CN100593048C - Process for producing cotton dissolving pulp - Google Patents
Process for producing cotton dissolving pulp Download PDFInfo
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- CN100593048C CN100593048C CN200810016759A CN200810016759A CN100593048C CN 100593048 C CN100593048 C CN 100593048C CN 200810016759 A CN200810016759 A CN 200810016759A CN 200810016759 A CN200810016759 A CN 200810016759A CN 100593048 C CN100593048 C CN 100593048C
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Abstract
The invention relates to a production technique of a dissolved cotton pulp, in particular to a production technique that utilizes the raw material of cotton linters and adopts simple techniques to produce the dissolved cotton pulp with even fiber length, high fibrillation degree, good intensity, less water soluble substances, high methylcellulose content, stable polymerization degree and less dust, has low COD discharge in waste water, and lowers environmental pollution. The dissolved cotton pulp produced by the production technique is mainly used for producing paper that is used for wiping upper-scale precise instruments, steel paper that is used for precise machining, a novel medicine loading agent of microcrystalline cellulose, explosive nitrocellulose, high-level nitrolacquer and building coating materials, etc.
Description
Technical field
The present invention relates to a kind of process for producing cotton dissolving pulp, relate in particular to a kind of cotton linter that utilizes and be raw material, produce cotton pulp dregs of rice technology, be mainly used to produce high-grade precision instrument wiping paper, accurate machined vulcan fibre, medical novel filler one microcrystalline cellulose and explosive nitrocotton and high-grade lacquer and building coating.
Background technology
In recent years, in the international market, it is strong to make explosive force, and the company of industries such as the nitrocotton of the explosive that active force is big and medical new drug extender also constantly increases this product consumption, is an advantageous conditions for this product of exploitation.
China produces cotton big country, has abundant cotton linter resource.In Xinjiang, high quality cotton producing regions such as Hebei, Shandong, Jiangsu, have the raw material of sufficient high-quality to guarantee.In the market, most is raw material with the cotton linter, produces the viscose cotton pulp, and process is by carrying out boiling under the high-alkali condition of high temperature, high-temperature bleaching, and added value of product is low, and production process produces waste water COD content height, is difficult to improvement.Be the feedstock production cotton pulp dregs of rice with the cotton linter wherein, be applied to high-grade precision instrument wiping, on market, also belong to blank with on paper, vulcan fibre, medical novel filler and the industries such as explosive nitrocotton and high-grade paint.
In the existing common production cotton pulp technology bleaching process, use clorox and chlorine to carry out multistage bleaching to cotton pulp, fiber is caused damage, fibre strength descends.And there is the high pollution wastewater problem that is difficult to administer in pulping process waste discharge COD content about 45000mg/l.
Chinese patent, application number are " 2007100150371 ", and a disclosed key name is called " utilizing cotton linter to produce the method for high whiteness cotton pulp ", are raw material with the cotton linter in the method, produce high whiteness cotton pulp, can only be used for the raw material of chemical fibre as textile industry.
Chinese patent, application number is: " 2006100684849 ", a disclosed key name is called " a kind of cotton pulp with high-degree of polymerization and preparation method thereof ", with the cotton linter is raw material, produce the cotton pulp dregs of rice of high polymerization degree, fibre length and freedom are not controlled, by the end product quality index, the degree of polymerization reaches 800-2800, can only be used for viscose and low-grade industries such as TYLOSE 30000.
Chinese patent, application number is: " 2006100684834 ", a disclosed key name is called " being used to make cellulose ether-esters low-viscosity cotton pulp and preparation method thereof ", with the cotton linter is raw material, produce the low viscous cotton pulp dregs of rice, by the end product quality index, the degree of polymerization only reaches 50-400, and these cotton pulp dregs of rice can only be used for making low sticking, low grade cellulose ether-esters and microcrystalline cellulose.
Summary of the invention
The purpose of this invention is to provide a kind of process for producing cotton dissolving pulp, solved problems of the prior art, this technology waste discharge COD content is low, has reduced the pollution to environment; And the fine content height of its first of the cotton pulp dregs of rice that invented technology is produced, stable polymerization degree, fibre length homogeneous, the characteristics that freedom is fit to, dust is few.
