CN102493257B - Masson pine dissolving pulp and production method thereof - Google Patents
Masson pine dissolving pulp and production method thereof Download PDFInfo
- Publication number
- CN102493257B CN102493257B CN 201110403237 CN201110403237A CN102493257B CN 102493257 B CN102493257 B CN 102493257B CN 201110403237 CN201110403237 CN 201110403237 CN 201110403237 A CN201110403237 A CN 201110403237A CN 102493257 B CN102493257 B CN 102493257B
- Authority
- CN
- China
- Prior art keywords
- pulp
- cooking
- black liquor
- bleaching
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 241000018650 Pinus massoniana Species 0.000 title claims abstract description 55
- 235000011609 Pinus massoniana Nutrition 0.000 title claims abstract description 55
- 229920000875 Dissolving pulp Polymers 0.000 title claims abstract description 35
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 238000010411 cooking Methods 0.000 claims abstract description 99
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 86
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000001301 oxygen Substances 0.000 claims abstract description 85
- 238000004061 bleaching Methods 0.000 claims abstract description 65
- 239000002023 wood Substances 0.000 claims abstract description 49
- LUNBMBVWKORSGN-TYEKWLQESA-N P-factor Chemical compound CC(C)C[C@@H](C(O)=O)NC(=O)[C@H](CC(N)=O)NC(=O)[C@@H]1CCCN1C(=O)[C@H](CCCNC(N)=N)NC(=O)[C@H](CC(O)=O)NC(=O)[C@H]1N(C(=O)[C@H](CC(N)=O)NC(=O)[C@@H](NC(=O)[C@H](CC=2C=CC=CC=2)NC(=O)[C@@H](NC(=O)[C@H](CC(N)=O)NC(=O)[C@H](CC=2C3=CC=CC=C3NC=2)NC(=O)[C@H](CO)NC(=O)[C@H](CCC(N)=O)NC(=O)[C@H](CC=2C=CC(O)=CC=2)NC(=O)[C@H](C)NC(=O)[C@H](CCCNC(N)=N)NC(=O)[C@H](CC(C)C)NC(=O)[C@H](CC=2C=CC=CC=2)NC(=O)[C@H](CC(O)=O)NC(=O)[C@H](C)NC(=O)[C@H](CC=2C=CC(O)=CC=2)NC(=O)[C@@H](N)[C@@H](C)O)[C@@H](C)O)C(C)C)CCC1 LUNBMBVWKORSGN-TYEKWLQESA-N 0.000 claims abstract description 11
- 101800002502 P-factor Proteins 0.000 claims abstract description 11
- 229920002678 cellulose Polymers 0.000 claims abstract description 9
- 239000001913 cellulose Substances 0.000 claims abstract description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052742 iron Inorganic materials 0.000 claims abstract description 4
- 239000002655 kraft paper Substances 0.000 claims abstract description 4
- 230000007062 hydrolysis Effects 0.000 claims abstract 7
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 98
- 238000000034 method Methods 0.000 claims description 56
- 239000003513 alkali Substances 0.000 claims description 49
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 48
- 239000002002 slurry Substances 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 21
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 claims description 14
- 229910001948 sodium oxide Inorganic materials 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- 102100030386 Granzyme A Human genes 0.000 claims description 9
- 101001009599 Homo sapiens Granzyme A Proteins 0.000 claims description 9
- 230000002378 acidificating effect Effects 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 2
- 238000012545 processing Methods 0.000 claims description 2
- 235000011121 sodium hydroxide Nutrition 0.000 claims 14
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims 4
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims 4
- 235000019398 chlorine dioxide Nutrition 0.000 claims 4
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 claims 4
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims 2
- 235000019341 magnesium sulphate Nutrition 0.000 claims 2
- 239000011259 mixed solution Substances 0.000 claims 2
- 238000004321 preservation Methods 0.000 claims 2
- 239000000243 solution Substances 0.000 claims 2
- 239000007921 spray Substances 0.000 claims 2
- 150000004676 glycans Chemical class 0.000 claims 1
- 229920001282 polysaccharide Polymers 0.000 claims 1
- 239000005017 polysaccharide Substances 0.000 claims 1
- 238000004537 pulping Methods 0.000 abstract description 5
- 150000002972 pentoses Chemical class 0.000 abstract 1
- 229920001131 Pulp (paper) Polymers 0.000 description 36
- 238000009835 boiling Methods 0.000 description 15
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 12
- 238000012216 screening Methods 0.000 description 11
- 239000004568 cement Substances 0.000 description 10
- 239000000463 material Substances 0.000 description 8
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 238000005507 spraying Methods 0.000 description 6
- 238000010792 warming Methods 0.000 description 6
- 238000001914 filtration Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 3
- 235000017491 Bambusa tulda Nutrition 0.000 description 3
- 241001330002 Bambuseae Species 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 3
- 239000011425 bamboo Substances 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 2
- 229920002488 Hemicellulose Polymers 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 241001349804 Juncus alpinoarticulatus Species 0.000 description 2
