CN102995478A - Bleaching method for preparing high quality low pollution bamboo wood dissolving slurry - Google Patents
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Abstract
The invention relates to a bleaching method for preparing a high quality low pollution bamboo wood dissolving slurry, which comprises the following steps: 1) removing parenchyma cells, employing a sieve method or a slurry washing method for removing parenchyma cells; 2) performing an oxidation reaction to remove a transition metal compound, removing boiled residual lignin in the unbleached slurry, performing ozone bleaching on washed slurry; 3) refining alkali in a reinforced mode; 4) bleaching chlorine dioxide; and 5) processing by acidifying at high temperature. According to the invention, delignification step by step, dynamic viscosity adjusting, whiteness enhancement, fine fiber generation reduction, and reaction capability activation are carried out on unbleached bamboo wood dissolving slurry, on the basis of increasing fiber strength, whiteness and filtering quality, the pollution load of the bleaching waste water is reduced, the bamboo wood dissolving slurry with high product quality and low environmental pollution is prepared, and provides a high quality raw material for producing the viscose fiber.
Description
Technical field
The present invention relates to a kind of low method for bleaching that pollutes bamboo wood dissolving pulp of high-quality that can improve dissolving pulp reactivity worth, intensity, improve strainability and environmental contamination reduction, particularly relate to a kind of take bamboo wood as raw material, remove the alkali refining → ClO 2 bleaching of heteroproteose cell → oxidation reaction → reinforcement → high temperature acidified processing by employing and come the low method for bleaching that pollutes bamboo wood dissolving pulp of preparation high-quality that the preparation feedback ability is good, strainability is high, low in the pollution of the environment, belong to fiber pulp manufacturing process technology field.
Background technology
Traditional non-cotton cellulosic dissolving pulp method for bleaching mainly adopts chloride high CEH tri-stage bleaching method, i.e. chlorination (C), alkalization (E), hypochlorite (H) bleaching.This traditional chlorine bleach produces because of shortcoming and endangers and is eliminated greatly gradually very much, because chlorine is a kind of strong oxidizer, the reaction non-selectivity, when removing lignin, react with carbohydrate (cellulose), cellulose is damaged and degrades, its defective mainly contains: 1. the finished product whiteness is low, intensity is low, remove the lignin weak effect, and the pulp respond is poor; Strainability and the spinnability of the viscose glue that 2. makes are poor.
The contaminated wastewater that the CEH tri-stage bleaching produces is very serious, except BOD, the COD of high load capacity, also has a large amount of organic chloride (AOX), the toxicity that has is very big, have strong carcinogenic, waste water is difficult to process, and also has most organic chloride not degrade in biochemical treatment.The bleaching water consumption is high.Therefore, the CEH tri-stage bleaching does not meet the requirement that improves quality, protection of the environment, energy savings, sustainable development.
The bamboo wood dissolving pulp tool from special performances cotton, that wooden dissolving pulp is different, adopt the equipment and technology that falls behind at present, poor product quality, environmental protection also is difficult to up to standard, its difference with the dissolving pulp such as cotton, wooden is mainly manifested in preparation process: the fiber dynamic viscosity is wayward, and the scattered error scope is large; Bleachability is poor; Respond is low etc.Cause the main cause of this phenomenon to have: the 1. existence of residual lignin in the slurry; 2. metal ion; 3. extract; 4. fiber fines and heteroproteose cell; 5. bamboo wood kind.
If still adopt conventional CEH bleaching, and in order to reach the purpose that improves pulp brightness and continue to remove residual lignin, can only be to use strong chlorine to carry out oxidation processes, the consequence that causes is that fibre strength acutely descends, the scattered error expanded range of dynamic viscosity, all degree can not guarantee; Reactivity worth, strainability worsen.
Summary of the invention
The object of the invention is to solve the problems referred to above that prior art exists, and provide a kind of and can improve dissolving pulp reactivity worth, intensity, improve the low method for bleaching that pollutes bamboo wood dissolving pulp of preparation high-quality of strainability and environmental contamination reduction.The present invention is directed to bamboo wood dissolving pulp self characteristic in preparation process, remove the alkali refining → ClO 2 bleaching of heteroproteose cell → oxidation reaction → reinforcement → high temperature acidified processing method for bleaching by employing and overcome above shortcoming and problem, prepare pulping lighter color, intensity is high, respond is good, strainability is high, low in the pollution of the environment bleaching dissolving bamboo pulp.
