CN101967765B - High-beating-degree cotton pulp product used for banknote paper and production method thereof - Google Patents
High-beating-degree cotton pulp product used for banknote paper and production method thereof Download PDFInfo
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- CN101967765B CN101967765B CN2010105346968A CN201010534696A CN101967765B CN 101967765 B CN101967765 B CN 101967765B CN 2010105346968 A CN2010105346968 A CN 2010105346968A CN 201010534696 A CN201010534696 A CN 201010534696A CN 101967765 B CN101967765 B CN 101967765B
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- 229920000742 Cotton Polymers 0.000 title claims abstract description 93
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 238000010009 beating Methods 0.000 claims abstract description 74
- 239000003513 alkali Substances 0.000 claims abstract description 22
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 9
- 239000003381 stabilizer Substances 0.000 claims abstract description 9
- 239000002002 slurry Substances 0.000 claims description 44
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 31
- 229920002472 Starch Polymers 0.000 claims description 19
- 235000019698 starch Nutrition 0.000 claims description 19
- 241000209094 Oryza Species 0.000 claims description 15
- 235000007164 Oryza sativa Nutrition 0.000 claims description 15
- 235000009566 rice Nutrition 0.000 claims description 15
- 239000008107 starch Substances 0.000 claims description 15
- 238000005304 joining Methods 0.000 claims description 13
- 230000000740 bleeding effect Effects 0.000 claims description 12
- 238000010792 warming Methods 0.000 claims description 10
- 239000012535 impurity Substances 0.000 claims description 9
- 238000007598 dipping method Methods 0.000 claims description 8
- 238000009897 hydrogen peroxide bleaching Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 3
- 238000009955 starching Methods 0.000 claims description 2
- 238000009835 boiling Methods 0.000 abstract description 9
- 238000004061 bleaching Methods 0.000 abstract description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000460 chlorine Substances 0.000 abstract description 2
- 229910052801 chlorine Inorganic materials 0.000 abstract description 2
- 238000004537 pulping Methods 0.000 abstract 7
- 238000002386 leaching Methods 0.000 abstract 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract 2
- 239000001301 oxygen Substances 0.000 abstract 2
- 229910052760 oxygen Inorganic materials 0.000 abstract 2
- 230000000149 penetrating effect Effects 0.000 abstract 2
- 206010033546 Pallor Diseases 0.000 abstract 1
- 230000000694 effects Effects 0.000 abstract 1
- 239000007788 liquid Substances 0.000 abstract 1
- 239000000835 fiber Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 10
- 230000008569 process Effects 0.000 description 7
- 239000000428 dust Substances 0.000 description 6
- 238000006116 polymerization reaction Methods 0.000 description 6
- 238000007667 floating Methods 0.000 description 5
- 229920002678 cellulose Polymers 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 241000202567 Fatsia japonica Species 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The invention provides a production method of a high-beating-degree cotton pulp product used for banknote paper, comprising the following steps: a) breaking and opening cotton linter; b) boiling and blanching, wherein, the alkali matching temperature is the normal temperature, the oven-dry amount of the matched alkali relative to the cotton linter is 0.5-4%; the oven-dry amount of hydrogen peroxide relative to the cotton linter is 0.5-5%; the matched alkali liquid ratio is 1:3-5; the relative oven-dry amount of oxygen bleaching stabilizer is 0.1-0.5%; and the relative oven-dry amount of penetrating agent is 0.5-0.9%; c) pulping and removing sands: 1) Holland pulping, wherein the current is 140A-160A, 2) fine fibering, wherein the pulping current is 150A-160A, 3) pulping again, and the pulping current is 300A-350A, 4) jordaning, and 5) removing the sands; and d) pulping. In the invention, low-temperature, low-alkali, boiling and leaching integrated pulping is adopted without chlorine, the boiling and leaching effects is improved by adding the oxygen leaching stabilizer and the penetrating agent assistant; and the produced cotton pulp has high beating degree, good strength, high folding endurance, and can be used for producing the banknote paper.