- 229920000297 Rayon Polymers 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 229920003086 cellulose ether Polymers 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229920005610 lignin Polymers 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000009941 weaving Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 229910001060 Gray iron Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000740 bleeding effect Effects 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002657 fibrous material Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000123 paper Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Paper (AREA)
Abstract
一种马尾松溶解浆及其生产方法，该马尾松溶解浆由马尾松木片经蒸汽预水解、硫酸盐法蒸煮、二段氧脱木素、D0EoPD1D2漂白而制得，白度不低于89%、甲种纤维素不低于91%、多戊糖不高于3%、动力粘度值为9～25mPa.s、灰分不高于0.1%、铁含量不高于15mg·kg-1。所述马尾松溶解浆的生产方法包括以下步骤：马尾松木片经过蒸汽预水解，蒸汽预水解P-因子为300～800；蒸汽预水解后进行硫酸盐法蒸煮制浆；浆料经二段氧脱木素后，进行D0EoPD1D2漂白；漂白后浆料进行洗涤干燥处理成马尾松溶解浆。A dissolving pulp of masson pine and a production method thereof, the dissolving pulp of masson pine is prepared by steam prehydrolysis of masson pine wood chips, kraft cooking, two-stage oxygen delignification, and D 0 Eo P D 1 D 2 bleaching, The whiteness is not lower than 89%, the cellulose A is not lower than 91%, the pentose is not higher than 3%, the dynamic viscosity is 9-25mPa.s, the ash content is not higher than 0.1%, and the iron content is not higher than 15mg • kg −1 . The production method of the masson pine dissolving pulp comprises the following steps: the masson pine wood chips undergo steam pre-hydrolysis, and the P-factor of the steam pre-hydrolysis is 300-800; after the steam pre-hydrolysis, kraft cooking and pulping are carried out; After delignification, D 0 Eo P D 1 D 2 bleaching is carried out; after bleaching, the pulp is washed and dried to become masson pine dissolving pulp.
Description
Technical field
The present invention relates to a kind of cellulose pulp, especially relate to a kind of Chinese red pine dissolving pulp, the invention still further relates to a kind of production method of cellulose pulp, especially relate to a kind of production method of Chinese red pine dissolving pulp.
Background technology
Common chemical pulping is the lignin of removing in pulping process in plant fiber material, keeps as much as possible cellulose and hemicellulose; Dissolving pulp requires to remove lignin and hemicellulose in pulping process, only keep cellulose, and therefore, early stage dissolving pulp is to adopt the high cotton linter production of content of cellulose.Due to socioeconomic fast development, living standards of the people improve constantly, and the consumption of resource is rapid growth also, particularly also rapid growth of the raw materials consumption of textile industry viscose glue, cellulose mystery and nitrated production field.At present the quantity of the prepared dissolving pulp of cotton linter far can not satisfy the demand in weaving dissolving pulp, nitrated dissolving pulp, acetate dissolution slurry, cellulose ether field.Along with the growth of dissolving pulp demand, at present raw materials for production are take timber as main, and domestic also have the enterprise that produces cellulose viscose pulp take bamboo as raw material.
Patent CN101158121A discloses the technique of making dissolving pulp with ethanol, sulfate, acetic acid, and technique sequentially comprises blank, screening ash disposal, washes material, ethanol extracting, sulphate cook, slurries separation, washing, purifying, chlorination processing, alkali treatment, acetic acid bleaching+H
2O
2The organic bleaching of oxidation, sour complexing are processed, are manufactured paper with pulp.Though production procedure can be effectively shortened in this invention, improve utilize production such as bamboo wood, timber, masson pine, ramulus mori, Chinese alpine rush for the dissolving pulp of weaving, nitrated dissolving pulp, acetate dissolution starch, cellulose ether dissolving pulp field the production efficiency of dissolving pulp, improve simultaneously the yield rate that bamboo wood, timber, masson pine, ramulus mori, Chinese alpine rush etc. are produced dissolving pulp.
Patent CN1013682951A discloses a kind of preparation method of Chinese red pine dissolving pulp, comprises the following steps: 1) get the raw materials ready, choose the masson pine raw material; 2) steam prehydrolysis, technical conditions are: 165～180 ℃ of temperature, pressure 6.5～8.0kg/cm
2, time 50～120min; 3) soda boiling, technical conditions are: total alkali content is with respect to oven dry stock amount 18～25%, total time: the 150～240min that heats up, little steam bleeding number of times: 〉=1 time, be divided into and be three phases: the phase I, be increased to 130～140 ℃ by initial temperature, heating-up time 70～90min; Second stage rises to 165～180 ℃ by 130～140 ℃, heating-up time 70～90min, and 5～10min wherein exits one time; Phase III, 165～180 ℃, insulation 50～70min; Batch turning after boiling, wash material, slightly starched; 4) the pressurized screen screening is adopted in washing, screening, desanding; 5) bleaching, technical conditions are: bleaching liquor effective chlorine density 20～30g/L, bleaching liquor base excess concentration 1～6g/L, bleaching time: 270～310min; 6) acid treatment, technical conditions are: with the relative oven dry stock amount 2.0～5.0% of acid amount, time: 40～60min, temperature: normal temperature; 7) the pressurized screen screening is adopted in bleaching screening; 8) papermaking.