For solving above technical problem, technical scheme of the present invention is to utilize cotton linter to be raw material, produces a kind of technology of the cotton pulp dregs of rice, may further comprise the steps:
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 85%-95% of two class one-level maturity 79-81% and the cotton linter amount 5%-15% of three class one-level maturity 78-79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled between 68-72 ℃, is 16%-17% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4-4.5, the relative oven dry stock amount of HY-PA bleeding agent is 0.45-0.5%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, in boiling vessel, carry out, heat up temperature 115-120 ℃ for the first time, behind the 22-27min that heats up for the first time, carry out the steam bleeding 15min first time, for the second time heat up temperature 143-145 ℃ again, behind the 18-20min that heats up for the second time, steam bleeding 10min for the second time, heating-up time is controlled at 22-27min for the third time again, after temperature reached 168-172 ℃, temperature retention time 110-130min finished boiling;
Survey: degree of polymerization 800-950;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches the dense 0.4-0.6% that is controlled at, and after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 260-290A, and slurry concentration is controlled at 1.5-1.9%, finishes once making beating,
Survey: freedom 730-740ML fibre length is represented with the Bauer screening ,+14 order 59-68%,
B, once after the making beating, carry out second time making beating, Current Control is at 280-320A, and slurry concentration is controlled at 1.5-1.9%,, finish pull an oar for the second time after,
Survey: freedom 719-729ML fibre length is represented with the Bauer screening ,+14 order 50-58%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 290-330A, and slurry concentration is controlled at 1.5-1.9%, finishes making beating for the third time,
Survey: freedom 700-718ML fibre length is represented with the Bauer screening ,+14 order 42-49%,
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.4-0.6%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.4-0.5%, and temperature is controlled at 68-72 ℃, and the time is controlled at 90-120min; Change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide respectively is 3-4%, the relative oven dry stock amount of NaOH is 2-2.5%, the relative oven dry stock amount of magnesium sulfate is 2.0-2.5%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.17-0.22%, temperature is controlled at 68-72 ℃, and behind the 100-110min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.3-2.7%, and the relative oven dry stock amount of oxalic acid is 0.22-0.27%, and acid treatment 40-50min washed 2-3 hour again;
The mass metering index:
The degree of polymerization: 690-750, irony :≤25ppm, whiteness: 〉=87%, ash :≤0.15%;
(8) back desanding: the cotton pulp after acid treatment, washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches the dense 0.6%-0.8% that is controlled at, and after the back desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 240-280A, and slurry concentration is controlled at 2.0-3.0%, and the back making beating is finished;
Survey: freedom 680-700ML, fibre length is with Bauer screening expression ,+14 order 35-42%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 320-380A, and slurry concentration is controlled at 2.0-3.0%, behind the defibrination;
Survey: fibre length is with Bauer screening expression ,+14 order 20-35%, freedom 650-680ML;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Among the present invention, raw material is paid attention to choosing:
1) require cotton linter that higher maturity is arranged, the fine content height of its first is given security for the high cellulose content product simultaneously;
2) cotton linter is pure, does not contain heterotypic fibre, and the sulfuric acid insoluble matter will lack.The sulfuric acid insoluble matter not only will consume part alkali in digestion process, make the chemical reaction heterogeneity in the whole digestion process, cause the half stuff quality heterogeneity after the boiling, the existence of sulfuric acid insoluble matter simultaneously causes sharp dust degree to increase, the cotton linter of other the insoluble object height of sulfuric acid, very easily when boiling, decompose a large amount of pigments, in bleaching process, influence whiteness and improve;
3) the cotton linter color and luster is pure, and color and luster is dim or have variegated cotton linter also can influence whiteness.
In the inventive method, in the preceding pulping process, by using three making beating of big tapering jordan, double disc refiner, and strict control process index, effectively controlling fiber length and freedom.
