CN101967764B - High-whiteness cotton pulp product for banknote paper and production method thereof - Google Patents
High-whiteness cotton pulp product for banknote paper and production method thereof Download PDFInfo
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- CN101967764B CN101967764B CN 201010534617 CN201010534617A CN101967764B CN 101967764 B CN101967764 B CN 101967764B CN 201010534617 CN201010534617 CN 201010534617 CN 201010534617 A CN201010534617 A CN 201010534617A CN 101967764 B CN101967764 B CN 101967764B
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- 229920000742 Cotton Polymers 0.000 title claims abstract description 92
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000003513 alkali Substances 0.000 claims abstract description 21
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 10
- 239000003381 stabilizer Substances 0.000 claims abstract description 10
- 238000010009 beating Methods 0.000 claims description 52
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 31
- 239000002002 slurry Substances 0.000 claims description 28
- 229920002472 Starch Polymers 0.000 claims description 17
- 235000019698 starch Nutrition 0.000 claims description 17
- 238000010792 warming Methods 0.000 claims description 15
- 230000000740 bleeding effect Effects 0.000 claims description 13
- 238000005304 joining 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 2
- 238000009955 starching Methods 0.000 claims description 2
- 238000004061 bleaching Methods 0.000 abstract description 10
- 238000009835 boiling Methods 0.000 abstract description 6
- 239000012752 auxiliary agent Substances 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 238000004537 pulping Methods 0.000 abstract 7
- 230000003647 oxidation Effects 0.000 abstract 2
- 238000007254 oxidation reaction Methods 0.000 abstract 2
- 230000000149 penetrating effect Effects 0.000 abstract 2
- 239000007788 liquid Substances 0.000 abstract 1
- 238000007670 refining Methods 0.000 abstract 1
- 239000000835 fiber Substances 0.000 description 13
- 208000032843 Hemorrhage Diseases 0.000 description 11
- 208000034158 bleeding Diseases 0.000 description 11
- 231100000319 bleeding Toxicity 0.000 description 11
- 239000008107 starch Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 8
- 238000006116 polymerization reaction Methods 0.000 description 6
- 238000007667 floating Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 4
- 229920002678 cellulose Polymers 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000428 dust Substances 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
- 238000004886 process control Methods 0.000 description 3
- 239000002994 raw material Substances 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
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 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
- 238000006213 oxygenation reaction Methods 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 high-whiteness cotton pulp for banknote paper, comprising the following steps: a) opening cotton linter; b) boiling and bleaching at the matching alkali temperature of 80-90 DEG C, 0.5-10 percent of matching alkali relative to the absolute dry quantity of the cotton linter, 0.5-15 percent of hydrogen peroxide relative to the absolute dry quantity of the cotton linter, the matching alkali liquid ratio of 1:3-5, 0.1-0.5 percent of oxidation bleaching stabilizing agent relative to the absolute dry quantity and 0.5-0.9 percent of penetrating agent relative to the absolute dry quantity; c) pulping and desanding: 1) carrying out Dutch type pulping with the current of 120A-140A; 2) fibrillating with the pulping current of 130A-160A; 3) then carrying out pulping with the puling pulping current of 270A-280A; 4) refining; and 5) desanding; and d) paper pulping. The production method adopts integrated pulping of low-temperature, low-alkali and chlorine-free boiling and bleaching, and improves boiling and bleaching effect by adding the oxidation bleaching stabilizing agent and an auxiliary agent of the penetrating agent; and the produced cotton pull has high whiteness, good strength and high folding endurance and can be used for producing the banknote paper.
Description
Technical field
The present invention relates to the Cotton Pulp production field, be specifically related to a kind of high-whiteness cotton pulp product for banknote paper and production method thereof.
Background technology
The banknote paper using is special 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, pound 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 gradually now cotton linter to substitute the combing machine noil and produces Cotton Pulp.
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.Preparing take cotton linter as raw material that Cotton Pulp uses on the products such as bank-note paper, cheque paper, passport paper, notarization document paper using is from now on only way.
