CN104611971A - A system and a method for bleaching bagasse pulp with chlorine dioxide - Google Patents
A system and a method for bleaching bagasse pulp with chlorine dioxide Download PDFInfo
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- CN104611971A CN104611971A CN201410796802.8A CN201410796802A CN104611971A CN 104611971 A CN104611971 A CN 104611971A CN 201410796802 A CN201410796802 A CN 201410796802A CN 104611971 A CN104611971 A CN 104611971A
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- bleaching
- section
- tower
- bagasse pulp
- pulp
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/12—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds
- D21C9/14—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds with ClO2 or chlorites
- D21C9/142—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds with ClO2 or chlorites with ClO2/Cl2 in a multistage process involving ClO2/Cl2 exclusively
Abstract
A system and a method for bleaching bagasse pulp with chlorine dioxide are disclosed. The system comprises bleaching towers used for bleaching the bagasse pulp, washing devices used for performing bagasse pulp cleaning steps and pipelines for guiding the bagasse pulp to flow. The method adopts the chlorine dioxide as a main bleaching agent, includes steps of D0 section bleaching, Ep section alkalization, D1 section bleaching, and the like, and overcomes the problems of traditional chlorine-containing bleaching systems and methods, namely severe water consumption and discharge of substances with severe toxicity. Compared with traditional methods, after bleaching, whiteness and viscosity of the pulp are improved, yellowing is reduced, the quality of the bagasse pulp is obviously improved, a water saving effect is obvious, organic chloride compounds (AOX) produced by chlorine-containing bleaching are reduced, the bleaching is more selective, washing water can be circulated and used, the COD and the discharge amount of middle-section wastewater are reduced, and requirements on energy conservation, emission reduction and clean production are satisfied.
Description
Technical field
The present invention relates to a kind of element chlorine free bleaching Apparatus and method in bagasse pulp production process, particularly a kind of bagasse pulp ClO 2 bleaching system and method.
Background technology
Bagasse is the distinctive fibrous raw material in Guangxi, utilizes bagasse to carry out pulping and paper-making, has very ripe experience in Guangxi.At present, the slurrying of China's non-wood fiber still generally uses traditional chlorine bleach technique.Traditional chlorine bleach, particularly CEH tri-stage bleaching waste water, except containing higher COD, BOD, also containing a large amount of organic chlorides (AOX), the general toxicity of these organic chlorides is stronger, part organic chloride belongs to carcinogenic, teratogenesis and mutagenic " three cause " material (be as bioxin), and be difficult to biochemical degradation; The Non-toxic process of these organic chlorides is more difficult, is discharged in rivers water body and can causes more serious environmental pollution; Secondly because traditional chlorine bleach technique contains chlorine, waste water not easily reuses, and causes water consumption large; More troublesome, in chlorination C section, because chlorine does not have selective to the lignin in slurry, in reduction slurry, also use cellulose to be reduced while lignin, the intensity of slurry is declined.Therefore, traditional chlorine bleach process not only makes Pulping Middle-stage Wastewater Pollution serious, also makes the development of non-wood fiber slurrying receive serious restriction simultaneously.
Domestic patent data discloses many about traditional chlorine bleach technique (or system) patented technology:
The free pulping method of such as [title] a kind of low polymerization degree bamboo pulp; [application number] CN201410024665.6, [applicant] Sichuan University of Science & Engineering; [summary] the invention belongs to the cleaning pulping field of bamboo pulp, particularly relate to a kind of free pulping method of low polymerization degree bamboo pulp, utilize true qualities sulfate bamboo pulp (hereinafter referred to as KP bamboo pulp) for raw material production bamboo pulp for cellulose viscose, also can be used for production of cellulose derivative product.Comprise the following steps: raw material preparation, alkaline cooking, concentrated, oxygen bleaching, bleaching and cellulase treatment-chlorine dioxide are once bleached-EOP bleaching-chlorine dioxide secondary and bleached and ferment treatment step.This invented technology flow process is simple, production efficiency is high, production capacity is large, pulping yield rate is high, the bamboo pulp produced can meet the requirement that viscose is produced completely, also can be used for production of cellulose derivative product, but containing higher COD, BOD and organic chloride (AOX) in bleaching effluent, environment structure is endangered.