In the technology of the present invention, cooking process, by three intensifications, the little steam bleeding of secondary, along with variations in temperature, cellulosic degradation speed is accelerated in the cotton linter, simultaneously with the stripping of most of water-soluble substances with low branch subbundle.In boiling, what at first react is materials such as oligosaccharides and lignin, is used by adding bleeding agent and NaOH, the water-soluble substances dissolution rate is accelerated, make alkali lye fully be penetrated into fibrous inside, can help cellulosic refining purification, the degree of polymerization is effectively controlled.
In the bleaching process, by adding the discoloration of chlorine dioxide, only and lignin generation oxidative degradation, fibre damage is little, the fibre strength height, and the pulping yield height avoids producing carcinogenic noxious materials such as bioxin and organohalogen compounds in reacting simultaneously.
By adding diethylene triamine pentacetic acid (DTPA), can be beneficial to the stripping and the removal of transition metal ionss such as accelerating manganese, iron, copper, improve whiteness more than 5%, avoid the hydrogen peroxide effective ingredient to lose efficacy simultaneously.
The present invention adopts simple process, with the cotton linter is raw material, whole pulping process waste water COD discharge capacity is at 27000-30000mg/l, reduced pollution to environment, the cotton pulp dregs of rice fibre length of this explained hereafter is even, brooming degree height, intensity are good, and the hydrotrope is few, the fine content height of first, stable polymerization degree, dust is few, can better be used to produce high-grade precision instrument wiping paper, accurate machined vulcan fibre, medical novel filler-microcrystalline cellulose and explosive nitrocotton and industries such as high-grade lacquer and building coating.
Its finished product leading indicator is as follows:
| The degree of polymerization | 720-760 | Whiteness: | ≥88％ |
| Irony | ≤10ppm | The first fibre | ≥98.5％ |
| Ash | ≤0.07％ | Moisture content | 10±1.5％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 20-35％ | Little dust 0.05-3.0mm 2 | ≤15mm 2/500g |
| Freedom | 650-680ML |
Specific embodiment
The present invention will be further described below in conjunction with embodiment:
Embodiment 1
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 85% of two class one-level maturity 80% and the cotton linter amount 15% of three class one-level maturity 79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled at 68 ℃, is 16% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4, the relative oven dry stock amount of HY-PA bleeding agent is 0.45%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, 115 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 22min, carry out the steam bleeding 15min first time, 143 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 18min, steam bleeding 10min for the second time, the heating-up time is controlled at 22min for the third time again, after temperature reaches 168 ℃, temperature retention time 110min finishes boiling;
Survey: the degree of polymerization 946;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches densely to be controlled at 0.4%, after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 260A, and slurry concentration is controlled at 1.5%, finishes once making beating,
Survey: freedom 740ML, fibre length is represented with the Bauer screening ,+14 orders 68%,
B, once after the making beating, carry out second time making beating, Current Control is at 280A, and slurry concentration is controlled at 1.5%,, finish pull an oar for the second time after,
Survey: freedom 729ML, fibre length is represented with the Bauer screening ,+14 orders 58%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 330A, and slurry concentration is controlled at 1.5%, finishes making beating for the third time,
Survey: freedom 718ML, fibre length is represented with the Bauer screening ,+14 orders 49%,
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.4%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.4%, temperature is controlled at 68 ℃, behind the 90min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3%, the relative oven dry stock amount of NaOH is 2%, the relative oven dry stock amount of magnesium sulfate is 2.0%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.17%, and temperature is controlled at 68 ℃, behind the 100min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.3%, and the relative oven dry stock amount of oxalic acid is 0.22%, and acid treatment 40min washed 2 hours again;
Survey: leading indicator:
The degree of polymerization: 753, irony: 19ppm, whiteness: 80%, ash: 0.14%;
(8) back desanding: acid treatment, the cotton pulp after the washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches densely to be controlled at 0.6%, after the back desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 240A, and slurry concentration is controlled at 2.0%, making beating after finishing;
Survey: freedom 700ML, fibre length is represented with the Bauer screening ,+14 orders 42%,
(10) defibrination changes double disc refiner again over to, and Current Control is at 380A, and slurry concentration is controlled at 2.0%, finishes defibrination;
Survey: freedom 680ML, fibre length is represented with the Bauer screening ,+14 orders 35%,
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 750 | Whiteness: | 88.3％ |
| Irony | 9ppm | The first fibre | 99.5％ |
| Ash | 0.07％ | Moisture content | 10.5％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 35％ | Little dust 0.05-3.0mm 2 | 13mm 2/500g |
| Freedom | 680ML |
Survey: waste water COD discharging content is at 27010mg/l in this implementing process.