At present in the international market, the cotton pulp product is most of be that viscose cotton pulp, manufacturing technique method adopt high temperature, high pressure, high-alkali conditions of cooking, and added value of product is low, in the production process, and waste water COD content height, treatment cost height.Application number is that 200710015037.1 Chinese patent " utilizes cotton linter to produce the method for high whiteness cotton pulp ", and the cotton pulp product whiteness of producing 〉=85% is high not enough, is not suitable for the production bank-note paper.
Summary of the invention
The problem that the present invention solves is to provide a kind of high-whiteness cotton pulp product for banknote paper and production method thereof, and the Cotton Pulp whiteness of production is high, is applicable to commercially produce bank-note paper.
In order to solve the problems of the technologies described above, technical scheme of the present invention is:
A kind of bank-note paper production method of high whiteness cotton pulp may further comprise the steps:
A) to the cotton linter opener, and carry out removal of impurities, squeezing, dipping;
B) cotton linter is boiled float, joining the alkali temperature is 80 ℃～90 ℃, it is dense in NaOH to join alkali alkali, the cotton linter oven-dry weight is 0.5%～10% relatively, hydrogen peroxide is 0.5%～15% 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 120A～140A;
2) fibrillating: the making beating electric current is 130A～160A;
3) will pull an oar through the slurry of fibrillating: the making beating Current Control is at 270A～290A;
4) defibrination;
5) desanding;
D) papermaking.
As preferably, described cotton linter is I class cotton linter and or II class cotton linter.
As preferably, maturity is that the percentage by weight of 65%～85% cotton linter is 10%～90% in the described I class cotton linter, and maturity is that the percentage by weight of 75%～85% cotton linter is 10%～90% in the described II class cotton linter.
As preferably, described 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 ℃～95 ℃, 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 ℃～100 ℃, be incubated 60 minutes for the second time～100 minutes, heated up for the third time 40 minutes～130 minutes, be warming up to 80 ℃～120 ℃, be incubated for the third time 20 minutes～80 minutes, then steam bleeding is finished to boil and is floated.
As preferably, described 1) during the holland type making beating, light cutter was discongested 10 minutes～60 minutes, and washing, concentrated is starched and densely is controlled at 3.0%～4.0%, beating time 90 minutes～120 minutes.
As preferably, described 2) beating time is 60 minutes～80 minutes during fibrillating, and starching dense is 3.5%～4.0%.
As preferably, described 3) be controlled at 1.8%～2.0% with the slurry when the slurry of fibrillating is pulled an oar is dense.
As preferably, described 4) power of defibrination is 340kW～380kW, starches densely to be controlled at 1.8%～2.0%.
As preferably, described 5) pressure of desanding is controlled at 2.8MPa～3.2MPa, starches densely to be controlled at 0.4%～0.6%.
As preferably, described d) papermaking comprises:
I) with slurry, concentration are controlled in 0.8%～1.2% scope;
II) papermaking, the pressure control range of papermaking 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
2The control of papermaking 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 high whiteness cotton pulp is by above-described production method preparation.
The bank-note paper provided by the invention production method of high whiteness cotton pulp, utilize cotton linter to be raw material, adopt low temperature, low alkali, boil bleaching integrated slurrying without chlorine, floating stabilizing agent, bleeding agent auxiliary agent by oxygenation promotes to boil and floats effect, the Cotton Pulp whiteness of producing is high, intensity is good, folding strength is high, can be used to produce Euro, pound bank-note paper, cheque paper, passport paper, notarization document paper using.
The specific embodiment
In order further to understand the present invention, below in conjunction with embodiment the preferred embodiment of the invention is described, but should be appreciated that these describe just as further specifying the features and advantages of the present invention, rather than to the restriction of claim of the present invention.
