CN108277674A - A kind of bleaching process of high whiteness bamboo pulp - Google Patents
A kind of bleaching process of high whiteness bamboo pulp Download PDFInfo
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- CN108277674A CN108277674A CN201810090171.6A CN201810090171A CN108277674A CN 108277674 A CN108277674 A CN 108277674A CN 201810090171 A CN201810090171 A CN 201810090171A CN 108277674 A CN108277674 A CN 108277674A
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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
- D21C9/1057—Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16
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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
- D21C9/02—Washing ; Displacing cooking or pulp-treating liquors contained in the pulp by fluids, e.g. wash water or other pulp-treating agents
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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
- 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
- D21C9/144—Bleaching ; Apparatus therefor with halogens or halogen-containing compounds with ClO2 or chlorites with ClO2/Cl2 and other bleaching agents in a multistage process
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Abstract
The present invention relates to pulping technology for paper-making fields, more particularly to a kind of bleaching process of high whiteness bamboo pulp, processing step includes two sections of delignification bleachings, for the first time washing, the ClO 2 bleaching under strong acid condition, addition bleaching boosters, hydrogen peroxide and oxygen boosting alkali density, third time washing, ClO 2 bleaching, the 4th washing and enzymatic treatment.Compared with prior art.After the present invention is cooperateed with using specifically enzymatic treatment is brightened, pulp brightness is up to 87 degree or more, compared with prior art common brightens enzymatic treatment, whiteness can be improved at least 3 degree or more, and stabilization will not there is a phenomenon where anti-yellow, and chemical bleaching agent Chlorine is down to 3kg/adm hereinafter, greatly reducing cost.
Description
Technical field
The present invention relates to pulping technology for paper-making fields, and in particular to a kind of bleaching process of high whiteness bamboo pulp.
Background technology
Dissolving pulp is widely used in the cellulose derivatives industries such as viscose rayon, nitrocellulose, acetate fiber of weaving, market
Demand is huge.Bamboo wood dissolving pulp wide market newly developed at present, can fill up the notch of China's dissolving pulp.However,
During paper-making pulping, the production equipment and technique of bamboo wood dissolving pulp fall behind relatively.In the prior art, the drift of bamboo wood dissolving pulp
White technique mainly uses traditional C~E containing chlorine~H (C~chlorine, E~alkali density, H~hypochlorite) tri-stage bleaching technique,
The tri-stage bleaching technique has following defect：1) tri-stage bleaching process consumes a large amount of bleaching agent (mainly chlorine dioxide, dioxygen
The chemical reagent such as water), not only make the cost of material of bleaching agent high, but also the contaminated wastewater generated is big, subsequent wastewater treatment at
This corresponding increase, to cause the production cost of slurrying high, production capacity is low；2) largely using in the waste water of bleaching agent, especially chlorine
Gas and hypochlorite will produce such as more than 40 kinds of organic chloride (AOX) of chloroform, dioxin in bleaching process, these have
Noxious material is not only carcinogenic, teratogenesis, toxicity are big but also difficult, constitutes and seriously threatens to ecological environment and health.As
It improves, pulp brightness is improved using enzyme is brightened although also having in the prior art, the existing enzyme that commonly brightens can only will be white
Degree improves 1~2 degree (about 85 degree of whiteness), if to be improved again to 86 degree or more of high whiteness, it is necessary to use two by increasing
Dosage (at least 4kg/admt or more) collective effect of oxidation chlorine bleach could realize that thus chemical bleaching agent dosage increases,
So that cost and pollution increasing, and high whiteness is difficult to stablize, and is easy to happen anti-Huang.
Invention content
In view of the above-mentioned deficiencies in the prior art, it is an object of the present invention to provide a kind of bleaching process of high whiteness bamboo pulp, make bamboo
Pulp brightness is up to 87 degree or more and whiteness is stablized.