Embodiment 2
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 85% of two class one-level maturity 80% and the cotton linter amount 15% of three class one-level maturity 79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled at 69 ℃, is 16.5%% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.1, the relative oven dry stock amount of HY-PA bleeding agent is 0.46%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, 116 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 23min, carry out the steam bleeding 15min first time, 144 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 19min, steam bleeding 10min for the second time, the heating-up time is controlled at 23min for the third time again, after temperature reaches 169 ℃, temperature retention time 112min finishes boiling;
Survey: the degree of polymerization 928;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches densely to be controlled at 0.45%, after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 265A, and slurry concentration is controlled at 1.55%, finishes once making beating,
Survey: freedom 738ML, fibre length is represented with the Bauer screening ,+14 orders 67%,
B, once after the making beating, carry out second time making beating, Current Control is at 285A, and slurry concentration is controlled at 1.55%,, finish pull an oar for the second time after,
Survey: freedom 728ML, fibre length is represented with the Bauer screening ,+14 orders 57%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 325A, and slurry concentration is controlled at 1.55%, finishes making beating for the third time,
Survey: freedom 714ML, fibre length is represented with the Bauer screening ,+14 orders 48%,
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.43%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.42%, temperature is controlled at 69 ℃, time 95min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3.2%, the relative oven dry stock amount of NaOH is 2.1%, the relative oven dry stock amount of magnesium sulfate is 2.1%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.18%, and temperature is controlled at 69 ℃, time 102min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.4%, and the relative oven dry stock amount of oxalic acid is 0.23%, and acid treatment 42min washed 2.4 hours again;
Survey: the degree of polymerization: 744, irony: 18ppm, whiteness: 80.7%, ash: 0.12%;
(8) back desanding: acid treatment, the cotton pulp after the washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches densely to be controlled at 0.7%, after the back desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 245A, and slurry concentration is controlled at 2.1%, making beating after finishing;
Survey: freedom 696ML, fibre length is with Bauer screening expression ,+14 orders 41%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 370A, and slurry concentration is controlled at 2.1%, finishes defibrination;
Survey: freedom 675ML, fibre length is with Bauer screening expression ,+14 orders 33%;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 741 | Whiteness: | 88.7％ |
| Irony | 8ppm | The first fibre | 99.2％ |
| Ash | 0.06％ | Moisture content | 8.7％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 33％ | Little dust 0.05-3.0mm 2 | 13mm 2/500g |
| Freedom | 675ML |
Survey: waste water COD discharging content is at 27530mg/l in this implementing process.