Above invention is adopted and is contained the elemental chlorine bleaching process, and waste water is difficult to process, and big for environment pollution, the whiteness of gained paper pulp is lower, and metal ion content is also higher.
Summary of the invention
In order to overcome the defective of prior art, technical problem to be solved by this invention is that the better Chinese red pine dissolving pulps of performance such as a kind of whiteness, viscosity, purity are provided; For this reason, the present invention also will provide a kind of method of making this Chinese red pine dissolving pulp.
For solving the problems of the technologies described above, dissolving pulp of the present invention by the masson pine wood chip through steam prehydrolysis, kraft cooking, two sections oxygen delignifications, D
0Eo
PD
1D
2Bleaching forms, whiteness is not less than 89%, alpha cellulose is not less than 91%, pentosan not higher than 3%, the dynamic viscosity value be 9～25mPa.s, ash content not higher than 0.1%, iron content is higher than 15mgkg
-1
In order to obtain above-mentioned Chinese red pine dissolving pulp, manufacture method of the present invention comprises following several step:
(1) in the pinus massoniana sheet was packed digester into, wood chip was through steam prehydrolysis, and the steam prehydrolysis P-factor is 300～800;
(2) through the post-job wood chip of step (1) in digester, be filled with the cooking liquor of 135～145 ℃, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, the cooking liquor sulphidity that this step is used is 15%～30%, with the effective alkali consumption of sodium oxide molybdena calculating as 7%～10% of over dry wood chip weight;
(3) utilize the cooking liquor that the cooking liquor of 145～170 ℃ adds step (2) to replace at least one black liquor slot, the effective alkali consumption that the cooking liquor sulphidity that this step is used is 15%～30%, calculate with sodium oxide molybdena is as 9%～12% of over dry wood chip weight;
(4) step (3) is added cooking liquor heat temperature raising in digester, after reaching 160～172 ℃ of temperature, stopping heating up enters holding stage, reaches at 900～1400 o'clock until the H factor, completes this step;
(5) with step (4) gained slurry, filter black liquor with pulp washing and add the cooking liquor in digester to replace at least one black liquor slot step (3), make the interior slurry temperature of digester lower than 100 ℃;
(6) with step (5) gained slurry, send in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening;
(7) step (6) gained masson pine prehydrolysis natural color pulp after two sections oxygen delignifications, carries out D
0Eo
PD
1D
2Bleaching;
(8) the bleaching disposed slurry washs drying and is processed into Chinese red pine dissolving pulp.
Preferably, the process conditions of the described steam prehydrolysis of step (1) are: be warming up to 160～175 ℃ with steam at 25～40 min after the masson pine chip filling, be incubated to the P-factor at 160～175 ℃ and reach 300～800.
Preferably, the described cooking liquor of step (3) is replaced at least one black liquor slot and is: enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot.
Preferably, the described cooking liquor of step (5) is replaced at least one black liquor slot and is: be not less than 160 ℃ enter the 3rd black liquor slot, 140～160 ℃ enter the 4th black liquor slot, lower than 140 ℃ enter the 5th black liquor slot or described the second black liquor slot.
Preferably, the cooking liquor that step (2) is described 135～145 ℃ is the interior black liquor of the second black liquor slot and/or the 5th black liquor slot and the mixed liquor of alkali lye, and described alkali lye is the causticization alkali that obtains in commercially available alkali or alkali recovery process.
Preferably, the cooking liquor that step (3) is described 145～170 ℃ is the interior black liquor of the 3rd black liquor slot and/or the 4th black liquor slot and the mixed liquor of alkali lye, and described alkali lye is the causticization alkali that obtains in commercially available alkali or alkali recovery process.
Preferably, the described two sections oxygen delignifications of step (7), first paragraph Oxygen Delignification of Fast-Growing condition is: NaOH consumption 2%～3%, oxygen pressure 1.0 ~ 1.5 MPa, MgSO
4Consumption 0.2%～0.4%, oxygen delignification slurry concentration 8%～12%, 85～95 ℃ of temperature, times 30～60 min; Slurry after one section oxygen delignification does not wash, and then carries out the second segment oxygen delignification, and second segment oxygen delignification condition is: oxygen pressure 1.0 ~ 1.5 MPa, 95～100 ℃ of oxygen delignification temperature, times 40～60 min.
Preferably, the described D of step (7)
0Eo
PD
1D
2Bleaching, D
0The process conditions of section are: ClO
2Consumption 1%～2%, bleached pulp concentration 8%～12%, time 40～60min, 60～75 ℃ of temperature are regulated with sulfuric acid and are made bleaching endpoint pH≤2.6; E
OPThe process conditions of section are: NaOH consumption 1%～2%, H
2O
2Consumption 0.5%～1%, O
2Pressure 1.0 ~ 1.5MPa, bleached pulp concentration 8%～12%, time 60～90min, 75～95 ℃ of temperature, bleaching endpoint pH 11～12; D
1The process conditions of section are: ClO
2Consumption 0.4%～0.8%, bleached pulp concentration 8%～12%, time 120～150min, 60～75 ℃ of temperature, making the bleaching endpoint pH with the sulfuric acid adjusting is 4～5; D
2The process conditions of section are: ClO
2Consumption 0.2%～0.5%, bleached pulp concentration 8%～12%, time 60～100min, 60～75 ℃ of temperature, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 4～5.