The technical solution adopted in the present invention is: the low method for bleaching that pollutes bamboo wood dissolving pulp of this preparation high-quality is characterized in including following steps.
1. remove heteroproteose cell.
Adopt screening or pulp washing method to carry out removing of heteroproteose cell, wherein: screening: screening the pulp concentration 0.7-2.5%, sieve plate specification Φ 0.10-2.5mm, pulp purity≤200kgCOD/adt; Or pulp washing method: sizing concentration 0.5-3.0%, temperature 50-90 ℃, pulp purity≤200kgCOD/adt.
Contained cell mainly contains fibrocyte, parenchyma cell, conduit, lithocyte, epidermal cell etc. in the bamboo wood.The bamboo pulp fiber cell accounts for 60～70% of gross area ratio, is lower than needlebush and is higher than general careless class.Lithocyte is more, accounts for 20～30% of the gross area, is one of feature of bamboo.Parenchyma cell, conduit, lithocyte, epidermal cell and be referred to as heteroproteose cell below the parts of fine fubril.Through microscopic examination, the size of heteroproteose cell is between 5-110um, and the water filtering performance of slurry was relatively poor when heteroproteose cell was more.Through to the analysis of heteroproteose cell chemical composition, its lignin content, ash, iron part are high, and lignin content is up to 48.6%.
The existence of heteroproteose cell has destroyed the intensity of pulping, has reduced the one-tenth pulp brightness, and the raising of the reactivity worth of restriction removes heteroproteose cell and is conducive to improve reactivity worth, is conducive to improve the spinnability of fiber, improves fibre strength and whiteness.
2. oxidation reaction.
(1) acidifying preliminary treatment.
Add pretreating agent in removing the disposed slurry of heteroproteose cell, finishing agent can be inorganic acid, also can be organic acid.Technological requirement is.
Pretreatment reaction PH :≤6.
Pretreatment time: 10-40 divides.
Pretreatment temperature: 20-60 ℃.
Measure 1-3kg/adt with acid.
Amount of chelant: 1-2 ‰.
In slurrying phase process, transition metal is retained in the paper pulp and causes occuring in the side reaction of oxidation reaction section, oxygen delignification selectively influenced.For fear of harmful side reaction, improve oxidation reaction section delignification efficient, obtain the slurry of the high dynamic viscosity of low kappa number, transistion metal compound must be removed, so the preliminary treatment of paper pulp is very necessary.
(2) oxygen delignification.
To evenly mix with oxygen and be placed in the oxygen reactor through the pretreated bamboo wood dissolving pulp that do not float, make oxygen and slurry generation oxidation, decoloring reaction, continue to remove the residual lignin in the brown stock material after the boiling, improve slurry purity, and dynamic viscosity is slightly descended.Technological requirement is.
The oxygen reaction time: 30-90 divides.
Reaction temperature: 50-105 ℃.
Oxygen consuming amount: 0.5-2.0%.
Dynamic viscosity fall off rate: 5-15%.
Purity behind the pulp washing :≤100kgCOD/adt.
In the oxygen delignification process, oxygen main with lignin structure in the phenol anion react, produce the phenol free radical, make lignin generation demethylation, and then the aromatic ring open loop is degraded to water-soluble organic acid, reach the effect that removes lignin.
The major advantage of oxygen delignification is: improve bleaching process efficient, allow the order of floating of lacking; Without chlorion, can put recovery system by sulfuric acid and process in the waste liquid; Reduce the chemical cost of the follow-up section of floating.
(3) ozone bleaching.
Slurry through washing enters ozone reactor, reacts with ozone.Technological requirement is.
Ozone consumption: 0.4-1.0%.
Reaction time: 1-10 divides.
Temperature: 20-60 ℃.
Ozone concentration: 1.5-3.5%.
Purity behind the pulp washing :≤50kgCOD/adt.
During the ozone bleaching, can produce a large amount of active oxygen radicals in the system, its oxidation potential is very high, can make the glycosidic linkage fracture of polysaccharide, the Main Function of ozone is to adjust the slurry dynamic viscosity, and dynamic viscosity is controlled in the technological requirement scope, and slurry is all spent raising; Its two, stronger active oxygen act on chromophoric group and with it the reaction, improved pulp brightness.
3, the alkali refining of strengthening.