Embodiment 3
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 90% of two class one-level maturity 79% and the cotton linter amount 10% of three class one-level maturity 79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled at 70 ℃, is 16.8% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.3, the relative oven dry stock amount of HY-PA bleeding agent is 0.49%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, 117 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 23min, carry out the steam bleeding 15min first time, 145 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 20min, steam bleeding 10min for the second time, the heating-up time is controlled at 24min for the third time again, after temperature reaches 170 ℃, temperature retention time 120min finishes boiling;
Survey: the degree of polymerization 912;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches densely to be controlled at 0.5%, after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 270A, and slurry concentration is controlled at 1.6%, finishes once making beating,
Survey: freedom 737ML, fibre length is represented with the Bauer screening ,+14 orders 66%,
B, once after the making beating, carry out second time making beating, Current Control is at 288A, and slurry concentration is controlled at 1.6%,, finish pull an oar for the second time after,
Survey: freedom 726ML, fibre length is represented with the Bauer screening ,+14 orders 55%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 320A, and slurry concentration is controlled at 1.6%, finishes making beating for the third time,
Survey: freedom 713ML, fibre length is with Bauer screening expression ,+14 orders 47%;
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.55%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.5%, temperature is controlled at 70 ℃, time 100min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3.6%, the relative oven dry stock amount of NaOH is 2.4%, the relative oven dry stock amount of magnesium sulfate is 2.3%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.19%, and temperature is controlled at 70 ℃, time 107min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.5%, and the relative oven dry stock amount of oxalic acid is 0.25%, and acid treatment 48min washed 2.5 hours again;
Survey: the degree of polymerization: 736, irony: 16ppm, whiteness: 80.7%, ash: 0.12%;
(8) back desanding: acid treatment, the cotton pulp after the washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches densely to be controlled at 0.7%, after the desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 250A, and slurry concentration is controlled at 2.3%, finishes making beating,
Survey: freedom 693ML, fibre length is with Bauer screening expression ,+14 orders 40%;
(10) defibrination changes double disc refiner again over to, and power is controlled at 201KW, and slurry concentration is controlled at 2.3%, finishes defibrination;
Survey: freedom 672ML, fibre length is with Bauer screening expression ,+14 orders 32%;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 732 | Whiteness: | 89.2％ |
| Irony | 8ppm | The first fibre | 99.1％ |
| Ash | 0.05％ | Moisture content | 9.8％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 32％ | Little dust 0.05-3.0mm 2 | 12mm 2/500g |
| Freedom | 672ML |
Survey: waste water COD discharging content is at 27650mg/l in this implementing process.
Embodiment 4
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 90% of two class one-level maturity 79% and the cotton linter amount 10% of three class one-level maturity 79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled at 71 ℃, is 16.8% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.4, the relative oven dry stock amount of HY-PA bleeding agent is 0.47%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, 119 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 26min, carry out the steam bleeding 15min first time, 144 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 20min, steam bleeding 10min for the second time, the heating-up time is controlled at 26min for the third time again, after temperature reaches 171 ℃, temperature retention time 125min finishes boiling;
Survey: the degree of polymerization 883;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches densely to be controlled at 0.55%, after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating,
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 275A, and slurry concentration is controlled at 1.7%, finishes once making beating,
Survey: freedom 736ML, fibre length is represented with the Bauer screening ,+14 orders 65%,
B, once after the making beating, carry out second time making beating, Current Control is at 290A, and slurry concentration is controlled at 1.7%,, finish pull an oar for the second time after,
Survey: freedom 724ML, fibre length is represented with the Bauer screening ,+14 orders 53%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 315A, and slurry concentration is controlled at 1.7%, finishes making beating for the third time,
Survey: freedom 710ML, fibre length is with Bauer screening expression ,+14 orders 45%;
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.5%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.46%, temperature is controlled at 71 ℃, time 116min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3.6%, the relative oven dry stock amount of NaOH is 2.5%, the relative oven dry stock amount of magnesium sulfate is 2.4%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.20%, and temperature is controlled at 71 ℃, time 113min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.5%, and the relative oven dry stock amount of oxalic acid is 0.26%, and acid treatment 48min washed 2.8 hours again;
Survey: the degree of polymerization: 731, irony: 16ppm, whiteness: 81.2%, ash: 0.11%;
(8) back desanding: acid treatment, the cotton pulp after the washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches densely to be controlled at 0.72%, after the desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 255A, and slurry concentration is controlled at 2.5%, finishes making beating;
Survey: freedom 690ML, fibre length is with Bauer screening expression ,+14 orders 39%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 350A, and slurry concentration is controlled at 2.5%, finishes defibrination;
Survey: freedom 669ML, fibre length is with Bauer screening expression ,+14 orders 30%;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 729 | Whiteness: | 89.4％ |
| Irony | 6ppm | The first fibre | ≥98.9％ |
| Ash | 0.05％ | Moisture content | 10.2％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 30％ | Little dust 0.05-3.0mm 2 | 10mm 2/500g |
| Freedom | 669ML |
Survey: waste water COD discharging content is at 27000mg/l in this implementing process.