Above preferred version can be implemented separately, also can two and two above scheme combination enforcements.
The invention has the beneficial effects as follows: because adopting steam prehydrolysis, oxygen delignification, element chlorine free bleaching, the generation of waste water and waste gas is few, and pollutional load is low, is easy to process, little to ambient influnence, the products obtained therefrom quality is easy to control, can satisfy well QUALITY STANDARD and customer requirements; Can reclaim the energy in digestion process, energy consumption is lower.Because adopting ClO 2 bleaching, effectively reduce in slurry the heavy metal ion contents such as gray iron, improve the reactivity worth of slurry.
The specific embodiment
Embodiment 1:
The pinus massoniana sheet is packed into after digester, is warming up to 160 ℃ with steam at 25min, carries out steam prehydrolysis, is incubated to the prehydrolysis P-factor to reach 400 under maximum temperature.Through the post-job wood chip of prehydrolysis in digester, be filled with the cooking liquor of 135～145 ℃, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, this step cooking liquor used is the black liquor and the mixed liquor of commercially available alkali and akali sulphide in aftermentioned the 5th black liquor slot, and sulphidity is 15%, take the effective alkali consumption of sodium oxide molybdena calculating as 7% of over dry wood chip weight.Cooking liquor in wood chip after utilizing the cooking liquor of 145～170 ℃ with elementary cooking operation cements out, enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot, the cooking liquor that this step is used is the mixed liquor of the black liquor of aftermentioned the 3rd black liquor slot and commercially available alkali, akali sulphide, and the effective alkali consumption that sulphidity is 30%, calculate take sodium oxide molybdena is as 12% of over dry wood chip weight.To the cooking liquor heat temperature raising in digester, after reaching 172 ℃ of temperature, stop heating up and enter holding stage, reach at 1300 o'clock until the H factor, filtering black liquor with pulp washing will add the cooking liquor in digester to cement out, make slurry temperature in digester lower than 100 ℃, be not less than 160 ℃ enter the 3rd black liquor slot, 140 ℃～160 ℃ enter the 4th black liquor slot and lower than 140 ℃ enter the 5th black liquor slot or the second black liquor slot.After completing, boiling with the gained slurry, sends in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening.Gained masson pine prehydrolysis natural color pulp is through two sections oxygen delignification, and first paragraph Oxygen Delignification of Fast-Growing condition is: the NaOH consumption be absolute dried paper pulp weight 3%, oxygen pressure 1.5 MPa, oxygen delignification slurry concentration 8%, 95 ℃ of temperature, MgSO
4Consumption be absolute dried paper pulp weight 0.4%, oxygen delignification times 30 min; Slurry after one section oxygen delignification does not wash, and then carries out the second segment oxygen delignification, and second segment oxygen delignification condition is: oxygen pressure 1.0 MPa, 95 ℃ of oxygen delignification temperature, oxygen delignification times 60 min.The oxygen delignification disposed slurry is through D
0Eo
PD
1D
2Bleaching, wherein D
0The process conditions of section are: ClO
2Consumption is 1% of absolute dried paper pulp weight, bleached pulp concentration 12%, and time 40min, 75 ℃ of bleaching temperatures, making the bleaching endpoint pH with the sulfuric acid adjusting is 2.3; E
OPThe process conditions of section are: the NaOH consumption is 2% of absolute dried paper pulp weight, H
2O
2Consumption is 1% of absolute dried paper pulp weight, O
2Pressure 1.5MPa, bleached pulp concentration 8%, time 90min, 75 ℃ of bleaching temperatures, bleaching endpoint pH 11; D
1The process conditions of section are: ClO
2Consumption is 0.8% of absolute dried paper pulp weight, bleached pulp concentration 8%, and time 120min, 75 ℃ of bleaching temperatures, making the bleaching endpoint pH with the sulfuric acid adjusting is 4; D
2The process conditions of section are: ClO
2Consumption is 0.2% of absolute dried paper pulp weight, bleached pulp concentration 8%, and time 60min, 60 ℃ of bleaching temperatures, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 5.
