METHOD FOR PRODUCTION OF POLY-VINYL ALCOHOL -FILAMENT FIBRE OF HIGH STRENGTH AND ELASTICITY

Abstract

A filament fibre production method including the process steps of: filtration of and/or applying evaporation process to wastewater containing Polyvinyl alcohol polymer from sizing process and/or painting process in a manner to contain Polyvinyl alcohol polymer at rate of 20-30% by mass, adding Carbonyl di-imidazole and Ethylenediamine or 4-chloro-Propionyl chloride and Etylendiamine into wastewater having Polyvinyl alcohol polymer in 20-30% rate as a result of filtration and/or evaporation process and obtaining PVA-Etylendiamine hydrogel solvent, adding dimethyl sulfoxide, Boric Acid, Acetic Acid and surface active agent into solvent bath containing PVA-Ethylendiamine hydrogel solvent at 20-30% rate, applying coagulation process to obtained PVA-Ethylendiamine hydrogel solvent with acetone of critic fluid phase, stretching Polyvinyl alcohol polymer passing through coagulation bath at 200 C.°-250 C.° temperature range when wet, and subjecting to fixing process.

Claims

1. A filament fibre production method comprising process steps of: filtration of and/or applying evaporation process to wastewater containing Polyvinyl alcohol polymer from sizing process and/or painting process in a manner to contain Polyvinyl alcohol polymer at rate of 20-30% by mass; into wastewater comprising Polyvinyl alcohol polymer in 20-30% rate as a result of filtration and/or evaporation process; adding Carbonyl di-imidazole and Ethylenediamine or 4-chloro-Propionyl chloride and Etylendiamine and obtaining PVA-Ethylenediamine hydrogel solvent; adding dimethyl sulfoxide, Boric Acid, Acetic Acid and surface active agent into solvent bath containing PVA-Ethylendiamine hydrogel solvent at 20-30% rate characterized comprising process steps of: applying coagulation process to obtained PVA-Ethylendiamine hydrogel solvent with acetone of critic fluid phase; and stretching Polyvinyl alcohol polymer passing through coagulation bath at 200 C.°-250 C.° temperature range when wet, and subjecting to fixing process.

2. The filament fibre production method according to claim 1, further comprising the process steps of adding dimethyl Sulfoxide in rate of 30-70% by mass, Boric Acid in rate of 0,1-1,0% by mass, Acetic Acid with pH value adjusted in range of 4 to 5 and surface active agent in rate of 1-20% by mass into wastewater mixture containing Polyvinyl Alcohol polymer in rate of 20-30% by mass onto wastewater comprising Polyvinyl alcohol polymer in 20-30% rate as a result of filtration and/or evaporation process.

3. The filament fibre production method according to claim 1, comprising the process step of adding non-ionic Polyethylene Glycol I as a surface active agent.

4. The filament fibre production method according to claim 1, comprising the process step of adding non-ionic Polyhydric alcohol as a surface active agent.

5. The filament fibre production method according to claim 1, comprising the process step of adding non-ionic Polyethylene Glycol in rate of 1-20% by mass as surface active agent.

6. The filament fibre production method according to claim 1, comprising the process step of adding non-ionic Polyhydric alcohol in rate of 1-20% by mass as surface active agent.

7. The filament fibre production method according to claim 1, comprising coagulation process of nozzle diameter varying between 0.11 mm and 0.08 mm.

8. The filament fibre production method according to claim 1, comprising coagulation process containing 10-100 g/lt NaOH, 100-300 g/lt Sodium Sulphate, acetone in rate of 2-20% by mass, 2-propanol in rate of 2-20% by mass.

9. The filament fibre production method according to claim 1, comprising a process of transition of acetone into critical fluid phase is at 235° C. temperature and pressure of 46.9 bars.

Description

FIGURES FOR BETTER UNDERSTANDING OF INVENTION

[0021] FIG. 1 shows schematic view of filament fibre production method of the invention.

DETAILED DESCRIPTION OF THE INVENTION

[0022] In this detailed description, the preferred embodiments of the invention have been described in a manner not forming any restrictive effect and only for purpose of better understanding of the matter.