Embodiment 1:
A) to the cotton linter opener, and carry out removal of impurities, squeezing, dipping.Maturity is that the percentage by weight of 70% cotton linter is that maturity is that the percentage by weight of 75% cotton linter is 60% in 40%, the II class cotton linter in the used I class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, dust removing machine for fibres cotton linter is carried out removal of impurities, then by cyclone separator, through screw press, dipping.Removal of impurities can make cotton linter in process contained cotton seed hulls, cotton leaf be 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 the alkali-hydrogen peroxide digesting technoloy, disposable boiling, two processes of bleaching finished in boiling vessel, boil the process of floating and adopt three intensifications, three insulations, main purpose is to allow reaction condition relax, prevent that the rapid decomposition of hydrogen peroxide 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 82 ℃, it is dense in NaOH to join alkali alkali, the cotton linter oven-dry weight is 1.2% relatively, hydrogen peroxide is 3.6% with respect to the cotton linter oven-dry weight, joining lye ratio is 1: 4, namely the volume of NaOH and hydrogen peroxide and with the ratio of the weight of cotton linter be 1: 4, hydrogen peroxide bleaching stabilizer is 0.3% with respect to oven-dry weight, bleeding agent is delivered to through conveying worm after sufficiently mixing and is boiled bleaching integrated operation with respect to oven-dry weight 0.5%.Boil the hydrogen peroxide bleaching stabilizer and the bleeding agent that float the process use and produced by the U.S. prompt molecular material technology in east, Hefei Co., Ltd, by the reaction of the metal ion in hydrogen peroxide bleaching stabilizer and the material, reduce the decomposition of hydrogen peroxide, finish to boil and float the white needs that require of height; Make the NaOH energy in time and lignin reaction by 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 50 minutes for the first time, be warming up to 86 ℃, be incubated 60 minutes for the first time; Heated up 80 minutes for the second time, be warming up to 100 ℃, be incubated 90 minutes for the second time, heated up for the third time 70 minutes, be warming up to 110 ℃ of then steam bleedings, be incubated for the third time 65 minutes and finish to boil and float.The cotton linter that boils after floating is detected, and recording the degree of polymerization is 1500～2200.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 12 minutes, and washing, concentrated starch and densely is controlled at 3.3%, the electric current 123A that pulls an oar, beating time 100 minutes is finished and is discongested and brooming.
Record fibre length 3.7mm, 13 ° of SR of beating degree.
(2) fibrillating:
Slurry enters fibrillating after brooming, making beating electric current 138A, and beating time 75 minutes is starched densely 3.5%, finishes fibrillating.
(3) enter the steep-taper jordan through the slurry of fibrillating and pull an oar, the making beating Current Control is at 272A, starches densely to be controlled at 1.9%, finishes making beating.
Record fibre length 3.5mm, 14 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, the slurry after the making beating enters double disc refiner, and defibrination power 350KW starches and densely is controlled at 1.9%, finishes defibrination.
Survey fibre length 2.8mm, 16 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, desanding pressure is controlled at 2.9MPa, starch and densely be controlled at 0.4%,, one-level is taked 606 desanders, secondary is taked 600 desanding, and presses three sections flow process controls of secondary, will starch simmer down to 3.5% after the desanding.
D) papermaking
With slurry concentration is controlled in 0.8% scope.
Papermaking wet end and press section, pressure control range: wet end couch roll pressure 1.6kgf/cm
2, a pressure pressure is controlled at 2.6kgf/cm
2, two pressure pressures are controlled at 3.5kgf/cm
2
The control of papermaking drying section temperature: first group of dryer temperature is controlled at 103 ℃, second group of dryer temperature is controlled at 126 ℃, and the 3rd group of dryer temperature is controlled at 128 ℃, and the 4th group of dryer temperature is controlled at 106 ℃, thereby assurance pulp moisture is removed under temperate condition, does not affect the pulp whiteness.
Rear pulp deciding grade and level weight 623g/m manufactures paper with pulp
2, moisture 8.2% after the paper cutter section, utilizes the magma packing.
The indices of the product that makes is:
The pulp index is the degree of polymerization 1978 whiteness 91%
Folding strength 1200 moisture 8.8%
Irony 45PPM fibre length 3.0mm
Embodiment 2:
A) to the cotton linter opener, and carry out removal of impurities, squeezing, dipping.Maturity is that the percentage by weight of 80% cotton linter is that maturity is that the percentage by weight of 80% cotton linter is 45% in 55%, the II class cotton linter in the used I class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, dust removing machine for fibres cotton linter is carried out removal of impurities, then by cyclone separator, through screw press, dipping.
B) cotton linter is boiled float.