Such as [title] CEH bleaching waste liquor wet method improves the method for bagasse alkaline cooking effect, [patent No.] CN200910094429.0, [patentee] Kunming University of Science and Technology, [summary] the invention discloses a kind of bagasse wet method stacked arrangement of bagasse alkaline cooking pre-treatment, using Bagasse Pulp CEH substituting as clear water, the wet method being back to use bagasse respectively stores up process, then carry out the alkaline cooking of bagasse, its processing step is: get C, E, the washes of H tri-stage bleaching sprays the bagasse stored up in stock ground and piles, leakage water is had to flow out to bottom, bagasse after spray 10 ~ 20 is through discharging, feeding, washing, boiling vessel is conveyed into after dehydration, at NaOH consumption 14 ~ 16%, anthraquinone consumption 0.01 ~ 0.3%, weight liquor ratio 1: 3 ~ 6, boiling temperature 155 ~ 160 DEG C, heat up 70 ~ 110min, boiling is carried out under the condition of insulation 60 ~ 90min.Bagasse pulp yield 2 ~ 5 percentage points can be improved, reduce organic chloride 22 ~ 31%, ton slurry water consumption decline 8 ~ 15m3.This invention is bleached bleaching process to CEH and is improved, but still containing certain COD, BOD and organic chloride (AOX) in bleaching effluent.
The such as preparation method of [title] a kind of bleaching straw pulp; [application number] CN201310177495.0, [applicant] Kunming University of Science and Technology, Longjiang, Jiamusi Fu Jiangzhi Co., Ltd; [summary] the invention discloses a kind of preparation method of bleaching straw pulp, the method comprises following operation: 1) grass as raw material and cooking liquor to be added in digesting apparatus with the weight ratio of 1:3-1:6 and to mix, then digesting apparatus is airtight, wherein, containing alkali in described cooking liquor; 2) in described airtight digesting apparatus, passing into oxygen makes oxygen pressure in digesting apparatus remain 0.3-1.0MPa, by described grass as raw material described cooking liquor boiling 30-240 minute at 90-130 DEG C; (3) slurry obtained after completing digestion process is carried out washing and screening, obtain screened stock; 4) the screened stock chlorine dioxide in described operation (3) is bleached.This invention is same as the further improvement to CEH bleaching process, two sections of driftages that the CEH bleaching process usually adopted than common alkaline straw-pulp is few, but still on Wastewater Pollutant content, does not have remarkable breakthrough.
Therefore the production water consumption that traditional traditional chlorine bleach system exists is serious, and the problem, particularly CEH tri-stage bleaching waste water of discharge extremely toxic substance, except containing except higher COD, BOD, the more important thing is containing a large amount of organic chlorides (AOX).Therefore need to improve further traditional bagasse pulp bleaching system and method.
Summary of the invention
The production water consumption that the object of the invention is to solve traditional bagasse pulp chlorine bleach system and method existence is serious, the problem of discharge extremely toxic substance, provide the bagasse pulp ClO 2 bleaching system that a set of water consumption is low, toxic emission is few, additionally provide the method utilizing this system bleaching bagasse pulp.
Bagasse pulp ClO 2 bleaching system of the present invention, comprises the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill performing bagasse pulp matting and guiding bagasse pulp.Described bleaching tower comprises tri-stage bleaching structure---the alkalization of D0 section bleaching tower, Ep section tower, D1 section bleaching tower.The downstream line of every section of bleaching tower connects wash mill.D0 section bleaching tower upstream line connects screenings entrance, and this place's pipeline is also provided with bleaching agent inlet.The upstream line of Ep section alkalization tower is disposed with alkali liquor inlet and hydrogen peroxide entrance, and the upstream line of D1 section bleaching tower is also provided with bleaching agent inlet.Bleaching system pipe end is screenings outlet.
As further illustrating of bagasse pulp ClO 2 bleaching system of the present invention, described wash mill is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and be that slag starches cleaning machine front by the sequence in operation, slag slurry screening machine is rear.
As further illustrating of bagasse pulp ClO 2 bleaching system of the present invention, the bagasse pulp injection end of described D0 section bleaching tower, Ep section alkalization tower, D1 section bleaching tower is also provided with blender, has the effect of fully mixing bagasse pulp and medicament.
Bagasse pulp ClO 2 bleaching system of the present invention can also make following improvement, and described D0 section bleaching tower is dense reaction tower in up-flow, and Ep section alkalization tower is for rise-falling streaming alkalization tower, and D1 section bleaching tower is up-flow bleaching tower.
As the further improvement explanation of bagasse pulp ClO 2 bleaching system of the present invention, described system unit is provided with remote interface units, and the Programmable Logic Controller outside remote interface units and system, industrial control computer form network monitoring system by respective communication process plate bus.