The alkali refining medium is highly basic NaOH, and it is a relatively good nucleopilic reagent, and most of organic bound chlorine is removed, and reduces AOX; And the acidic moiety of neutralization part and workshop section's degraded, the anion form that obtains has increased the solubility of lignin.With oxygen (O) and/or hydrogen peroxide (H
2
O
2
) reinforced alkaline is refining, can in the situation without serious cellulose degradation, reduce D section chlorine dioxide expense and reduction Kappa number.And, oxygen (O) and hydrogen peroxide (H
2
O
2
) can add simultaneously and use or only add and use wherein a kind of.Technological requirement is.
The alkali refining time: 30-90 divides.
PH：10.5-14。
Temperature: 60-90 ℃.
Hydrogen peroxide (H
2
O
2
) consumption: 0.25-0.75%.
Oxygen (O) consumption: 0.2-0.6%.
Wash rear alkalinity :≤0.06 g/l.
4, ClO 2 bleaching.
For the self-characteristic of bamboo wood dissolving pulp, adopt element chlorine free bleaching behind the alkali refining, bleaching agent is chlorine dioxide.In bleaching process, chlorine dioxide reacts with lignin selectively and removes lignin; And cellulose degradation is few, and fiber fines produces few, has improved fibre strength; Retention of whiteness is good; The COD load is low in the waste water, the organic chloride content that decrease toxicity is large.By the ClO 2 bleaching bamboo wood dissolving pulp, effectively reduced fiber degradation, reduced lignin content, so that the pulp activity is further improved, respond, strainability improve.ClO 2 bleaching in carry out under the dense condition, technological requirement is.
Chlorine: 0.8-1.5%.
Reaction density: 8-14%.
Reaction temperature: 60-80 ℃.
Reaction time: 80-160 divides.
Reaction acidity: 0.08-0.20g/l.
Wash rear acid content :≤0.02 g/l.
5, high temperature acidified processing.
When processing slurry with acid, the H+ in the acid exchanges the Fe++ on the cellulose, Mg++ or Ca++, again becomes the COOH(carboxyl), numerous metal ions is dissolved in the water and flush away, thereby has reduced the ash of pulp.(high temperature peracid) treatment process of use strengthening not only can reduce ash and irony, can also remove pentose in the dissolving pulp, glycal aldehydic acid, thereby greatly improves the respond of pulp, for the yellow glue provides the high-quality pulp.Acid treatment is carried out with hydrochloric acid or sulfuric acid, and technological requirement is.
Reaction density: 4-8%.
Reaction temperature: 50-80 ℃.
Reaction time: 30-90 divides.
Reaction acidity: 0.8-1.8g/l.
Wash rear acid content :≤0.02 g/l.
For realizing better purpose of the present invention, described ClO 2 bleaching step also can be divided into two sections carries out, and is called D1 section and D2 section, and D1 section chlorine dosage accounts for the 55-80% of total chlorine amount; D2 section chlorine dosage accounts for the 20-45% of total chlorine amount.
The present invention compared with prior art, its beneficial effect is.
By this process, carried out the delignification of the degree of depth processes not floating bamboo dissolved pulp, activate fibrocellular performance, effectively adjusted the dynamic viscosity scope of bamboo wood dissolving slurry, made it more stable homogeneous, improve whiteness and the intensity of slurry, by the bamboo wood dissolving pulp that this technical scheme makes, dynamic viscosity 10-26mpa.s, content of alphacellulose is greater than 95%, lignin content is lower than 0.6%, finished product whiteness (ISO) 〉=86%.Reactivity worth＜250 second, viscose is done fracture strength 〉=2.4CN/dtex, and wet breaking strength 〉=1.5CN/dtex filters KW value 60-100ml.
In bleaching process, use ozone and chlorine dioxide action-reaction medicament, the ozone bleaching strong adaptability, temperature is low, and the dissolved matter after the bleaching only is the catabolite of lignin and carbohydrate, and chlorine dioxide reacts with lignin selectively and removes lignin; And cellulose degradation is few, and fiber fines produces few, the organic chloride content that decrease toxicity is large.Thereby greatly alleviated the pollution that bleaching waste liquor causes, bleaching effluent COD＜30kg/t air dried pulp, AOX＜0.08kg/t air dried pulp.
By above technical scheme, the delignification, dynamic viscosity adjustment, raising whiteness, the minimizing fiber fines that have carried out targetedly substep to not floating bamboo wood dissolving pulp produce, have activated respond, on the basis of improving the quality such as fibre strength, whiteness, strainability, reduced the pollutional load of bleaching effluent, product quality height, the low bamboo wood dissolving pulp of environmental pollution have been made, for viscose production provides high-quality raw material.