To achieve the goals above, the present invention adopts the following technical scheme that：
A kind of bleaching process of high whiteness bamboo pulp, including following processing step are provided：
A, two sections of delignification bleachings：
A1) one section of delignification bleaching：
The caustic soda and 1~3kg/ for accounting for air dried pulp weight 2.0%~3.0% are added into the slurry after wash engine washing concentrating
The magnesium sulfate of admt is sent into first segment medium-consistency pulp mixer, in the first paragraph dense mixing after low-pressure steam is heated to 90~95 DEG C
20~25kg/admt oxygen mix is added in device and uniformly enters lifting/lowering streaming reaction tube afterwards, slurry is in lifting/lowering streaming reaction tube
The interior residence time is 5~10min；
A2) two sections of delignification bleachings：
The slurry come out from first segment downflow tower is sent into dense mixed in second segment after middle pressure steam is heated to 95~102 DEG C
Clutch, in second segment medium-consistency pulp mixer be added 20~25kg/admt oxygen mix it is uniform, send to upflow tower stop 60~
80min, slurry is spurted to oxygen and is taken off in blow bin after upflow tower top pressure reaches 300~600kPa, spare；
B, it washs for the first time：
The slurry that step a is obtained is spare after wash engine washing concentrating；
C, the ClO 2 bleaching under strong acid condition：
Then sulfuric acid is added in dense standpipe during the slurry that step b is obtained is sent into, it is 2.0~3.0 to adjust pH value, is then used
Slurry is heated to being sent into medium-consistency pulp mixer after 75~85 DEG C by steam, then into medium-consistency pulp mixer be added 6~10kg/admt,
The ClO 2 solution of a concentration of 9.0~10.0g/l is simultaneously uniformly mixed, and then slurry enters in upflow tower, from up-flow tower top
Portion's overflow to downflow tower, slurry is 120~150min in the residence time of upflow tower and downflow tower；
D, it washs for second：
Slurry is drawn to wash engine from downflow tower and is washed, concentrates, spare；
E, bleach boosters are added：
The model AP8138 that the slurry obtained after step d washings is produced in the addition Bark Mann of wash engine stern notch
Bleach boosters stoste, control bleach boosters additive amount is 0.2~0.3kg/admt, and temperature is 75~80 DEG C, and pH value is
11.5~12.0；
F, hydrogen peroxide and oxygen boosting alkali density：
Caustic soda, hydrogen peroxide and oxygen is added in wash engine stern notch in the slurry obtained after step d washings, adjusts pH value 11.5
Medium-consistency pulp mixer is sent into after~12 to be uniformly mixed, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower,
Slurry is 60~70min in the residence time of upflow tower and downflow tower, and temperature is 80~85 DEG C；
G, third time is washed：
Slurry after step e, f is sent to wash engine washing concentrating, spare；
H, ClO 2 bleaching：
Sulfuric acid is added in wash engine stern notch in the slurry obtained after step g washings, in being sent into after adjusting pH value 3.5~4.5
1~3kg/admt, the ClO 2 solution of a concentration of 9.0~10.0g/l and mixing are added into medium-consistency pulp mixer for dense mixer
Uniformly, then slurry enters in upflow tower, and from overflow at the top of upflow tower to downflow tower, slurry stops upflow tower and downflow tower
It is 250~300min to stay the time, and temperature is 80~85 DEG C；
When slurry is extracted out from bleaching action tower bottom, 0.5~2kg/admt, the thio sulphur of a concentration of 100~120g/l is added
Acid sodium solution neutralizes the residual chlorine that unreacted is complete in slurry；
I, the 4th washing：
Slurry after step h is sent to wash engine washing concentrating, spare；
J, enzymatic treatment is brightened：
The model that the slurry obtained after step i washings is produced in the addition Bark Mann of wash engine stern notch
BUZYME3500's brightens proenzyme liquid, and it is 0.16~0.25kg/admt that enzyme additive amount is brightened in control, dense during then slurry is delivered to
Tower, controlled at 47~65 DEG C, pH value is 4.5~7.0, and the slurry after brightening enzymatic treatment is delivered to the storage of finished pulp tower
It deposits, it is spare.
Preferably, in the step j, brighten enzyme additive amount be 0.25kg/admt, dense tower during then slurry is delivered to,
Controlled at 50 DEG C, pH value 6.0.
Preferably, in the step j, brighten enzyme additive amount be 0.20kg/admt, dense tower during then slurry is delivered to,
Controlled at 58 DEG C, pH value 5.0.
Preferably, in the step j, brighten enzyme additive amount be 0.16kg/admt, dense tower during then slurry is delivered to,
Controlled at 62 DEG C, pH value 5.5.