Utilize above system to carry out the method for bagasse pulp ClO 2 bleaching, namely using chlorine dioxide as main bleaching agent, form D0-Ep-D1 bleaching process method, comprise the following steps:
(1) D0 section bleaching, add chlorine dioxide oven dry stock to not floating in bagasse pulp, the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 33 ~ 40 kg, and wherein chlorine dioxide oven dry stock is containing effective chlorine with being 78 ~ 80%, adds middle pressure steam simultaneously; Medicament and bagasse pulp enter D0 section bleaching tower and react after blender mixes, and add antichlor and remove residual chlorine in slurry and wash after having reacted.Reaction temperature controls at 45 ~ 55 DEG C, reaction time 40min, and going out D0 tower pulp brightness is 50 ~ 55%ISO.
(2) Ep section alkalization, NaOH and hydrogen peroxide oven dry stock is added successively to the D0 section bagasse pulp after washing, the NaOH oven dry stock addition of bagasse pulp per ton is 11 ~ 14 kg, hydrogen peroxide oven dry stock addition is 20 ~ 30 kg, wherein NaOH oven dry stock concentration is 100%, and hydrogen peroxide oven dry stock concentration is 27.5%; Add middle pressure steam, medicament and bagasse pulp enter the Ep section tower that alkalizes and react after blender mixes, and have reacted rear washing simultaneously.Reaction temperature controls at 65 ~ 75 DEG C, and bagasse pulp first reacts 25min with NaOH, then reacts 95min with hydrogen peroxide, and going out Ep tower pulp brightness is 70 ~ 75%ISO.
(3) D1 section bleaching, in after washing, dense bagasse pulp adds chlorine dioxide oven dry stock, and the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 8 ~ 11 kg/t oven dry stocks, wherein chlorine dioxide oven dry stock containing effective chlorine with being 20 ~ 22%, add middle pressure steam simultaneously, add middle pressure steam simultaneously; Medicament and bagasse pulp enter D1 section bleaching tower and react after blender mixes, and add antichlor after having reacted and remove residual chlorine in slurry and wash, reaction temperature controls at 60 ~ 65 DEG C, and the reaction time is about 180min, and going out D1 tower pulp brightness is more than 82%ISO.
Bagasse pulp ClO 2 bleaching system and method for the present invention, instead of original chlorine bleach system and method, namely replace chlorine and calcium hypochlorite in former bagasse pulp bleaching production procedure with chlorine dioxide, add hydrogen peroxide in alkali treatment section, the technique effect brought thus:
(1) compare traditional traditional chlorine bleach system and method, after drift, pulp brightness raising, viscosity improve, and brightness reversion reduces, and the quality of bagasse pulp is obviously improved.
(2) paper pulp produced more environmental protection, as multiple paper for daily use raw materials such as toilet paper, cup paper, paper dishware.
(3) bagasse pulp ClO 2 bleaching system and method for the present invention, dense during technological reaction condition is, and water-saving result is obvious, meets energy-saving and emission-reduction and cleanly production requirement.
(4) bagasse pulp ClO 2 bleaching system and method for the present invention, decrease chlorine bleach and produce organic chloride (AOX), make bleaching have more selective, washings can recycle simultaneously, reduce middle-stage wastewater COD discharge capacity.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.
Fig. 1 is bagasse pulp ClO 2 bleaching system syndeton schematic diagram of the present invention.
In figure: 1-screenings entrance; 2-D0 section bleaching tower; 3-wash mill; 4-Ep section alkalization tower; 5-hydrogen peroxide entrance; 6-D1 section bleaching tower; 7-alkali liquor inlet; 8-screenings exports; 9-bleaching agent inlet.
Fig. 2 is the process chart of bagasse pulp ClO 2 bleaching method of the present invention.
Detailed description of the invention
As shown in Figure 1, 2, bagasse pulp ClO 2 bleaching system of the present invention, comprises the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill 3 performing bagasse pulp matting and guiding bagasse pulp; Described bleaching tower comprises tri-stage bleaching structure---the alkalization of D0 section bleaching tower 2, Ep section tower 4, D1 section bleaching tower 6; The downstream line of every section of bleaching tower connects wash mill; D0 section bleaching tower upstream line connects screenings entrance 1, and this place's pipeline is also provided with bleaching agent inlet 9; The upstream line that the upstream line of Ep section alkalization tower is disposed with alkali liquor inlet 7 and hydrogen peroxide entrance 5, D1 section bleaching tower is also provided with bleaching agent inlet; Bleaching system pipe end is screenings outlet 8.