Embodiment 2:
The pinus massoniana sheet is packed into after digester, is warming up to 175 ℃ with steam at 40min, carries out steam prehydrolysis, is incubated to the prehydrolysis P-factor to reach 650 under maximum temperature.Through the post-job wood chip of prehydrolysis in digester, be filled with the cooking liquor of 135～145 ℃, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, this step cooking liquor used is the mixed liquor of the causticization alkali that obtains in black liquor and alkali recovery process in aftermentioned the 5th black liquor slot, and sulphidity is 30%, take the effective alkali consumption of sodium oxide molybdena calculating as 10% of over dry wood chip weight.Cooking liquor in wood chip after utilizing the cooking liquor of 145～160 ℃ with elementary cooking operation cements out, enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot, the cooking liquor that this step is used is the mixed liquor of the black liquor of aftermentioned the 3rd black liquor slot and commercially available alkali, akali sulphide, and the effective alkali consumption that sulphidity is 15%, calculate take sodium oxide molybdena is as 9% of over dry wood chip weight.To the cooking liquor heat temperature raising in digester, after reaching 160 ℃ of temperature, stop heating up and enter holding stage, reach at 1400 o'clock until the H factor, filtering black liquor with pulp washing will add the cooking liquor in digester to cement out, make slurry temperature in digester lower than 100 ℃, be not less than 160 ℃ enter the 3rd black liquor slot, 140 ℃～160 ℃ enter the 4th black liquor slot and lower than 140 ℃ enter the 5th black liquor slot or the second black liquor slot.After completing, boiling with the gained slurry, sends in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening.Gained masson pine prehydrolysis natural color pulp is through two sections oxygen delignification, and first paragraph Oxygen Delignification of Fast-Growing condition is: the NaOH consumption be absolute dried paper pulp weight 2%, oxygen pressure 1.0MPa, MgSO
4Consumption be absolute dried paper pulp weight 0.2%, oxygen delignification slurry concentration 12%, 85 ℃ of temperature, times 60 min; Slurry after one section oxygen delignification does not wash, and then carries out the second segment oxygen delignification, and second segment oxygen delignification condition is: oxygen pressure 1.5MPa, 100 ℃ of oxygen delignification temperature, times 40 min.The oxygen delignification disposed slurry is through D
0Eo
PD
1D
2Bleaching, wherein D
0The process conditions of section are: ClO
2Consumption is 2% of absolute dried paper pulp weight, bleached pulp concentration 8%, and time 40min, temperature 60 C, making the bleaching endpoint pH with the sulfuric acid adjusting is 2.4; E
OPThe process conditions of section are: the NaOH consumption is 1% of absolute dried paper pulp weight, H
2O
2Consumption is 0.5% of absolute dried paper pulp weight, O
2Pressure 1.0MPa, bleached pulp concentration 12%, time 60min, 95 ℃ of temperature, bleaching endpoint pH 12; D
1The process conditions of section are: ClO
2Consumption is 0.4% of absolute dried paper pulp weight, bleached pulp concentration 12%, and time 150min, temperature 60 C, making the bleaching endpoint pH with the sulfuric acid adjusting is 5; D
2The process conditions of section are: ClO
2Consumption is 0.5% of absolute dried paper pulp weight, bleached pulp concentration 12%, and time 100min, 75 ℃ of temperature, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 4.
Embodiment 3:
The pinus massoniana sheet is packed into after digester, is warming up to 170 ℃ with steam at 35min, carries out steam prehydrolysis, is incubated to the prehydrolysis P-factor to reach 500 under maximum temperature.Through the post-job wood chip of prehydrolysis in digester, be filled with the cooking liquor of 135～145 ℃, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, this step cooking liquor used is the mixed liquor of the causticization alkali that obtains in black liquor and alkali recovery process in aftermentioned the second black liquor slot, and sulphidity is 22%, take the effective alkali consumption of sodium oxide molybdena calculating as 8% of over dry wood chip weight.Cooking liquor in wood chip after utilizing the cooking liquor of 145～168 ℃ with elementary cooking operation cements out, enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot, the cooking liquor that this step is used is the mixed liquor of the causticization alkali that obtains in the black liquor of aftermentioned the 4th black liquor slot and alkali recovery process, and the effective alkali consumption that sulphidity is 23%, calculate take sodium oxide molybdena is as 11% of over dry wood chip weight.To the cooking liquor heat temperature raising in digester, after reaching 168 ℃ of temperature, stop heating up and enter holding stage, reach at 1350 o'clock until the H factor, filtering black liquor with pulp washing will add the cooking liquor in digester to cement out, make slurry temperature in digester lower than 100 ℃, be not less than 160 ℃ enter the 3rd black liquor slot, 140 ℃～160 ℃ enter the 4th black liquor slot and lower than 140 ℃ enter the 5th black liquor slot or the second black liquor slot.After completing, boiling with the gained slurry, sends in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening.Gained masson pine prehydrolysis natural color pulp is through two sections oxygen delignification, and the process conditions of first paragraph oxygen delignification are: the NaOH consumption be absolute dried paper pulp weight 2.5%, oxygen pressure 1.3 MPa, MgSO
4Consumption be absolute dried paper pulp weight 0.3%, oxygen delignification slurry concentration 10%, 90 ℃ of temperature, time 45min; Slurry after one section oxygen delignification then carries out the second segment oxygen delignification without washing, and second segment oxygen delignification condition is: oxygen pressure 1.1MPa, 97 ℃ of oxygen delignification temperature, times 50 min.The oxygen delignification disposed slurry is through D
0Eo
PD
1D
2Bleaching, D
0The process conditions of section are: ClO
2Consumption is 1.5% of absolute dried paper pulp weight, bleached pulp concentration 10%, and time 50min, temperature 70 C, making the bleaching endpoint pH with the sulfuric acid adjusting is 2.5; E
OPThe process conditions of section are: the NaOH consumption is 1.5% of absolute dried paper pulp weight, H
2O
2Consumption is 0.7% of absolute dried paper pulp weight, O
2Pressure 1.0MPa, bleached pulp concentration 10%, time 75min, 85 ℃ of temperature, bleaching endpoint pH 11.5; D
1The process conditions of section are: ClO
2Consumption is 0.6% of absolute dried paper pulp weight, bleached pulp concentration 10%, and time 135min, 68 ℃ of temperature, making the bleaching endpoint pH with the sulfuric acid adjusting is 4.5; D
2The process conditions of section are: ClO
2Consumption is 0.35% of absolute dried paper pulp weight, bleached pulp concentration 10%, and time 80min, temperature 70 C, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 4.5.