Preferably, in the step e, bleach boosters additive amount is 0.25kg/admt, and temperature is 78 DEG C, and pH value is
11.8。
Preferably, in the step e, bleach boosters additive amount is 0.2kg/admt, and temperature is 75 DEG C, and pH value is
11.5。
Preferably, in the step e, bleach boosters additive amount is 0.3kg/admt, and temperature is 80 DEG C, and pH value is
12.0。
The beneficial effects of the invention are as follows：
A kind of bleaching process of high whiteness bamboo pulp of the present invention passes through two sections of delignification bleachings, washs for the first time, is strong successively
ClO 2 bleaching under the conditions of acid, second of washing, addition bleaching boosters, hydrogen peroxide and oxygen boosting alkali density, the
The bleaching process of washing, ClO 2 bleaching, the 4th washing and enzymatic treatment three times.Compared with prior art, have following excellent
Point：
(1) present invention determines use on the basis of traditional CEH tri-stage bleaching techniques by lot of experiments
The enzyme that brightens of the model BUZYME3500 of specific Bark Mann production carries out enzymatic treatment to bamboo pulp, and controls this and brighten enzyme
Additive amount is 0.16~0.25kg/admt, reaction temperature is 47~65 DEG C, and pH value is 4.5~7.0, makes to brighten at enzyme by this
Pulp brightness after reason is up to 87 degree or more, and compared with prior art common brightens enzymatic treatment, whiteness can be improved at least 3 degree with
On, and bamboo pulp whiteness is stablized at 87 degree or more, will not there is a phenomenon where anti-Huangs；
(2) present invention has advanced optimized two sections of delignifications, chlorine dioxide and hydrogen peroxide and oxygen boosting alkali density work
The process conditions of sequence, and the processing of synergic whitening enzyme, greatly reduce the dosages such as bleaching agent chlorine dioxide, hydrogen peroxide, make dioxy
The dosage for changing chlorine drops to 1~3kg/adm, and the dosage of hydrogen peroxide declines 1kg/admt, and therefore, bleaching process of the invention is significantly
Production cost is reduced, under conditions of manufacturing the pulpboard of high whiteness, the chemical bleachings agent such as chlorine dioxide can be greatly reduced
Usage amount reduces harmful substance and subsequent wastewater treatment difficulty in waste water, realizes the annual huge warp for saving about million yuan
Ji benefit；
(3) present invention can significantly improve the water filtering performance of slurry, reduce the water content of pulpboard by brightening enzymatic treatment,
Pulpboard water content is set to reduce about 1.5%, to be conducive to improve the production capacity of pulpboard.
Specific implementation mode
The invention will be further described with the following Examples.
Embodiment 1.
A kind of bleaching process of high whiteness bamboo pulp of the present invention, including following processing step：
A, two sections of delignification bleachings：
A1) one section of delignification bleaching：
The sulfuric acid of the caustic soda and 1kg/admt that account for air dried pulp weight 1.2% is added into the slurry after wash engine washing concentrating
Magnesium is sent into first segment medium-consistency pulp mixer after low-pressure steam is heated to 90 DEG C, and 20kg/ is added in dense mixer in the first paragraph
Admt oxygen mix uniformly enters lifting/lowering streaming reaction tube afterwards, and residence time of the slurry in lifting/lowering streaming reaction tube be
6min；
A2) two sections of delignification bleachings：
The slurry come out from first segment downflow tower is sent into second segment medium-consistency pulp mixer after middle pressure steam is heated to 95 DEG C,
It is uniform that 20kg/admt oxygen mix is added in second segment medium-consistency pulp mixer, send to upflow tower and stops 65min, slurry is flowing up
After top of tower pressure reaches 380kPa, spurts to oxygen and take off in blow bin, it is spare；
B, it washs for the first time：
The slurry that step a is obtained is spare after wash engine washing concentrating；
C, the ClO 2 bleaching under strong acid condition：
Dense standpipe in being sent into after the pulp concentration obtained after step b washings, is then added sulfuric acid, and it is 2.0 to adjust pH value,
Then slurry is heated to steam being sent into medium-consistency pulp mixer after 75 DEG C, 6kg/admt, dense is then added into medium-consistency pulp mixer
Degree is the ClO 2 solution of 9.0g/l and is uniformly mixed that then slurry enters in upflow tower, from overflow at the top of upflow tower to
Downflow tower, slurry are 120min in the residence time of upflow tower and downflow tower；
D, it washs for second：
Slurry is drawn to wash engine from downflow tower and is washed, concentrates, spare；
E, bleach boosters are added：
The model AP8138 that the slurry obtained after step d washings is produced in the addition Bark Mann of wash engine stern notch
Bleach boosters stoste, control bleach boosters additive amount be 0.2kg/admt, temperature be 75 DEG C, pH value 11.5；
F, hydrogen peroxide and oxygen boosting alkali density：
Caustic soda, hydrogen peroxide and oxygen is added in wash engine stern notch in the slurry obtained after step d washings, adjusts pH value 11.5
Medium-consistency pulp mixer is sent into after~12 to be uniformly mixed, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower,
Slurry is 60min in the residence time of upflow tower and downflow tower, and temperature is 8 DEG C；
G, third time is washed：
Slurry after step e, f is sent to wash engine washing concentrating, spare；
H, sulfuric acid is added in wash engine stern notch in the slurry obtained after step g washings, it is dense mixed in being sent into after adjusting pH value 3.5
Clutch, be added into medium-consistency pulp mixer 3kg/admt, a concentration of 9.0g/l ClO 2 solution and be uniformly mixed, then slurry
It enters in upflow tower, from upflow tower top overflow to downflow tower, slurry is in the residence time of upflow tower and downflow tower
250min, temperature are 80 DEG C；
When slurry is extracted out from bleaching action tower bottom, 1kg/admt, a concentration of 100g/l hypo solutions is added, in
The complete residual chlorine with unreacted in slurry；
I, the 4th washing：
Slurry after step h is sent to wash engine washing concentrating, spare；
J, enzymatic treatment is brightened：
The model that the slurry obtained after step i washings is produced in the addition Bark Mann of wash engine stern notch
BUZYME3500's brightens proenzyme liquid, and it is 0.25kg/admt, dense tower during then slurry is delivered to, control that enzyme additive amount is brightened in control
Temperature processed is 50 DEG C, pH value 6.0, and the slurry after brightening enzymatic treatment is delivered to the storage of finished pulp tower, spare.