By bleaching bamboo wood dissolving pulp, viscose, the bleaching effluent that above technical scheme makes, as follows with conventional CEH Bleaching Quality contrast:
Specific embodiments
The invention will be further described below in conjunction with embodiment.
The low method for bleaching that pollutes bamboo wood dissolving pulp of this preparation high-quality that the present invention provides includes following steps.
1, removes heteroproteose cell.
The existence of heteroproteose cell has destroyed the intensity of pulping, has reduced the one-tenth pulp brightness, and the raising of the reactivity worth of restriction removes heteroproteose cell and is conducive to improve reactivity worth, is conducive to improve the spinnability of fiber, improves fibre strength and whiteness.Heteroproteose cell remove screening, the pulp washing method of mainly containing.
Embodiment 1.
Screening the pulp concentration 0.7%.
Sieve plate specification Φ 0.10mm.
Pulp purity: 200kgCOD/adt.
Embodiment 2.
Screening the pulp concentration 2.5%.
Sieve plate specification Φ 2.5mm.
Pulp purity: 100kgCOD/adt.
Embodiment 3.
Sizing concentration 0.5%.
Temperature 50 C.
Pulp purity: 150kgCOD/adt.
Embodiment 4.
Sizing concentration 3.0%.
Temperature: 90 ℃.
Pulp purity: 120kgCOD/adt.
2, oxidation reaction.
(1) acidifying preliminary treatment.
Add pretreating agent in removing the disposed slurry of heteroproteose cell, finishing agent can be inorganic acid, also can be organic acid.
Embodiment 5.
Pretreating agent: hydrochloric acid.
Pretreatment reaction PH :≤6.
Pretreatment time: 40 minutes.
Pretreatment temperature: 60 ℃.
Measure 1kg/adt with acid.
Amount of chelant: 1 ‰.
Embodiment 6.
Pretreating agent: sulfuric acid.
Pretreatment reaction PH :≤4.
Pretreatment time: 25 minutes.
Pretreatment temperature: 40 ℃.
Measure 2kg/adt with acid.
Amount of chelant: 1.5 ‰.
Embodiment 7.
Pretreating agent: hydrochloric acid.
Pretreatment reaction PH :≤2.
Pretreatment time: 10 minutes.
Pretreatment temperature: 20 ℃.
Measure 3kg/adt with acid.
Amount of chelant: 2 ‰.
(2) oxygen delignification.
To evenly mix with oxygen and be placed in the oxygen reactor through the pretreated bamboo wood dissolving pulp that do not float, make oxygen and slurry generation oxidation, decoloring reaction, continue to remove the residual lignin in the brown stock material after the boiling, improve slurry purity, and dynamic viscosity is slightly descended.
Embodiment 8.
The oxygen reaction time: 30 minutes.
Reaction temperature: 50 ℃.
Oxygen consuming amount: 0.5%.
Dynamic viscosity fall off rate: 5%.
Purity behind the pulp washing: 100kgCOD/adt.
Embodiment 9.
The oxygen reaction time: 60 minutes.
Reaction temperature: 80 ℃.
Oxygen consuming amount: 1.5%.
Dynamic viscosity fall off rate: 10%.
Purity behind the pulp washing: 80kgCOD/adt.
Embodiment 10.
The oxygen reaction time: 90 minutes.
Reaction temperature: 105 ℃.
Oxygen consuming amount: 2.0%
Dynamic viscosity fall off rate: 15%.
Purity behind the pulp washing: 60kgCOD/adt.
(3) ozone bleaching.
Slurry through washing enters ozone reactor, reacts with ozone.
Embodiment 11.
Ozone consumption: 0.4%.
Reaction time: 10 minutes.
Temperature: 20 ℃.
Ozone concentration: 1.5%.
Purity behind the pulp washing: 50kgCOD/adt.
Embodiment 12.
Ozone consumption: 0.7%.
Reaction time: 5 minutes.
Temperature: 40 ℃.
Ozone concentration: 2.5%.
Purity behind the pulp washing: 40kgCOD/adt.
Embodiment 13.
Ozone consumption: 1.0%.
Reaction time: 1 minute.
Temperature: 60 ℃.
Ozone concentration: 3.5%.
Purity behind the pulp washing: 30kgCOD/adt.
3, the alkali refining of strengthening.
Embodiment 14.
The alkali refining time: 30 minutes.
PH：14。
Temperature: 60 ℃.
Hydrogen peroxide (H
2
O
2
) consumption: 0.25%.
Oxygen (O) consumption: 0.2%.
Wash rear alkalinity: 0.06 g/l.