Description
Technical field
The present invention relates to cotton pulp dregs of rice production field, be specifically related to a kind of bank-note paper with high beating degree cotton pulp dregs of rice product and production method thereof.
Background technology
Banknote is special paper with paper, the bright and clean exquisiteness of quality, tough and tensile folding, and well-pressed smooth, whiteness is very high.In recent years, in the international market, make Euro, sterling and the used raw material combing machine noil output of various cheque paper and descend gradually; And; The exploitation of various blend fibres, pure combing machine noil is fewer and feweri, brings into use cotton linter to substitute the combing machine noil now gradually and produces the cotton pulp dregs of rice.
Cotton in China cultivated area and annual production are the No. 1 in the world, so cotton linter resource is abundant, and the quality grade of cotton linter containing assorted lacking because major part be manual the harvesting, quality grade height.With the cotton linter is that the feedstock production cotton pulp dregs of rice are used bank-note paper, cheque paper, passport paper, notarization document with being only way from now on the products such as paper.
Bank-note paper has very high requirement with the cotton pulp dregs of rice to beating degree; High beating degree cotton pulp can reduce the beating time of speciality paper production process; Improve the speciality paper plant output; Stay-in-grade high beating degree cotton pulp is that decisive factor is played in very high bank-note paper production to the quality stability requirement, and therefore high beating degree cotton pulp is the product of home and abroad speciality paper and the market in urgent need of security cheque paper.
Yet in the international market; The cotton pulp product is most of uses cotton pulp for viscose, manufacturing technique method employing high temperature, high pressure, high-alkali conditions of cooking, and added value of product is low; In the production process; Waste water COD content is high, and treatment cost is high, the low 14SR～20SR that is generally of the beating degree of the cotton pulp dregs of rice of preparation.
Summary of the invention
The problem that the present invention solves is to provide a kind of bank-note paper with high beating degree cotton pulp dregs of rice product and production method thereof, and the cotton pulp dregs of rice beating degree of production is high, is applicable to and commercially produces bank-note paper.
In order to solve the problems of the technologies described above, technical scheme of the present invention is:
A), and carry out removal of impurities, squeezing, dipping to the cotton linter opener;
B) cotton linter is boiled float; Joining the alkali temperature is normal temperature, and it is dense in NaOH to join alkali alkali, and the cotton linter oven-dry weight is 0.5%～4% relatively; Hydrogen peroxide solution is 0.5%～5% with respect to the cotton linter oven-dry weight; Joining lye ratio is 1: 3～5, and hydrogen peroxide bleaching stabilizer is 0.1%～0.5% with respect to oven-dry weight, and bleeding agent is with respect to oven-dry weight 0.5%～0.9%;
C) making beating desanding comprises:
1) slurry discongest, brooming: holland type making beating, making beating electric current 140A～160A;
2) fibrillating: the making beating electric current is 150A～160A;
3) will pull an oar through the slurry of fibrillating: the making beating Current Control is at 300A～350A;
4) defibrination;
5) desanding;
D) copy slurry.
As preferably, said cotton linter be I class cotton linter with or II class cotton linter.
As preferably, maturity is that the percentage by weight of 65%～85% cotton linter is 10%～90% in the said I class cotton linter, and maturity is that the percentage by weight of 75%～85% cotton linter is 10%～90% in the said II class cotton linter.
As preferably, said boil to float in the rotary spherical digester carry out, heated up 30 minutes～120 minutes for the first time, be warming up to 60 ℃～120 ℃, be incubated 20 minutes for the first time～80 minutes; Heated up 30 minutes～120 minutes for the second time, be warming up to 70 ℃～130 ℃, be incubated 60 minutes for the second time～100 minutes, steam bleeding is accomplished to boil and is floated then.
As preferably, said 1) during the holland type making beating, light cutter was discongested 30 minutes～60 minutes, washing, concentrated, and starched densely to be controlled at 3.0%～4.0%, beating time 120 minutes～140 minutes.