Joining the alkali temperature is 90 ℃, it is dense in NaOH to join alkali alkali, the cotton linter oven-dry weight is 5% relatively, hydrogen peroxide is 6% with respect to the cotton linter oven-dry weight, joining lye ratio is 1: 5, hydrogen peroxide bleaching stabilizer is 0.3% with respect to oven-dry weight, and bleeding agent is delivered to through conveying worm after sufficiently mixing and boiled bleaching integrated operation with respect to oven-dry weight 0.9%.
Boil to float in the rotary spherical digester and carry out, heated up 80 minutes for the first time, be warming up to 87 ℃, be incubated 75 minutes for the first time; Heated up 90 minutes for the second time, be warming up to 105 ℃, be incubated 90 minutes for the second time, heated up for the third time 65 minutes, be warming up to 110 ℃, be incubated for the third time 78 minutes and finish to boil and float.The cotton linter that boils after floating is detected, and recording the degree of polymerization is 1890.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 30 minutes, and washing, concentrated starch and densely is controlled at 3.5%, the electric current 140A that pulls an oar, beating time 100 minutes is finished and is discongested and brooming.
Record fibre length 3.4mm, 14.2 ° of SR of beating degree.
(2) fibrillating:
Slurry enters fibrillating after brooming, making beating electric current 140A, and beating time 60 minutes is starched densely 3.5%, finishes fibrillating.
(3) through the slurry of fibrillating, enter the steep-taper jordan and pull an oar, the making beating Current Control is starched and densely is controlled at 1.9% at 280A, finishes making beating.
Record fibre length 3.2mm, 15 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, the slurry after the making beating enters double disc refiner, and defibrination power 380KW starches and densely is controlled at 1.9%, finishes defibrination.
Record fibre length 2.6mm, 16 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, desanding pressure is controlled at 3.0MPa, starch and densely be controlled at 0.5%, one-level is taked 606 desanders, and secondary is taked 600 desanding, and press three sections flow process controls of secondary, will starch simmer down to 3.5% after the desanding.
D) papermaking
With slurry concentration is controlled in 0.9% scope.
Papermaking wet end and press section, pressure control range: wet end couch roll pressure 1.8kgf/cm
2, a pressure pressure is controlled at 3.0kgf/cm
2, two pressure pressures are controlled at 4.0kgf/cm
2
The control of papermaking drying section temperature: first group of dryer temperature is controlled at 105 ℃, second group of dryer temperature is controlled at 130 ℃, and the 3rd group of dryer temperature is controlled at 135 ℃, and the 4th group of dryer temperature is controlled at 103 ℃, thereby assurance pulp moisture is removed under temperate condition, does not affect the pulp whiteness.
Rear pulp deciding grade and level weight 612g/m manufactures paper with pulp
2, moisture 8.9% after the paper cutter section, utilizes the magma packing.
The indices of the product that makes is:
The pulp index is the degree of polymerization 1826 whiteness 91%
Folding strength 1500 moisture 8.9%
Irony 50PPM fibre length 2.6mm
Embodiment 3:
A) to the cotton linter opener, and carry out removal of impurities, squeezing, dipping.Maturity is that the percentage by weight of 75% cotton linter is that maturity is that the percentage by weight of 82% cotton linter is 30% in 70%, the II class cotton linter in the used I class cotton linter.Shredding becomes cotton-shaped to cotton linter to adopt opener, and with condensers, seven roller de-burring machines, dust removing machine for fibres cotton linter is carried out removal of impurities, then by cyclone separator, through screw press, dipping.
B) cotton linter is boiled float.
Joining the alkali temperature is 83 ℃, it is dense in NaOH to join alkali alkali, the cotton linter oven-dry weight is 6% relatively, hydrogen peroxide is 10% with respect to the cotton linter oven-dry weight, joining lye ratio is 1: 4, hydrogen peroxide bleaching stabilizer is 0.5% with respect to oven-dry weight, and bleeding agent is delivered to through conveying worm after sufficiently mixing and boiled bleaching integrated operation with respect to oven-dry weight 0.8%.
