres | |
| EP2772571A1 (en) | Spun-dyed meta-type fully aromatic polyamide fiber | |
| US5162091A (en) | Polyester fibers and process of making | |
| US5302453A (en) | Molecular orientation articles molded from high-molecular weight polyethylene and processes for preparing same | |
| CN108048946B (en) | Hydrophilic flame-retardant polyester fiber material and preparation method thereof | |
| US5820806A (en) | Process for the preparation of polyketone fibers | |
| JPS6128015A (en) | Production of poly(p-phenylenebenzo-bis-thiazole fiber | |
| Kaneda et al. | Wholly aromatic polyamides containing bridged biphenylylene groups, 1. Poly (3, 8‐phenanthridinonediyl terephthalamide) | |
| JP2911563B2 (en) | Polyamide, and molded articles, films and fibers obtained from the polyamide | |
| JPH0641814A (en) | Production of drawn molded body of ultrahigh-molecular weight polypropylene | |
| US3624193A (en) | Polyamide filamentmaking process including solid-state polymerization | |
| US4045512A (en) | Melt blending polyamide process | |
| JP2994701B2 (en) | Melt viscosity-reducing agent for polyester resin, and polyester fiber | |
| JP3169961B2 (en) | Composition of ethylene / carbon monoxide copolymer | |
| RU2217530C1 (en) | Natural silk solving method | |
| JP2000226730A (en) | Solution-dyed polyamide fiber and its production | |
| CN115103870B (en) | Stain resistant branched polyamides | |
| KR20040010625A (en) | Carbon black pigmented yarn with improved physical properties | |
| KR20220140609A (en) | Polyamide-Based Masterbatch Blends | |
| KR100855696B1 (en) | Method for producing polyamide 6 having improved dyeability and spinnability | |
| EP0351707A2 (en) | High strength fibers of stereoregular polystyrene | |
| CA1123563A (en) | Process for melt spinning acrylonitrile polymer hydrates | |
| JP2553129B2 (en) | Polyvinyl alcohol fiber with good fatigue resistance |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Discontinued |