As preferably, said 2) beating time is 60 minutes～80 minutes during fibrillating, and starching dense is 3.5%～4.0%.
As preferably, said 3) slurry that will be when the slurry of fibrillating is pulled an oar is dense to be controlled at 1.8%～2.0%.
As preferably, said 4) power of defibrination is 340kW～380kW, starches densely to be controlled at 1.8%～2.0%.
As preferably, said 5) Pressure control of desanding is at 2.8MPa～3.2MPa, starches densely to be controlled at 0.4%～0.6%.
As preferably, said d) copying slurry comprises:
I) join slurry, concentration is controlled in 0.8%～1.2% scope;
II) copy slurry, copy the pressure control range of slurry wet end and press section: wet end couch roll pressure 1.5kgf/cm
2～2.8kgf/cm
2, a pressure pressure is controlled at 2.5kgf/cm
2～3.5kgf/cm
2, two pressure pressures are controlled at 3.2kgf/cm
2～4.0kgf/cm
2Copy the control of slurry drying section temperature: first group of dryer temperature is controlled at 100 ℃～108 ℃, and second group of dryer temperature is controlled at 120 ℃～150 ℃, and the 3rd group of dryer temperature is controlled at 125 ℃～155 ℃, and the 4th group of dryer temperature is controlled at 100 ℃～108 ℃.
A kind of bank-note paper is with the high beating degree cotton pulp dregs of rice, by above-described production method preparation.
Bank-note paper provided by the invention is with the production method of the high beating degree cotton pulp dregs of rice; Utilize cotton linter to be raw material, adopt low temperature, low alkali, no chlorine to boil bleaching integrated slurrying, utilize the hollander making beating earlier; Promote beating degree in conjunction with big tapering jordan; Take the double plate defibrination further to adjust beating degree meeting the demands again, the cotton pulp dregs of rice beating degree of production is high, intensity is good, folding strength is high, can be used to produce Euro, sterling bank-note paper, cheque paper, passport paper, notarization document and uses paper.
The specific embodiment
In order further to understand the present invention, below in conjunction with embodiment the preferred embodiment of the invention is described, describe just to further specifying feature and advantage of the present invention but should be appreciated that these, rather than to the restriction of claim of the present invention.
Embodiment 1:
A), and carry out removal of impurities, squeezing, dipping to the cotton linter opener.Maturity is that the percentage by weight of 73% cotton linter is 60% in the used I class cotton linter, and maturity is that the percentage by weight of 78% cotton linter is 30% in the II class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, fiber dust removing machine cotton linter is carried out removal of impurities, then through cyclone separator, through screw press, dipping.Removal of impurities can make cotton linter in process, the cotton seed hulls that is contained, cotton leaf removed, thereby can reduce boiling intensity, and the reduction process conditions avoid cellulose self intensity to be destroyed.
B) cotton linter is boiled float.The present invention utilizes alkali one hydrogen peroxide digesting technoloy; Disposable completion boiling in boiling vessel, two processes of bleaching are boiled the process of floating and are adopted secondary temperature elevation, secondary insulation, and main purpose is to let reaction condition relax; Prevent that the rapid decomposition of hydrogen peroxide solution causes the ball internal pressure to increase sharply under the high temperature; Cellulose is damaged, and when improving whiteness, reduces the damage of fiber as far as possible.
Joining the alkali temperature is 83 ℃, and it is dense in NaOH to join alkali alkali, and the cotton linter oven-dry weight is 0.8% relatively; Hydrogen peroxide solution is 4.5% with respect to the cotton linter oven-dry weight; Joining lye ratio is 1: 4, promptly the volume of NaOH and hydrogen peroxide solution and with the ratio of the weight of cotton linter be 1: 4, hydrogen peroxide bleaching stabilizer is 0.2% with respect to oven-dry weight; Bleeding agent boils bleaching integrated operation through fully mixing after conveying worm is delivered to respect to oven-dry weight 0.8%.Boil the U.S. prompt molecular material technology of hydrogen peroxide bleaching stabilizer and east, the bleeding agent Hefei Co., Ltd production that the process of floating is used,, reduce the invalid decomposition of hydrogen peroxide solution, accomplish to boil and float the high needs that require in vain through the reaction of the metal ion in hydrogen peroxide bleaching stabilizer and the material; Make the timely and lignin reaction of NaOH ability through bleeding agent, cotton seed hulls, cotton skin are removed, thus the purification cellulose.