Embodiment 4:
The pinus massoniana sheet is packed into after digester, is warming up to 168 ℃ with steam at 30min, carries out steam prehydrolysis, is incubated to the prehydrolysis P-factor to reach 300 under maximum temperature.Through the post-job wood chip of prehydrolysis in digester, be filled with the cooking liquor of 135～145 ℃, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, this step cooking liquor used is the mixed liquor of the causticization alkali that obtains in black liquor and alkali recovery process in aftermentioned the second black liquor slot and the 5th black liquor slot, and sulphidity is 25%, take the effective alkali consumption of sodium oxide molybdena calculating as 8% of over dry wood chip weight.Cooking liquor in wood chip after utilizing the cooking liquor of 145～170 ℃ with elementary cooking operation cements out, enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot, the cooking liquor that this step is used is the mixed liquor of the causticization alkali that obtains in the black liquor of aftermentioned the 3rd black liquor slot and the 4th black liquor slot and alkali recovery process, and the effective alkali consumption that sulphidity is 24%, calculate take sodium oxide molybdena is as 11% of over dry wood chip weight.To the cooking liquor heat temperature raising in digester, after reaching 167 ℃ of temperature, stop heating up and enter holding stage, reach at 900 o'clock until the H factor, filtering black liquor with pulp washing will add the cooking liquor in digester to cement out, make slurry temperature in digester lower than 100 ℃, be not less than 160 ℃ enter the 3rd black liquor slot, 140 ℃～160 ℃ enter the 4th black liquor slot and lower than 140 ℃ enter the 5th black liquor slot or the second black liquor slot.After completing, boiling with the gained slurry, sends in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening.Gained masson pine prehydrolysis natural color pulp is through two sections oxygen delignification, and the process conditions of first paragraph oxygen delignification are: the NaOH consumption be absolute dried paper pulp weight 2.7%, oxygen pressure 1.5 MPa, 95 ℃ of temperature, MgSO
4Consumption be absolute dried paper pulp weight 0.4%, oxygen delignification slurry concentration 11%, times 40 min; Slurry after one section oxygen delignification does not wash, and then carries out the second segment oxygen delignification, and the process conditions of second segment oxygen delignification are: oxygen pressure 1.2 MPa, 98 ℃ of temperature, times 58 min.The oxygen delignification disposed slurry is through D
0Eo
PD
1D
2Bleaching, D
0The process conditions of section are: ClO
2Consumption is 1.8% of absolute dried paper pulp weight, bleached pulp concentration 11.5%, and time 55min, temperature 70 C, making the bleaching endpoint pH with the sulfuric acid adjusting is 2.6; E
OPThe process conditions of section are: the NaOH consumption is 1.4% of absolute dried paper pulp weight, H
2O
2Consumption is 0.7% of absolute dried paper pulp weight, O
2Pressure 1.1MPa, bleached pulp concentration 10.3%, time 80min, 85 ℃ of temperature, bleaching endpoint pH 11.6; D
1The process conditions of section are: ClO
2Consumption is 0.6% of absolute dried paper pulp weight, bleached pulp concentration 11.7%, and time 140min, 72 ℃ of temperature, making the bleaching endpoint pH with the sulfuric acid adjusting is 4.5; D
2The process conditions of section are: ClO
2Consumption is 0.29% of absolute dried paper pulp weight, bleached pulp concentration 10.5%, and time 85min, 72 ℃ of temperature, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 4.7.