Boil to float in the rotary spherical digester and carry out, heated up 75 minutes for the first time, be warming up to 92 ℃, be incubated 75 minutes for the first time; Heated up 100 minutes for the second time, be warming up to 105 ℃, be incubated 97 minutes for the second time, heated up for the third time 80 minutes, be warming up to 118 ℃ of then steam bleedings, be incubated for the third time 80 minutes, then steam bleeding is finished to boil and is floated.The cotton linter that boils after floating is detected, and recording the degree of polymerization is 1900.
C) making beating desanding.
(1) slurry discongest, brooming:
Employing hollander making beating, light cutter was discongested 60 minutes, and washing, concentrated starch and densely is controlled at 3.8%, the electric current 135A that pulls an oar, beating time 120 minutes is finished and is discongested and brooming.
Survey fibre length 3.6mm, 14.1 ° of SR of beating degree.
(2) fibrillating:
Slurry enters for the first time fibrillating after brooming, making beating electric current 145A, and beating time 80 minutes is starched densely 3.5%, finishes fibrillating.
(3) through the slurry of fibrillating, enter the steep-taper jordan and pull an oar, the making beating Current Control is starched and densely is controlled at 1.8% at 280A, finishes making beating.
Record fibre length 3.0mm, 14.5 ° of SR of beating degree.
(4) defibrination: further promote for making beating degree, the slurry after the making beating enters double disc refiner, and defibrination power 360KW starches and densely is controlled at 1.8%, finishes defibrination.
Record fibre length 2.7mm, 15.1 ° of SR of beating degree.
(5) desanding: will pull an oar and defibrination after slurry, send into the desanding operation, desanding pressure is controlled at 3.0MPa, starch and densely be controlled at 0.6%,, one-level is taked 606 desanders, secondary is taked 600 desanding, and presses three sections flow process controls of secondary, will starch simmer down to 3.5% after the desanding.
D) papermaking
With slurry concentration is controlled in 1.0% scope.
Papermaking wet end and press section, pressure control range: wet end couch roll pressure 2.2kgf/cm
2, a pressure pressure is controlled at 2.1kgf/cm
2, two pressure pressures are controlled at 3.8kgf/cm
2
The control of papermaking drying section temperature: first group of dryer temperature is controlled at 105 ℃, second group of dryer temperature is controlled at 130 ℃, and the 3rd group of dryer temperature is controlled at 128 ℃, and the 4th group of dryer temperature is controlled at 108 ℃, thereby assurance pulp moisture is removed under temperate condition, does not affect the pulp whiteness.
Rear pulp deciding grade and level weight 678g/m manufactures paper with pulp
2, moisture 9.3% after the paper cutter section, utilizes the magma packing.
The indices of the product that makes is:
The pulp index is the degree of polymerization 1900 whiteness 92%
Folding strength 1556 moisture 9.3%
Irony 45PPM fibre length 2.7mm
More than a kind of high-whiteness cotton pulp product for banknote paper provided by the present invention and production method thereof are described in detail.Used specific case herein 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 (10)
1. the production method of a bank-note paper usefulness high whiteness cotton pulp is characterized in that, may further comprise the steps:
A) to the cotton linter opener, and carry out removal of impurities, squeezing, dipping;
B) cotton linter is boiled float, joining the alkali temperature is 80 ℃～90 ℃, it is dense in NaOH to join alkali alkali, the cotton linter oven-dry weight is 0.5%～10% relatively, hydrogen peroxide is 0.5%～15% 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%;
Described 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 ℃～95 ℃, 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 ℃～100 ℃, be incubated 60 minutes for the second time～100 minutes, heated up for the third time 40 minutes～130 minutes, be warming up to 80 ℃～120 ℃, be incubated for the third time 20 minutes～80 minutes; Then steam bleeding is finished to boil and is floated;
C) making beating desanding comprises:
1) slurry discongest, brooming: holland type making beating, making beating electric current 120A～140A;
2) fibrillating: the making beating electric current is 130A～160A;
3) will pull an oar through the slurry of fibrillating: the making beating Current Control is at 270A～290A;
4) defibrination;
5) desanding;
D) papermaking.
2. production method according to claim 1 is characterized in that, described cotton linter is I class cotton linter and/or II class cotton linter.