Boil to float in the rotary spherical digester and carry out, heated up 35 minutes for the first time, be warming up to 90 ℃, be incubated 70 minutes for the first time; Heated up 30 minutes for the second time, be warming up to 110 ℃, be incubated 90 minutes for the second time, steam bleeding is accomplished to boil and is floated then.Cotton linter to boiling after floating detects, and recording the degree of polymerization is 2160.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 40 minutes, washing, concentrated, starch densely to be controlled at 3.5%, making beating electric current 155A, beating time 125 minutes, completion is discongested and brooming.
Record fibre length 3.6mm, 14.5 ° of SR of beating degree.
(2) fibrillating:
Slurry gets into fibrillating after brooming, making beating electric current 155A, and beating time 75 minutes is starched densely 3.6%, accomplishes fibrillating.
(3) get into big tapering jordan through the slurry of fibrillating and pull an oar, the making beating Current Control is at 335A, starch densely to be controlled at 1.9%, accomplishes and pulls an oar.
Record fibre length 3.0mm, 20.2 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, slurry after the making beating gets into double disc refiner, and defibrination power 350KW starch and densely is controlled at 1.9%, the completion defibrination.
Survey fibre length 2.9mm, 21 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, the desanding Pressure control is at 2.9MPa, starch densely to be controlled at 0.4%,, one-level is taked 606 desanders, secondary is taked 600 desanding, and by three sections flow processs controls of one-level, will starch simmer down to 3.5% after the desanding.
D) copy slurry
Joining slurry concentration is controlled in 0.8% scope.
Copy slurry wet end and press section, pressure control range: wet end couch roll pressure 1.7kgf/cm
2, a pressure pressure is controlled at 2.6kgf/cm
2, two pressure pressures are controlled at 3.5kgf/cm
2
Copy the control of slurry drying section temperature: first group of dryer temperature is controlled at 102 ℃; Second group of dryer temperature is controlled at 127 ℃, and the 3rd group of dryer temperature is controlled at 126 ℃, and the 4th group of dryer temperature is controlled at 105 ℃; Thereby assurance pulp moisture is removed under temperate condition, does not influence the pulp whiteness.
The back pulp deciding grade and level weight of manufacturing paper with pulp 530g/m
2, moisture 8.5% after the paper cutter section, utilizes the magma packing.
Each item index of the product that makes is:
The degree of polymerization 2060 whiteness 83%
Folding strength 1037 moisture 8.7%
Irony 32PPM fibre length 2.9mm
Deciding grade and level weight 532g/m
2, beating degree 21SR
Dust 30mm
2/ m
2Fluorescence 10mm
2/ m
2
Embodiment 2:
A), and carry out removal of impurities, squeezing, dipping to the cotton linter opener.Maturity is that the percentage by weight of 78% cotton linter is 67% in the used I class cotton linter, and maturity is that the percentage by weight of 72% cotton linter is 33% in the II class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, fiber dust removing machine cotton linter is carried out removal of impurities, then through cyclone separator, through screw press, dipping.
B) cotton linter is boiled float.
Joining the alkali temperature is normal temperature; It is dense in NaOH to join alkali alkali, and the cotton linter oven-dry weight is 3.1% relatively, and hydrogen peroxide solution is 3.5% with respect to the cotton linter oven-dry weight; Joining lye ratio is 1: 3.5; Hydrogen peroxide bleaching stabilizer is 0.4% with respect to oven-dry weight, and bleeding agent boils bleaching integrated operation through fully mixing after conveying worm is delivered to respect to oven-dry weight 0.6%.