Embodiment 5
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 85% of two class one-level maturity 81% and the cotton linter amount 15% of three class one-level maturity 78%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled at 72 ℃, is 17% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.5, the relative oven dry stock amount of HY-PA bleeding agent is 0.5%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, 120 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 27min, carry out the steam bleeding 15min first time, 145 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 20min, steam bleeding 10min for the second time, the heating-up time is controlled at 27min for the third time again, after temperature reaches 172 ℃, temperature retention time 130min finishes boiling;
Survey: the degree of polymerization 876;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3Mpa, starches densely to be controlled at 0.6%, after the desanding, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 280A, and slurry concentration is controlled at 1.8%, finishes once making beating,
Survey: freedom 735ML, fibre length is represented with the Bauer screening ,+14 orders 64%,
B, once after the making beating, carry out second time making beating, Current Control is at 295A, and slurry concentration is controlled at 1.8%,, finish pull an oar for the second time after,
Survey: freedom 723ML, fibre length is represented with the Bauer screening ,+14 orders 52%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 310A, and slurry concentration is controlled at 1.8%, finishes making beating for the third time,
Survey: freedom 708ML, fibre length is represented with the Bauer screening ,+14 orders 44%,
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.6%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.5%, temperature is controlled at 72 ℃, time 120min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 4%, the relative oven dry stock amount of NaOH is 2.5%, the relative oven dry stock amount of magnesium sulfate is 2.5%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.22%, and temperature is controlled at 72 ℃, time 110min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.7%, and the relative oven dry stock amount of oxalic acid is 0.27%, and acid treatment 50min washed 3 hours again;
Survey: the degree of polymerization: 726, irony: 12ppm, whiteness: 81.3%, ash: 0.11%;
(8) back desanding: acid treatment, the cotton pulp after the washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3Mpa, starches densely to be controlled at 0.8%, after the desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 260A, and slurry concentration is controlled at 2.7%, finishes making beating;
Survey: freedom 688ML, fibre length is with Bauer screening expression ,+14 orders 38%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 340A, and slurry concentration is controlled at 2.7%, finishes defibrination;
Survey: freedom 665ML, fibre length is with Bauer screening expression ,+14 orders 29%;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 723 | Whiteness: | 89.6％ |
| Irony | 6ppm | The first fibre | 98.7％ |
| Ash | 0.05％ | Moisture content | 8.3％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 29％ | Little dust 0.05-3.0mm 2 | 8mm 2/500g |
| Freedom | 665ML |
Survey: waste water COD discharging content is at 27500mg/l in this implementing process.
Embodiment 6
The processing step that present embodiment adopted is consistent with embodiment 1,
(1) chooses the cotton linter amount 85% of two class one-level maturity 81% and the cotton linter amount 15% of three class one-level maturity 78%;
(2) joining the alkali temperature and be controlled at 69 ℃, is 16.6% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.3, and the relative oven dry stock amount of HY-PA bleeding agent is 0.49%;
(3) boiling, 119 ℃ of the temperature that heats up for the first time, heat up for the first time behind the 26min, carry out the steam bleeding 15min first time, 144 ℃ of the temperature that heats up for the second time again, heat up the second time behind the 19min, steam bleeding 10min for the second time, the heating-up time is controlled at 27min for the third time again, after temperature reaches 171 ℃, temperature retention time 127min finishes boiling;
(5) preceding making beating:
A, big tapering jordan, the Current Control of once pulling an oar are at 285A, and slurry concentration is controlled at 1.75%;
Survey: freedom 734ML, fibre length is with Bauer screening expression ,+14 orders 63%;
B, making beating for the second time, Current Control are at 300A, and slurry concentration is controlled at 1.75%,
Survey: freedom 720ML, fibre length is represented with the Bauer screening ,+14 orders 50%,
C, making beating for the third time, Current Control are at 300A, and slurry concentration is controlled at 1.75%,
Survey: freedom 706ML, fibre length is represented with the Bauer screening ,+14 orders 43%,
(6) bleaching: in first bleaching tower, the relative oven dry stock amount of chlorine dioxide is 0.51%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.43%, and temperature is controlled at 70 ℃, time 112min, change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3.6%, and the relative oven dry stock amount of NaOH is 2.3%, the relative oven dry stock amount of magnesium sulfate is 2.5%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.18%, and temperature is controlled at 70 ℃, time 104min;
(7) acid treatment: the relative oven dry stock amount of hydrochloric acid is 2.6%, and the relative oven dry stock amount of oxalic acid is 0.25%, and acid treatment 47min washed 2.7 hours;
(9) back making beating, through big tapering jordan, Current Control is at 260A, and slurry concentration is controlled at 2.8%, finishes making beating;
Survey: freedom 684ML, fibre length is with Bauer screening expression ,+14 orders 35%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 340A, and slurry concentration is controlled at 2.8%, finishes defibrination;
Survey: freedom 660ML, fibre length is with Bauer screening expression ,+14 orders 27%;
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 724 | Whiteness: | 89.7％ |
| Irony | 6ppm | The first fibre | 98.5％ |
| Ash | 0.05％ | Moisture content | 10.8％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 27％ | Little dust 0.05-3.0mm 2 | 8mm 2/500g |
| Freedom | 660ML |
Survey: waste water COD discharging content is at 27840mg/l in this implementing process.
Embodiment 7
The processing step that present embodiment adopted is consistent with embodiment 1,
(2) in joining alkali, dipping operation: joining the alkali temperature and be controlled at 72 ℃, is 16.5% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4.3, and the relative oven dry stock amount of the saturating agent of HY-PA is 0.48%;
(5) preceding making beating:
A, once pull an oar Current Control at 290A, slurry concentration is controlled at 1.9%;
B, making beating for the second time, Current Control are at 310A, and slurry concentration is controlled at 1.9%,
C, making beating for the third time, Current Control are at 295A, and slurry concentration is controlled at 1.9%,
(6) bleaching, in first bleaching tower, the relative oven dry stock amount of chlorine dioxide is 0.49%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.45%, temperature is controlled at 70 ℃, and time 115min changes second bleaching tower over to after the washing, adding the relative oven dry stock amount of hydrogen peroxide more respectively is 3.7%, the relative oven dry stock amount of NaOH is 2.6%, and the relative oven dry stock amount of magnesium sulfate is 2.5%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.21%, temperature is controlled at 70 ℃, time 114min;
(9) back making beating, through big tapering jordan, Current Control is at 260A, and slurry concentration is controlled at 3.0%, finishes making beating;
Survey: freedom 679ML, fibre length is with Bauer screening expression ,+14 orders 32%
(10) defibrination changes double disc refiner again over to, and Current Control is at 340A, and slurry concentration is controlled at 3.0%, finishes defibrination;
Survey: freedom 654ML, fibre length is with Bauer screening expression ,+14 orders 25%;
Adopt the foregoing description gained cotton pulp dregs of rice leading indicator as follows:
| The degree of polymerization | 722 | Whiteness: | 89.8％ |
| Irony | 5ppm | The first fibre | 98.5％ |
| Ash | 0.05％ | Moisture content | 11.2％ |
| Fibre length (with Bauer screening expression ,+14 orders) | 25％ | Little dust 0.05-3.0mm 2 | 9mm 2/500g |
| Freedom | 654ML |
Survey: waste water COD discharging content is at 28000mg/l in this implementing process.