Described wash mill 3 is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and be that slag starches cleaning machine front by the sequence in operation, slag slurry screening machine is rear.
The bagasse pulp injection end of described D0 section bleaching tower 2, Ep section alkalization tower 4, D1 section bleaching tower 6 is also provided with blender, has the effect of fully mixing bagasse pulp and medicament.
Described D0 section bleaching tower 2 is dense reaction tower in up-flow, and Ep section alkalization tower 4 is for rise-falling streaming alkalization tower, and D1 section bleaching tower 6 is up-flow bleaching tower.
Described system unit is provided with remote interface units, and the Programmable Logic Controller outside remote interface units and system, industrial control computer form network monitoring system by respective communication process plate bus.
Embodiment 1: brown stock enters bagasse pulp ClO 2 bleaching system of the present invention after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 34.7 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 11.9 kg/t oven dry stocks (with 100% densimeters), it is 23 kg/t oven dry stocks (with 27.5% densimeters) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 9.5 kg/t oven dry stocks (effective chlorine meters), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 83.6%, and qualification rate is 99.5%.
Embodiment 2: brown stock enters bagasse pulp ClO 2 bleaching system of the present invention after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 36.7 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 12.6 kg/t oven dry stocks (with 100% densimeters), it is 27kg/t oven dry stock (with 27.5% densimeter) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 9.9kg/t oven dry stock (effective chlorine meter), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 84.8%, and qualification rate is 99.6%.
Embodiment 3: brown stock enters bagasse pulp ClO 2 bleaching system of the present invention after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 38.9 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 12.8 kg/t oven dry stocks (with 100% densimeters), it is 30kg/t oven dry stock (with 27.5% densimeter) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 10.5kg/t oven dry stock (effective chlorine meter), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 85.8%, and qualification rate is 99.8%.
Claims (6)
1. a bagasse pulp ClO 2 bleaching system, comprises the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill (3) performing bagasse pulp matting and guiding bagasse pulp; It is characterized in that: described bleaching tower comprises tri-stage bleaching structure---D0 section bleaching tower (2), Ep section alkalization tower (4), D1 section bleaching tower (6); The downstream line of every section of bleaching tower connects wash mill; D0 section bleaching tower upstream line connects screenings entrance (1), and this place's pipeline is also provided with bleaching agent inlet (9); The upstream line of Ep section alkalization tower is disposed with alkali liquor inlet (7) and hydrogen peroxide entrance (5), and the upstream line of D1 section bleaching tower is also provided with bleaching agent inlet; Bleaching system pipe end is screenings outlet (8).
2. bagasse pulp ClO 2 bleaching system according to claim 1, it is characterized in that: described wash mill (3) is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and by the sequence in operation be slag slurry cleaning machine front, slag slurry screening machine rear.
3. bagasse pulp ClO 2 bleaching system according to claim 1, it is characterized in that: the bagasse pulp injection end of described D0 section bleaching tower (2), Ep section alkalization tower (4), D1 section bleaching tower (6) is also provided with blender, there is the effect of fully mixing bagasse pulp and medicament.
4. according to the arbitrary described bagasse pulp ClO 2 bleaching system of claim 1-3, it is characterized in that: described D0 section bleaching tower (2) is reaction tower dense in up-flow, Ep section alkalization tower (4) is for rise-falling streaming alkalization tower, and D1 section bleaching tower (6) is up-flow bleaching tower.
5. bagasse pulp ClO 2 bleaching system according to claim 4, it is characterized in that: described system unit is provided with remote interface units, the Programmable Logic Controller outside remote interface units and system, industrial control computer form network monitoring system by respective communication process plate bus.