Boil to float in the rotary spherical digester and carry out, heated up 45 minutes for the first time, be warming up to 110 ℃, be incubated 75 minutes for the first time; Heated up 38 minutes for the second time, be warming up to 115 ℃, be incubated 95 minutes for the second time, steam bleeding is accomplished to boil and is floated then.Cotton linter to boiling after floating detects, and recording the degree of polymerization is 2043.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 50 minutes, washing, concentrated, starch densely to be controlled at 3.6%, making beating electric current 150A, beating time 135 minutes, completion is discongested and brooming.
Record fibre length 3.6mm, 14.5 ° of SR of beating degree.
(2) fibrillating:
Slurry gets into fibrillating after brooming, making beating electric current 158A, and beating time 65 minutes is starched densely 3.8%, accomplishes fibrillating.
(3) through the slurry of fibrillating, get into big tapering jordan and pull an oar, the making beating Current Control starch and densely is controlled at 1.8% at 340A, accomplishes and pulls an oar.
Record fibre length 2.0mm, 20.6 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, slurry after the making beating gets into double disc refiner, and defibrination power 355KW starch and densely is controlled at 1.8%, the completion defibrination.
Record fibre length 3.1mm, 21.5 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, the desanding Pressure control is at 3.1MPa, starches densely to be controlled at 0.5%, one-level is taked 606 desanders, secondary is taked 600 desanding, and presses three sections flow processs controls of secondary, will starch simmer down to 3.6% after the desanding.
D) copy slurry
Joining slurry concentration is controlled in 0.8% scope.
Copy slurry wet end and press section, pressure control range: wet end couch roll pressure 1.7kgf/cm
2, a pressure pressure is controlled at 2.6kgf/cm
2, two pressure pressures are controlled at 3.5kgf/cm
2
Copy the control of slurry drying section temperature: first group of dryer temperature is controlled at 102 ℃; Second group of dryer temperature is controlled at 137 ℃, and the 3rd group of dryer temperature is controlled at 146 ℃, and the 4th group of dryer temperature is controlled at 105 ℃; Thereby assurance pulp moisture is removed under temperate condition, does not influence the pulp whiteness.
The back pulp deciding grade and level weight of manufacturing paper with pulp 612g/m
2, moisture 8.9% after the paper cutter section, utilizes the magma packing.
Each item index of the product that makes is:
The degree of polymerization 2012 whiteness 83.5%
Folding strength 938 moisture 8.4%
Irony 31PPM fibre length 3.1mm
Deciding grade and level weight 555g/m
2, beating degree 21.5SR
Dust 18mm
2/ m
2Fluorescence 9mm
2/ m
2
Embodiment 3:
A), and carry out removal of impurities, squeezing, dipping to the cotton linter opener.Maturity is that the percentage by weight of 75% cotton linter is 70% in the used I class cotton linter, and maturity is that the percentage by weight of 82% cotton linter is 30% in the II class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, fiber dust removing machine cotton linter is carried out removal of impurities, then through cyclone separator, through screw press, dipping.
B) cotton linter is boiled float.
Joining the alkali temperature is normal temperature; It is dense in NaOH to join alkali alkali, and the cotton linter oven-dry weight is 3.8% relatively, and hydrogen peroxide solution is 4.0% with respect to the cotton linter oven-dry weight; Joining lye ratio is 1: 4.5; Hydrogen peroxide bleaching stabilizer is 0.45% with respect to oven-dry weight, and bleeding agent boils bleaching integrated operation through fully mixing after conveying worm is delivered to respect to oven-dry weight 0.7%.
Boil to float in the rotary spherical digester and carry out, heated up 45 minutes for the first time, be warming up to 115 ℃, be incubated 60 minutes for the first time; Heated up 95 minutes for the second time, be warming up to 109 ℃, be incubated 98 minutes for the second time, steam bleeding is accomplished to boil and is floated then.Cotton linter to boiling after floating detects, and recording the degree of polymerization is 2023.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 55 minutes, washing, concentrated, starch densely to be controlled at 4.0%, making beating electric current 155A, beating time 140 minutes, completion is discongested and brooming.