Embodiment 15.
The alkali refining time: 60 minutes.
PH：10.5。
Temperature: 75 ℃.
Hydrogen peroxide (H
2
O
2
) consumption: 0.75%.
Wash rear alkalinity: 0.04 g/l.
Embodiment 16.
The alkali refining time: 90 minutes.
PH：12。
Temperature: 90 ℃.
Oxygen (O) consumption: 0.6%.
Wash rear alkalinity: 0.03 g/l.
4, ClO 2 bleaching.
ClO 2 bleaching in carry out under the dense condition, ClO 2 bleaching herein also can be divided into two sections to carry out, and is called D1 section and D2 section, D1 section chlorine dosage accounts for the 55-80% of total chlorine amount; D2 section chlorine dosage accounts for the 20-45% of total chlorine amount.
Embodiment 17.
Chlorine: 0.8%.
Reaction density: 8%.
Reaction temperature: 60 ℃.
Reaction time: 80 minutes.
Reaction acidity: 0.08g/l.
Wash rear acid content: 0.005 g/l.
Embodiment 18.
Chlorine: 1.0%.
Reaction density: 10%.
Reaction temperature: 70 ℃.
Reaction time: 120 minutes.
Reaction acidity: 0.15g/l.
Wash rear acid content: 0.01 g/l.
Embodiment 19.
Chlorine: 1.5%.
Reaction density: 14%.
Reaction temperature: 80 ℃.
Reaction time: 160 minutes.
Reaction acidity: 0.20g/l.
Wash rear acid content: 0.02 g/l.
Embodiment 20.
Chlorine: 1.2%.
Reaction density: 12%.
Reaction temperature: 68 ℃.
The D1 section.
Chlorine dosage accounts for 60% of total chlorine amount.
Reaction time: 100 minutes.
Reaction acidity: 0.10g/l.
Wash rear acid content: 0.02 g/l.
The D2 section.
D2 section chlorine dosage accounts for 40% of total chlorine amount.
Reaction time: 60 minutes.
Reaction acidity: 0.10g/l.
Wash rear acid content: 0.01 g/l.
5, high temperature acidified processing.
(high temperature peracid) treatment process of use strengthening not only can reduce ash and irony, can also remove pentose in the dissolving pulp, glycal aldehydic acid, thereby greatly improves the respond of pulp, for the yellow glue provides the high-quality pulp.Acid treatment is carried out with hydrochloric acid or sulfuric acid.
Embodiment 21.
Acidizer: hydrochloric acid.
Reaction density: 4%.
Reaction temperature: 50 ℃.
Reaction time: 30 minutes.
Reaction acidity: 0.8g/l.
Wash rear acid content: 0.1 g/l.
Embodiment 22.
Acidizer: sulfuric acid.
Reaction density: 6%.
Reaction temperature: 65 ℃.
Reaction time: 60 minutes.
Reaction acidity: 1.4g/l.
Wash rear acid content: 0.015 g/l.
Embodiment 23.
Acidizer: hydrochloric acid.
Reaction density: 8%.
Reaction temperature: 80 ℃.
Reaction time: 90 minutes.
Reaction acidity: 1.8g/l.
Wash rear acid content: 0.02 g/l.
Should be pointed out that in this specific embodiment of listing it only is illustrative, and do not mean that the scope of the invention is limited that protection scope of the present invention is as the criterion with appending claims.