6. utilize claim 1 the method for bagasse pulp ClO 2 bleaching system bleaching bagasse pulp, the method is using chlorine dioxide as main bleaching agent, forms D0-Ep-D1 bleaching process method, it is characterized in that comprising the following steps:
(1) D0 section bleaching: add chlorine dioxide oven dry stock to not floating in bagasse pulp, the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 33 ~ 40 kg, wherein chlorine dioxide oven dry stock is containing effective chlorine with being 78 ~ 80%, adds middle pressure steam simultaneously; Medicament and bagasse pulp enter D0 section bleaching tower and react after blender mixes, and add antichlor and remove residual chlorine in slurry and wash after having reacted; Reaction temperature controls at 45 ~ 55 DEG C, reaction time 40min, and going out D0 tower pulp brightness is 50 ~ 55%ISO;
(2) Ep section alkalization: add NaOH and hydrogen peroxide oven dry stock successively to the D0 section bagasse pulp after washing, the NaOH oven dry stock addition of bagasse pulp per ton is 11 ~ 14 kg, hydrogen peroxide oven dry stock addition is 20 ~ 30 kg, wherein NaOH oven dry stock concentration is 100%, and hydrogen peroxide oven dry stock concentration is 27.5%; Add middle pressure steam, medicament and bagasse pulp enter the Ep section tower that alkalizes and react after blender mixes, and have reacted rear washing simultaneously; Reaction temperature controls at 65 ~ 75 DEG C, and bagasse pulp first reacts 25min with NaOH, then reacts 95min with hydrogen peroxide, and going out Ep tower pulp brightness is 70 ~ 75%ISO;
(3) D1 section bleaching: in after washing, dense bagasse pulp adds chlorine dioxide oven dry stock, the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 8 ~ 11 kg/t oven dry stocks, wherein chlorine dioxide oven dry stock is containing effective chlorine with being 20 ~ 22%, adds middle pressure steam simultaneously, adds middle pressure steam simultaneously; Medicament and bagasse pulp enter D1 section bleaching tower and react after blender mixes, and add antichlor and remove residual chlorine in slurry and wash after having reacted; Reaction temperature controls at 60 ~ 65 DEG C, and the reaction time is about 180min, and going out D1 tower pulp brightness is more than 82%ISO.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410796802.8A CN104611971A (en) | 2014-12-22 | 2014-12-22 | A system and a method for bleaching bagasse pulp with chlorine dioxide |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410796802.8A CN104611971A (en) | 2014-12-22 | 2014-12-22 | A system and a method for bleaching bagasse pulp with chlorine dioxide |
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| CN104611971A true CN104611971A (en) | 2015-05-13 |
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| CN201410796802.8A Pending CN104611971A (en) | 2014-12-22 | 2014-12-22 | A system and a method for bleaching bagasse pulp with chlorine dioxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105040500A (en) * | 2015-09-06 | 2015-11-11 | 长沙理工大学 | Elemental chlorine free bleaching method of reed pulp |
| CN108118552A (en) * | 2017-11-22 | 2018-06-05 | 云南新平南恩糖纸有限责任公司 | Bagasse paper production line |
| CN115948928A (en) * | 2023-02-15 | 2023-04-11 | 宜宾五粮液股份有限公司 | Bleaching and pulping process of waste distiller's grains of white spirit |
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| CN1401848A (en) * | 2002-08-01 | 2003-03-12 | 山东轻工业学院 | Paper pulp bleaching process |
| CN101545229A (en) * | 2009-05-06 | 2009-09-30 | 广西大学 | ClO2 bleaching method of bagasse pulp |
| EP1644574B1 (en) * | 2003-06-30 | 2013-03-06 | Andritz Oy | Method for treating pulp in connection with the bleaching of chemical pulp |
| CN204570365U (en) * | 2014-12-22 | 2015-08-19 | 南宁糖业股份有限公司 | A kind of bagasse pulp ClO 2 bleaching system |
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2014
- 2014-12-22 CN CN201410796802.8A patent/CN104611971A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1401848A (en) * | 2002-08-01 | 2003-03-12 | 山东轻工业学院 | Paper pulp bleaching process |
| EP1644574B1 (en) * | 2003-06-30 | 2013-03-06 | Andritz Oy | Method for treating pulp in connection with the bleaching of chemical pulp |
| CN101545229A (en) * | 2009-05-06 | 2009-09-30 | 广西大学 | ClO2 bleaching method of bagasse pulp |
| CN204570365U (en) * | 2014-12-22 | 2015-08-19 | 南宁糖业股份有限公司 | A kind of bagasse pulp ClO 2 bleaching system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105040500A (en) * | 2015-09-06 | 2015-11-11 | 长沙理工大学 | Elemental chlorine free bleaching method of reed pulp |
| CN108118552A (en) * | 2017-11-22 | 2018-06-05 | 云南新平南恩糖纸有限责任公司 | Bagasse paper production line |
| CN115948928A (en) * | 2023-02-15 | 2023-04-11 | 宜宾五粮液股份有限公司 | Bleaching and pulping process of waste distiller's grains of white spirit |
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Application publication date: 20150513 |