Survey fibre length 3.4mm, 15.0 ° of SR of beating degree.
(2) fibrillating:
Slurry gets into fibrillating for the first time after brooming, making beating electric current 155A, and beating time 80 minutes is starched densely 3.5%, accomplishes fibrillating.
(3) through the slurry of fibrillating, get into big tapering jordan and pull an oar, the making beating Current Control starch and densely is controlled at 1.95% at 345A, accomplishes and pulls an oar.
Record fibre length 1.9mm, 21.0 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, slurry after the making beating gets into double disc refiner, and defibrination power 345KW starch and densely is controlled at 1.8%, the completion defibrination.
Record fibre length 1.85mm, 22.0 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, the desanding Pressure control is at 3.1MPa, starch densely to be controlled at 0.6%,, one-level is taked 606 desanders, secondary is taked 600 desanding, and presses three sections flow processs controls of secondary, will starch simmer down to 3.5% after the desanding.
D) copy slurry
Joining slurry concentration is controlled in 0.7% scope.
Copy slurry wet end and press section, pressure control range: wet end couch roll pressure 2.1kgf/cm
2, a pressure pressure is controlled at 2.8kgf/cm
2, two pressure pressures are controlled at 3.9kgf/cm
2
Copy the control of slurry drying section temperature: first group of dryer temperature is controlled at 105 ℃; Second group of dryer temperature is controlled at 128 ℃, and the 3rd group of dryer temperature is controlled at 130 ℃, and the 4th group of dryer temperature is controlled at 103 ℃; Thereby assurance pulp moisture is removed under temperate condition, does not influence the pulp whiteness.
The back pulp deciding grade and level weight of manufacturing paper with pulp 618g/m
2, moisture 9.5% after the paper cutter section, utilizes the magma packing.
Each item index of the product that makes is:
The degree of polymerization 2023 whiteness 83.5%
Folding strength 815 moisture 9.5%
Irony 37PPM fibre length 1.85mm
Deciding grade and level weight 618g/m
2, beating degree 22.0SR
Dust 30mm
2/ m
2Fluorescence 8mm
2/ m
2
More than a kind of bank-note paper provided by the present invention has been carried out detailed introduction with high beating degree cotton pulp dregs of rice product and production method thereof.Used concrete example among this paper principle of the present invention and embodiment are set forth, the explanation of above embodiment just is used for helping to understand method of the present invention and core concept thereof.Should be pointed out that for those skilled in the art, under the prerequisite that does not break away from the principle of the invention, can also carry out some improvement and modification to the present invention, these improvement and modification also fall in the protection domain of claim of the present invention.