Claims (1)
1, a kind of process for producing cotton dissolving pulp is characterized in that: this technology may further comprise the steps:
(1) selects materials, opener, dry method removal of impurities: choose the cotton linter amount 85%-95% of two class one-level maturity 79-81% and the cotton linter amount 5%-15% of three class one-level maturity 78-79%, adopt opener that cotton linter is torn, and carry out selected removal of impurities with de-burring machine, deliver to screw press, dipping by cyclone separator then;
(2) join alkali, dipping: joining the alkali temperature and be controlled between 68-72 ℃, is 16%-17% in the relative oven dry stock amount of NaOH, joins lye ratio 1: 4-4.5, the relative oven dry stock amount of HY-PA bleeding agent is 0.45-0.5%, through screw extrusion, fully permeate with cotton linter and to mix, through helical feed to cooking process;
(3) boiling, in boiling vessel, carry out, heat up temperature 115-120 ℃ for the first time, behind the 22-27min that heats up for the first time, carry out the steam bleeding 15min first time, for the second time heat up temperature 143-145 ℃ again, behind the 18-20min that heats up for the second time, steam bleeding 10min for the second time, heating-up time is controlled at 22-27min for the third time again, after temperature reached 168-172 ℃, temperature retention time 110-130min finished boiling;
Survey: degree of polymerization 800-950;
(4) preceding desanding: with cotton pulp after the boiling, change in the desander, Pressure control is pulled an oar at 0.3MPa, starches the dense 0.4-0.6% that is controlled at, and after desanding is finished, changes big tapering jordan over to;
(5) preceding making beating:
A, the big tapering jordan of warp, the Current Control of once pulling an oar is at 260-290A, and slurry concentration is controlled at 1.5-1.9%, finishes once making beating,
Survey: freedom 730-740ML fibre length is represented with the Bauer screening ,+14 order 59-68%,
B, once after the making beating, carry out second time making beating, Current Control is at 280-320A, and slurry concentration is controlled at 1.5-1.9%, finish pull an oar for the second time after,
Survey: freedom 719-729ML fibre length is represented with the Bauer screening ,+14 order 50-58%,
After c, the making beating for the second time, pull an oar for the third time, Current Control is at 290-330A, and slurry concentration is controlled at 1.5-1.9%, finishes making beating for the third time,
Survey: freedom 700-718ML fibre length is represented with the Bauer screening ,+14 order 42-49%,
D, for the third time the making beating finish, carry out water washing after, change in the bleaching tower;
(6) bleaching: in first bleaching tower, adding the relative oven dry stock amount of chlorine dioxide respectively is 0.4-0.6%, and the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.4-0.5%, and temperature is controlled at 68-72 ℃, and the time is controlled at 90-120min; Change second bleaching tower after the washing over to, adding the relative oven dry stock amount of hydrogen peroxide respectively is 3-4%, the relative oven dry stock amount of NaOH is 2-2.5%, the relative oven dry stock amount of magnesium sulfate is 2.0-2.5%, the relative oven dry stock amount of diethylene triamine pentacetic acid (DTPA) is 0.17-0.22%, temperature is controlled at 68-72 ℃, and behind the 100-110min, bleaching is finished;
(7) acid treatment: the cotton pulp after will bleaching, adding the relative oven dry stock amount of hydrochloric acid respectively is 2.3-2.7%, and the relative oven dry stock amount of oxalic acid is 0.22-0.27%, and acid treatment 40-50min washed 2-3 hour again;
The mass metering index:
The degree of polymerization: 690-750, irony :≤25ppm, whiteness: 〉=87%, ash :≤0.15%;
(8) back desanding: the cotton pulp after acid treatment, washing changes sand removing machine over to, and Pressure control is carried out desanding at 0.3MPa, starches the dense 0.6%-0.8% that is controlled at, and after the back desanding, changes big tapering jordan over to;
(9) back making beating, through big tapering jordan, Current Control is at 240-280A, and slurry concentration is controlled at 2.0-3.0%, and the back making beating is finished;
Survey: freedom 680-700ML, fibre length is with Bauer screening expression ,+14 order 35-42%;
(10) defibrination changes double disc refiner again over to, and Current Control is at 320-380A, and slurry concentration is controlled at 2.0-3.0%, behind the defibrination;
Survey: fibre length is with Bauer screening expression ,+14 order 20-35%, freedom 650-680ML;
(11) copy slurry: through pulp machine, after manufacturing paper with pulp, oven dry makes finished product.
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