Claims (2)
1. one kind prepares the low method for bleaching that pollutes bamboo wood dissolving pulp of high-quality, it is characterized in that including following steps:
(1) remove heteroproteose cell:
Adopt screening or pulp washing method to carry out removing of heteroproteose cell, wherein:
Screening: screening the pulp concentration 0.7-2.5%, sieve plate specification Φ 0.10-2.5mm, pulp purity≤200kgCOD/adt; Or
Pulp washing method: sizing concentration 0.5-3.0%, temperature 50-90 ℃, pulp purity≤200kgCOD/adt;
(2) oxidation reaction:
1) acidifying preliminary treatment:
Add pretreating agent in removing the disposed slurry of heteroproteose cell, pretreating agent is inorganic acid or organic acid, and technological parameter is:
Pretreatment reaction PH :≤6,
Pretreatment time: 10-40 divides,
Pretreatment temperature: 20-60 ℃
With acid amount 1-3 kg/adt,
Amount of chelant: 1-2 ‰;
2) oxygen delignification:
To evenly mix with oxygen and be placed in the oxygen reactor through the pretreated bamboo wood dissolving pulp that do not float, make oxygen and slurry generation oxidation, decoloring reaction, continue to remove the residual lignin in the brown stock material after the boiling, improve slurry purity, and dynamic viscosity is descended, technological parameter is:
The oxygen reaction time: 30-90 divides,
Reaction temperature: 50-105 ℃,
Oxygen consuming amount: 0.5-2.0%
Dynamic viscosity fall off rate: 5-15%
Purity behind the pulp washing :≤100kgCOD/adt;
3) ozone bleaching:
Slurry through washing enters ozone reactor, reacts with ozone, and technological parameter is:
Ozone consumption: 0.4-1.0%,
Reaction time: 1-10 divides;
Temperature: 20-60 ℃,
Ozone concentration: 1.5-3.5%,
Purity behind the pulp washing :≤50kgCOD/adt;
(3) alkali refining of strengthening:
The alkali refining medium is highly basic NaOH, with oxygen (O) and/or hydrogen peroxide (H
2O
2) reinforced alkaline is refining, technological parameter is:
The alkali refining time: 30-90 divides,
PH：10.5-14，
Temperature: 60-90 ℃,
Hydrogen peroxide (H
2O
2) consumption: 0.25-0.75%,
Oxygen (O) consumption: 0.2-0.6%,
Wash rear alkalinity :≤0.06 g/l;
(4) ClO 2 bleaching:
Adopt element chlorine free bleaching behind the alkali refining, bleaching agent is chlorine dioxide, ClO 2 bleaching in carry out under the dense condition, technological requirement is:
Chlorine: 0.8-1.5%,
Reaction density: 8-14%
Reaction temperature: 60-80 ℃,
Reaction time: 80-160 divides;
Reaction acidity: 0.08-0.20g/l,
Wash rear acid content :≤0.02 g/l;
(5) high temperature acidified processing
Process slurry with hydrochloric acid or sulfuric acid, technological parameter is:
Reaction density: 4-8%
Reaction temperature: 50-80 ℃,
Reaction time: 30-90 divides,
Reaction acidity: 0.8-1.8g/l,
Wash rear acid content :≤0.02 g/l.
2. described preparation high-quality hangs down the method for bleaching that pollutes bamboo wood dissolving pulp according to claim 1, it is characterized in that described ClO 2 bleaching step is divided into two sections and carries out, and is called D1 section and D2 section, and D1 section chlorine dosage accounts for the 55-80% of total chlorine amount; D2 section chlorine dosage accounts for the 20-45% of total chlorine amount.
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| CN112359631A (en) * | 2020-10-29 | 2021-02-12 | 陕西科技大学 | Method for bleaching chlorine-free bamboo pulp |
| CN114908596A (en) * | 2022-04-26 | 2022-08-16 | 赣南师范大学 | Method for preparing dissolving pulp by bleaching bamboo pulp, dissolving pulp and application thereof |
| CN117306291A (en) * | 2023-09-27 | 2023-12-29 | 中国制浆造纸研究院有限公司 | A flexible pulping method for dissolving pulp |
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| CN104790241B (en) * | 2015-05-12 | 2016-08-17 | 四川理工学院 | A kind of clean method for preparing of high-purity high-quality bamboo wood dissolving pulp |
| CN110629576A (en) * | 2019-08-27 | 2019-12-31 | 齐鲁工业大学 | A method for preparing dissolving pulp by full chlorine-free bleaching of poplar kraft pulp |
| CN110629576B (en) * | 2019-08-27 | 2022-04-12 | 齐鲁工业大学 | Method for preparing dissolving pulp by completely chlorine-free bleaching of poplar sulfate pulp |
| CN112359631A (en) * | 2020-10-29 | 2021-02-12 | 陕西科技大学 | Method for bleaching chlorine-free bamboo pulp |
| CN114908596A (en) * | 2022-04-26 | 2022-08-16 | 赣南师范大学 | Method for preparing dissolving pulp by bleaching bamboo pulp, dissolving pulp and application thereof |
| CN114908596B (en) * | 2022-04-26 | 2024-02-09 | 赣南师范大学 | Method for preparing dissolving pulp from bleached bamboo pulp, dissolving pulp and its application |
| CN117306291A (en) * | 2023-09-27 | 2023-12-29 | 中国制浆造纸研究院有限公司 | A flexible pulping method for dissolving pulp |
| CN117306291B (en) * | 2023-09-27 | 2026-03-13 | 中国制浆造纸研究院有限公司 | A flexible pulping method for dissolving pulp |
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