Claims (2)
1. a bank-note paper is characterized in that with the production method of the high beating degree cotton pulp dregs of rice, may further comprise the steps:
A) to the cotton linter opener; And carry out removal of impurities, squeezing, dipping; Said cotton linter be I class cotton linter with or II class cotton linter; Maturity is that the percentage by weight of 65%～85% cotton linter is 10%～90% in the said I class cotton linter, and maturity is that the percentage by weight of 75%～85% cotton linter is 10%～90% in the said II class cotton linter;
B) cotton linter is boiled float; Joining the alkali temperature is normal temperature, and it is dense in NaOH to join alkali alkali, and the cotton linter oven-dry weight is 0.5%～4% relatively; Hydrogen peroxide solution is 0.5%～5% with respect to the cotton linter oven-dry weight; Joining lye ratio is 1: 3～5, and hydrogen peroxide bleaching stabilizer is 0.1%～0.5% with respect to oven-dry weight, and bleeding agent is with respect to oven-dry weight 0.5%～0.9%;
Said boil to float in the rotary spherical digester carry out, heated up 30 minutes～120 minutes for the first time, be warming up to 60 ℃～120 ℃, be incubated 20 minutes for the first time～80 minutes; Heated up 30 minutes～120 minutes for the second time, be warming up to 70 ℃～130 ℃, be incubated 60 minutes for the second time～100 minutes, steam bleeding is accomplished to boil and is floated then;
C) making beating desanding comprises:
1) slurry discongest, brooming: holland type making beating, making beating electric current 140A～160A, light cutter was discongested 30 minutes～60 minutes, washing, concentrated, and starched densely to be controlled at 3.0%～4.0%, beating time 120 minutes～140 minutes;
2) fibrillating: the making beating electric current is 150A～160A, and beating time is 60 minutes～80 minutes, and starching dense is 3.5%～4.0%;
3) will pull an oar through the slurry of fibrillating: the making beating Current Control is starched and densely is controlled at 1.8%～2.0% at 300A～350A;
4) defibrination, power are 340kW～380kW, starch densely to be controlled at 1.8%～2.0%;
5) desanding, Pressure control be at 2.8MPa～3.2MPa, starches densely to be controlled at 0.4%～0.6%;
D) copy slurry, comprising:
I) join slurry, concentration is controlled in 0.8%～1.2% scope;
II) copy slurry, copy the pressure control range of slurry wet end and press section: wet end couch roll pressure 1.5kgf/cm
2～2.8kgf/cm
2, a pressure pressure is controlled at 2.5kgf/cm
2～3.5kgf/cm
2, two pressure pressures are controlled at 3.2kgf/cm
2～4.0kgf/cm
2Copy the control of slurry drying section temperature: first group of dryer temperature is controlled at 100 ℃～108 ℃, and second group of dryer temperature is controlled at 120 ℃～150 ℃, and the 3rd group of dryer temperature is controlled at 125 ℃～155 ℃, and the 4th group of dryer temperature is controlled at 100 ℃～108 ℃.
2. a bank-note paper is characterized in that with the high beating degree cotton pulp dregs of rice, by the described production method preparation of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105346968A CN101967765B (en) | 2010-11-05 | 2010-11-05 | High-beating-degree cotton pulp product used for banknote paper and production method thereof |
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| CN105421131B (en) * | 2015-10-30 | 2017-05-10 | 重庆市南川区金鑫纸业有限公司 | Pulping method for inner core layer of paper pulp |
| CN112900134A (en) * | 2021-01-25 | 2021-06-04 | 合肥银山棉麻股份有限公司 | Method for improving fracture length index of cotton pulp board |
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| CN101302725A (en) * | 2008-06-10 | 2008-11-12 | 山东银鹰化纤有限公司 | Process for producing cotton dissolving pulp |
| CN101638810A (en) * | 2009-08-20 | 2010-02-03 | 襄樊源力生物科技有限公司 | Method for high effective environmental pollution energy conservation purified cotton production |
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| CN101302725A (en) * | 2008-06-10 | 2008-11-12 | 山东银鹰化纤有限公司 | Process for producing cotton dissolving pulp |
| CN101638810A (en) * | 2009-08-20 | 2010-02-03 | 襄樊源力生物科技有限公司 | Method for high effective environmental pollution energy conservation purified cotton production |
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Denomination of invention: High-beating-degree cotton pulp product used for banknote paper and production method thereof Effective date of registration: 20141202 Granted publication date: 20120725 Pledgee: Suzhou SME financing Company limited by guarantee Pledgor: ANHUI SNOW DRAGON FIBRE TECHNOLOGY Co.,Ltd. Registration number: 2014990001019 |
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Address after: No. 816, North Side of Jinjiang Fifth Road, Economic and Technological Development Zone, Suzhou City, Anhui Province, 234001 Patentee after: Anhui Xuelong New Materials (Group) Co.,Ltd. Address before: No. 318 Suhuai South Road, Suzhou City, Anhui Province, 234000 Patentee before: ANHUI SNOW DRAGON FIBRE TECHNOLOGY Co.,Ltd. |