Embodiment 5:
The pinus massoniana sheet is packed into after digester, is warming up to 173 ℃ with steam at 35min, carries out steam prehydrolysis, is incubated to the prehydrolysis P-factor to reach 800 under maximum temperature.Through the post-job wood chip of prehydrolysis in digester, be filled with 135～145 cooking liquor, in and the acidic materials that produce of prehydrolysis and wood chip is carried out elementary boiling, this step cooking liquor used is the mixed liquor of the causticization alkali that obtains in black liquor and alkali recovery process in aftermentioned the second black liquor slot and the 5th black liquor slot, and sulphidity is 27%, take the effective alkali consumption of sodium oxide molybdena calculating as 8.5% of over dry wood chip weight.Cooking liquor in wood chip after utilizing the cooking liquor of 145～165 ℃ with elementary cooking operation cements out, enter the first black liquor slot lower than the cooking liquors of 100 ℃, the cooking liquor that is not less than 100 ℃ enters the second black liquor slot, the cooking liquor that this step is used is the mixed liquor of the causticization alkali that obtains in the black liquor of aftermentioned the 3rd black liquor slot and the 4th black liquor slot and alkali recovery process, and the effective alkali consumption that sulphidity is 22%, calculate take sodium oxide molybdena is as 10% of over dry wood chip weight.To the cooking liquor heat temperature raising in digester, after reaching 168 ℃ of temperature, stop heating up and enter holding stage, reach at 1400 o'clock until the H factor, filtering black liquor with pulp washing will add the cooking liquor in digester to cement out, make slurry temperature in digester lower than 100 ℃, be not less than 160 ℃ enter the 3rd black liquor slot, 140 ℃～160 ℃ enter the 4th black liquor slot and lower than 140 ℃ enter the 5th black liquor slot or the second black liquor slot.After completing, boiling with the gained slurry, sends in spraying pot, through black liquid extraction, obtain masson pine prehydrolysis natural color pulp by screening.Gained masson pine prehydrolysis natural color pulp is through two sections oxygen delignification, and the process conditions of first paragraph oxygen delignification are: the NaOH consumption be absolute dried paper pulp weight 2.7%, oxygen pressure 1.4 MPa, MgSO
4Consumption be absolute dried paper pulp weight 0.3%, oxygen delignification slurry concentration 11%, 90 ℃ of temperature, times 35 min; Slurry after one section oxygen delignification does not wash, and then carries out the second segment oxygen delignification, and the process conditions of second segment oxygen delignification are: oxygen pressure 1.1 MPa, 97 ℃ of oxygen delignification temperature, times 52 min.The oxygen delignification disposed slurry is through D
0Eo
PD
1D
2Bleaching, D
0The process conditions of section are: ClO
2Consumption is 1.5% of absolute dried paper pulp weight, bleached pulp concentration 10.7%, and time 55min, temperature 70 C, making the bleaching endpoint pH with the sulfuric acid adjusting is 2.5; E
OPThe process conditions of section are: the NaOH consumption is 1.2% of absolute dried paper pulp weight, H
2O
2Consumption is 0.6% of absolute dried paper pulp weight, O
2Pressure 1.02MPa, bleached pulp concentration 11.7%, time 70min, 85 ℃ of temperature, bleaching endpoint pH 11.7; D
1The process conditions of section are: ClO
2Consumption is 0.5% of absolute dried paper pulp weight, bleached pulp concentration 11%, and time 130min, 69 ℃ of temperature, making the bleaching endpoint pH with the sulfuric acid adjusting is 4.6; D
2The process conditions of section are: ClO
2Consumption is 0.26% of absolute dried paper pulp weight, bleached pulp concentration 11.8, and time 92min, 67 ℃ of temperature, making the bleaching endpoint pH with sulfuric acid or NaOH adjusting is 4.5.
The part process of above-described embodiment and test data is as follows as a result:
| Test event | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| The prehydrolysis P factor | 400 | 650 | 500 | 300 | 800 |
| The boiling H-factor | 1300 | 1400 | 1350 | 900 | 1400 |
| Screened yield after boiling (%) | 35.70 | 34.43 | 35.42 | 36.26 | 33.97 |
| Brown stock viscosity (mLg -1） | 766 | 714 | 727 | 655 | 623 |
| Whiteness (ISO%) | 90.23 | 90.52 | 89.73 | 89.21 | 91.03 |
| Alpha cellulose (%) | 91.64 | 92.65 | 92.06 | 91.02 | 92.1 |
| Pentosan (%) | 2.93 | 2.82 | 2.90 | 3.62 | 2.57 |
| Dynamic viscosity (mPa.s) | 25 | 22 | 23 | 19 | 9 |
| Ash content (%) | 0.06 | 0.06 | 0.05 | 0.06 | 0.05 |
| Iron content (mgkg -1） | 12 | 14 | 13 | 15 | 15 |
In the present invention, the analysis of liquid used and product quality is all undertaken by national standard method, and definite method of the P factor please refer to " pulping chemistry " that Chen Jiaxiang writes, and light industry in June nineteen ninety publishing house publishes, and the content that the 232-236 page discloses is determined.
Obviously, the invention is not restricted to above preferred embodiment, also can change other process conditions in spirit of the present invention, have same effect, therefore do not repeat.Those of ordinary skill in the art can from content disclosed by the invention directly or all methods of associating, also belong to content of the present invention.