3. production method according to claim 2, it is characterized in that, maturity is that the percentage by weight of 65%～85% cotton linter is 10%～90% in the described I class cotton linter, and maturity is that the percentage by weight of 75%～85% cotton linter is 10%～90% in the described II class cotton linter.
4. production method according to claim 1 is characterized in that, described 1) during the holland type making beating, light cutter was discongested 10 minutes～60 minutes, and washing, concentrated is starched and densely is controlled at 3.0%～4.0%, beating time 90 minutes～120 minutes.
5. production method according to claim 1 is characterized in that, described 2) beating time is 60 minutes～80 minutes during fibrillating, and starching dense is 3.5%～4.0%.
6. production method according to claim 1 is characterized in that, described 3) be controlled at 1.8%～2.0% with the slurry when the slurry of fibrillating is pulled an oar is dense.
7. production method according to claim 1 is characterized in that, described 4) power of defibrination is 340kW～380kW, starches densely to be controlled at 1.8%～2.0%.
8. production method according to claim 1 is characterized in that, described 5) pressure of desanding is controlled at 2.8MPa～3.2MPa, starches densely to be controlled at 0.4%～0.6%.
9. production method according to claim 1 is characterized in that, described d) papermaking comprises:
I) with slurry, concentration are controlled in 0.8%～1.2% scope;
II) papermaking, the pressure control range of papermaking 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
2The control of papermaking 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 ℃.
10. a bank-note paper high whiteness cotton pulp is characterized in that, by each described production method preparation in the claim 1 to 9.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010534617 CN101967764B (en) | 2010-11-05 | 2010-11-05 | High-whiteness cotton pulp product for banknote paper and production method thereof |
Applications Claiming Priority (1)
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| CN102535239A (en) * | 2012-02-29 | 2012-07-04 | 安徽雪龙纤维科技股份有限公司 | Refined cotton and production method thereof |
| CN103103842A (en) * | 2012-12-14 | 2013-05-15 | 中冶美利纸业股份有限公司 | Pulping method for waste Renminbi |
| 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 |
| CN109778580B (en) * | 2019-01-31 | 2022-01-21 | 山东银鹰股份有限公司 | Preparation method of cotton pulp for high-strength filter paper |
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| CN1718917A (en) * | 2004-07-09 | 2006-01-11 | 周家贵 | Production technology of extra low viscose refined cotton |
| CN101105012A (en) * | 2007-06-14 | 2008-01-16 | 山东海龙股份有限公司 | Method for producing high whiteness cotton pulp by using cotton linter |
| CN101130934A (en) * | 2006-08-26 | 2008-02-27 | 山东海龙股份有限公司 | Colored cotton linter pulp used for producing viscose fiber and method for making the same |
| CN101302725A (en) * | 2008-06-10 | 2008-11-12 | 山东银鹰化纤有限公司 | Process for producing cotton dissolving pulp |
| CN101328695A (en) * | 2008-06-10 | 2008-12-24 | 山东银鹰化纤有限公司 | Production process of cotton pulp for manufacturing automobile oil-gas filter parer |
| 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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| CN1718917A (en) * | 2004-07-09 | 2006-01-11 | 周家贵 | Production technology of extra low viscose refined cotton |
| CN101130934A (en) * | 2006-08-26 | 2008-02-27 | 山东海龙股份有限公司 | Colored cotton linter pulp used for producing viscose fiber and method for making the same |
| CN101105012A (en) * | 2007-06-14 | 2008-01-16 | 山东海龙股份有限公司 | Method for producing high whiteness cotton pulp by using cotton linter |
| CN101302725A (en) * | 2008-06-10 | 2008-11-12 | 山东银鹰化纤有限公司 | Process for producing cotton dissolving pulp |
| CN101328695A (en) * | 2008-06-10 | 2008-12-24 | 山东银鹰化纤有限公司 | Production process of cotton pulp for manufacturing automobile oil-gas filter parer |
| 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-whiteness cotton pulp product for banknote paper and production method thereof Effective date of registration: 20200317 Granted publication date: 20130403 Pledgee: Suzhou SME financing Company limited by guarantee Pledgor: ANHUI SNOW DRAGON FIBRE TECHNOLOGY Co.,Ltd. Registration number: Y2020340000010 |
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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. |