[0023] The invention relates to a method for filament fibre production for use in textile sector. In the method of the invention, said filament fibre is obtained by means of recycling of wastewater containing polyvinyl alcohol (PVA) polymer. Process steps of the method of invention are shown schematically in FIG. 1. According to the FIGURE, wastewater containing Polyvinyl alcohol (PVA) polymer is obtained from two different sources. One of the is sizing process. Said sizing process is realized by means of providing absorption of agents such as carboxy methyl cellulose, polyvinyl alcohol by yarns to be used in weaving in order to increase resistance of yarn. During that time while said sizing agents (carboxy methyl cellulose, polyvinyl alcohol) are fixed onto yarn surface by physical powers, the section not appliqued is discharged into wastewater. Rate of Polyvinyl alcohol (PVA) in said wastewater is 1-1,5% by mass. Another source of wastewater containing Polyvinyl alcohol (PVA) polymer is obtained from painting process. In normal process, in order to achieve high water absorption and soft touching features, cotton yarn is spun in reverse spinning with polyvinyl alcohol (PVA) polymer and after said spinning, weaving is started and fabric of various constructions are obtained. When the obtained fabrics is treated with acidic water at high or low temperatures during painting process, wastewater containing polyvinyl alcohol (PVA) polymer at 1-1,5% rate by mass is obtained. Rate of Polyvinyl alcohol (PVA) polymer rate in the wastewater obtained in said processes by mass is brought to 20-30% range by mass in filtration and/or evaporation process steps and thus regained concentrate Polyvinyl Alcohol (PVA) polymer is obtained. Polymerization date of said obtained polymer is in the range of 500-3500. In the method of the invention, chemical reactions are performed to prepare dope solvent in the first process step. There are two alternative reactions for preparation of said dope solvent. In the first alternative reaction is initiated by adding Carbonyldiimidazole (CDI) and Etylendiamine in rate of 10-20% rate by mass into medium having Polyvinyl alcohol (PVA) polymer. Said reaction is shown in FIGURE below.

##STR00002##

[0024] In other alternative, reaction is executed by adding 4-Chloro Propionyl chloride and Ethylenediamine in range of 10-20% onto Polyvinyl alcohol (PVA) polymer. Said reaction is shown in FIGURE below.

##STR00003## ##STR00004##

[0025] Thus PVA-Ethylenediamine hydrogel solvent is prepared by use of either of said two alternatives. This provides increase in disassociation arising as a result of getting closure between PVA polymers, cross bonding between non-concentrated PVA molecules. Thus, formation of aggregation increases, physical structure of colloidal suspension in homogeneity form occurs. The obtained hydrogel structure is shown below.

##STR00005##

[0026] Colloidal suspension physical structure in homogenous form obtained in this stage is formed to increase polymerization rate, strength, elasticity and efficiency of Polyvinyl alcohol (PVA) in wastewater. In the second process step, dimethyl Sulfoxide in rate of 30-40% by mass, Boric Acid in rate of 0,1-1,0% by mass, Acetic Acid with pH value in range of 4 to 5 are added to waste water mixture containing Polyvinyl Alcohol (PVA) Etylendiamine hydrogel solvent in rate of 20-30% by mass. In addition to said added chemicals, surface active agent is also added in this stage. As surface active agent, Polyethylene Glycol in rate of 1/20% by mass or non-ionic Polyhydric alcohol in rate of 1-20% by mass can be used. However, coagulation process is needed to improve strength, elasticity features of Polyvinyl alcohol (PVA) polymer based filament aimed to be obtained and to provide surface homogeneity. Said coagulation process provides convey of acetone is diffused form between Polyvinyl alcohol (PVA) polymer and thus penetration of acetone into Polyvinyl alcohol (PVA) polymer is provided in critic phase. In said Coagulation Bath, nozzle diameter may vary from 0.11 mm to 0.08 mm and 10-100 g/It NaOH, 100-300 g/It Sodium Sulphate, acetone in rate of 2-20% by mass, 2-propanol in rate of 2-20% by mass are used. In the last process step, during super critic phase spinning process is applied. Transition of acetone into critical fluid phase is executed preferably at 235° C. temperature and pressure of 46.9 bars. Density rate of acetone under such circumstances varies from 0.2 g/cm.sup.3-0.9 g/cm.sup.3, viscosity 0.2-1.0 poise, and diffusion rate 0.1-3.3 cm.sup.2/sec. Polyvinyl alcohol (PVA) polymer solvent from nozzles gets solidified in coagulation bath and transformed into filament fibre structure. Polyvinyl alcohol (PVA) polymer from coagulation bath is wound onto roller in fibre form by pressure from nozzles. At this stage it is shrunk at saturated evaporation medium at temperature range of 200° C.-250° C. and fixing between winding rollers is made. Said fixing process fixes spinning forces between Polyvinyl alcohol (PVA) polymer. For that purpose, wet spinning or wet jet dry spinning can be applied. In wet jet dry spinning process, differently from wet spinning, after coagulation bath, shrinking between winding rollers in saturated evaporation medium at temperature range of 200° C.-250° C. is performed and then fixing process is performed.