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110403237 CN102493257B (en) | 2011-12-07 | 2011-12-07 | Masson pine dissolving pulp and production method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110403237 CN102493257B (en) | 2011-12-07 | 2011-12-07 | Masson pine dissolving pulp and production method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102493257A CN102493257A (en) | 2012-06-13 |
| CN102493257B true CN102493257B (en) | 2013-06-05 |
Family
ID=46185113
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110403237 Active CN102493257B (en) | 2011-12-07 | 2011-12-07 | Masson pine dissolving pulp and production method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102493257B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6075976B2 (en) * | 2012-06-15 | 2017-02-08 | 日本製紙株式会社 | Method for producing dissolved kraft pulp |
| CN102888772B (en) * | 2012-10-17 | 2015-01-28 | 四川永丰纸业股份有限公司 | Method for preparing bamboo pulp by replacing cooking sulfate with steaming sulfate |
| US10947669B2 (en) * | 2016-02-16 | 2021-03-16 | Valmet Ab | Method for recovering concentrated hydrolysate after hydrolysis of cellulose material |
| JP6423838B2 (en) * | 2016-09-23 | 2018-11-14 | 日本製紙株式会社 | Method for producing dissolved kraft pulp |
| WO2019039982A1 (en) * | 2017-08-25 | 2019-02-28 | Valmet Ab | Improved compact process for producing prehydrolyzed pulp |
| CN109505178B (en) * | 2018-11-21 | 2021-08-17 | 湖南骏泰新材料科技有限责任公司 | Cooking method for preparing cellulose from agricultural and forestry residues |
| CN110904710A (en) * | 2019-11-06 | 2020-03-24 | 福建省青山纸业股份有限公司 | Bamboo pulp preparation process |
| CN110983848A (en) * | 2019-11-06 | 2020-04-10 | 福建省青山纸业股份有限公司 | Preparation process of bamboo unbleached pulp |
| CN114277598A (en) * | 2021-03-30 | 2022-04-05 | 赣南师范大学 | Preparation method of hollow, porous heterocell and bamboo dissolving pulp |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101368295A (en) * | 2008-09-19 | 2009-02-18 | 福建省南纸股份有限公司 | Preparation method for Chinese red pine dissolving pulp |
| CN101748630A (en) * | 2009-12-14 | 2010-06-23 | 昆明理工大学 | Acid-free pre-hydrolysis enzymolysis-free method for preparing bamboo pulp of Dendrocalamus giganteus Munro series |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI103898B1 (en) * | 1994-01-24 | 1999-10-15 | Sunds Defibrator Pori Oy | Process for the preparation of prehydrolysed chemical pulp and / or cellulose pulp |
-
2011
- 2011-12-07 CN CN 201110403237 patent/CN102493257B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101368295A (en) * | 2008-09-19 | 2009-02-18 | 福建省南纸股份有限公司 | Preparation method for Chinese red pine dissolving pulp |
| CN101748630A (en) * | 2009-12-14 | 2010-06-23 | 昆明理工大学 | Acid-free pre-hydrolysis enzymolysis-free method for preparing bamboo pulp of Dendrocalamus giganteus Munro series |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102493257A (en) | 2012-06-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102493257B (en) | Masson pine dissolving pulp and production method thereof | |
| CN102493256A (en) | Eucalyptus dissolving pulp and production method thereof | |
| JP5808795B2 (en) | Method and system for the production of high alpha dissolving pulp | |
| CN101748630B (en) | Method for preparing dragon bamboo series bamboo pulp without acid prehydrolysis and without enzymatic hydrolysis | |
| CN104790241B (en) | A kind of clean method for preparing of high-purity high-quality bamboo wood dissolving pulp | |
| CN101613970A (en) | Bagasse dissolving pulp pulping process of preextraction hemicellulose and products thereof | |
| CN102888772B (en) | Method for preparing bamboo pulp by replacing cooking sulfate with steaming sulfate | |
| CN103382671A (en) | Clean pulping technology for high-polymerization-degree bamboo pulp | |
| CN103924470A (en) | Unbleached pulp production method for increasing whiteness of pulp | |
| CN107974856B (en) | Method for applying green chelating agent in pulp hydrogen peroxide bleaching | |
| CN106245418A (en) | A kind of method utilizing Chinese herb residues to prepare natural color pulp and utilize the method that this natural color pulp prepares true qualities package paper | |
| CN103243596B (en) | A kind of Acetate-grade pulp and preparation method thereof | |
| CN104452397B (en) | Method for improving reactive performance of prehydrolysis sulfate dissolving pulp | |
| CN103526623B (en) | A kind of xylanase pretr eatment improves the method for soda-oxygen pulping effect | |
| CN103669064B (en) | A kind of preparation technology of vinegar-grade bamboo pulp | |
| CN108914669A (en) | A kind of preparation method and dissolving pulp of dissolving pulp | |
| CN108797176B (en) | Method for preparing dissolving pulp from all cotton stalks | |
| CN111618961B (en) | A kind of preparation method of viscose grade bamboo dissolving pulp | |
| CN102587185B (en) | Method for cleaning and bleaching eucalyptus dissolving pulp | |
| CN103556249A (en) | Palm viscose and preparation method thereof | |
| CN101158121B (en) | Process for manufacturing dissolved pulp by using ethanol, sulfate and acetic acid | |
| CN104928958A (en) | Method of producing corrugated paper with straw | |
| CN103774478A (en) | Method of removing hemicelluloses by intensifying bamboo pre-hydrolysis by use of oxalic acid | |
| JP6581137B2 (en) | Method for producing dissolved kraft pulp | |
| CN101871135A (en) | Method for producing bleaching man-made fiber pulp |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 418005 Huaihua Industrial Park, Hunan, Huaihua Patentee after: Hunan Jun Thai New Materials Technology Co. Ltd. Patentee after: Changsha University of Sciences and Technology Address before: 418005 Huaihua Industrial Park, Hunan, Huaihua Patentee before: Hu'nan Juntai Pulp Paper Co., Ltd. Patentee before: Changsha University of Sciences and Technology |