Embodiment 2.
A kind of bleaching process of high whiteness bamboo pulp of the present invention, including following processing step：
A, two sections of delignification bleachings：
A1) one section of delignification bleaching：
The sulfuric acid of the caustic soda and 2kg/admt that account for air dried pulp weight 2.5% is added into the slurry after wash engine washing concentrating
Magnesium is sent into first segment medium-consistency pulp mixer after low-pressure steam is heated to 93 DEG C, and 22kg/ is added in dense mixer in the first paragraph
Admt oxygen mix uniformly enters lifting/lowering streaming reaction tube afterwards, and residence time of the slurry in lifting/lowering streaming reaction tube be
7min；
A2) two sections of delignification bleachings：
The slurry come out from first segment downflow tower is sent into second segment medium-consistency pulp mixer after middle pressure steam is heated to 98 DEG C,
It is uniform that 22kg/admt oxygen mix is added in second segment medium-consistency pulp mixer, send to upflow tower and stops 70min, slurry is flowing up
After top of tower pressure reaches 500kPa, spurts to oxygen and take off in blow bin, it is spare；
B, it washs for the first time：
The slurry that step a is obtained is spare after wash engine washing concentrating；
C, the ClO 2 bleaching under strong acid condition：
Dense standpipe in being sent into after the pulp concentration obtained after step b washings, is then added sulfuric acid, and it is 2.5 to adjust pH value,
Then slurry is heated to steam being sent into medium-consistency pulp mixer after 80 DEG C, 8kg/admt, dense is then added into medium-consistency pulp mixer
Degree is the ClO 2 solution of 9.5g/l and is uniformly mixed that then slurry enters in upflow tower, from overflow at the top of upflow tower to
Downflow tower, slurry are 135min in the residence time of upflow tower and downflow tower；
D, it washs for second：
Slurry is drawn to wash engine from downflow tower and is washed, concentrates, spare；
E, bleach boosters are added：
The model AP8138 that the slurry obtained after step d washings is produced in the addition Bark Mann of wash engine stern notch
Bleach boosters stoste, control bleach boosters additive amount be 0.25kg/admt, temperature be 78 DEG C, pH value 11.8；
F, hydrogen peroxide and oxygen boosting alkali density：
Caustic soda, hydrogen peroxide and oxygen is added in wash engine stern notch in the slurry obtained after step d washings, adjusts pH value 11.5
Medium-consistency pulp mixer is sent into after~12 to be uniformly mixed, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower,
Slurry is 65min in the residence time of upflow tower and downflow tower, and temperature is 83 DEG C；
G, third time is washed：
Slurry after step e, f is sent to wash engine washing concentrating, spare；
H, sulfuric acid is added in wash engine stern notch in the slurry obtained after step g washings, it is dense mixed in being sent into after adjusting pH value 4.0
Clutch, be added into medium-consistency pulp mixer 2kg/admt, a concentration of 9.6g/l ClO 2 solution and be uniformly mixed, then slurry
It enters in upflow tower, from upflow tower top overflow to downflow tower, slurry is in the residence time of upflow tower and downflow tower
280min, temperature are 82 DEG C；
When slurry is extracted out from bleaching action tower bottom, 1.5kg/admt, a concentration of 110g/l hypo solutions is added,
Neutralize the residual chlorine that unreacted is complete in slurry；
I, the 4th washing：
Slurry after step h is sent to wash engine washing concentrating, spare；
J, enzymatic treatment is brightened：
The model that the slurry obtained after step i washings is produced in the addition Bark Mann of wash engine stern notch
BUZYME3500's brightens proenzyme liquid, and it is 0.20kg/admt, dense tower during then slurry is delivered to, control that enzyme additive amount is brightened in control
Temperature processed is 58 DEG C, pH value 5.0, and the slurry after brightening enzymatic treatment is delivered to the storage of finished pulp tower, spare
Embodiment 3.
A kind of bleaching process of high whiteness bamboo pulp of the present invention, including following processing step：
A, two sections of delignification bleachings：
A1) one section of delignification bleaching：
The sulfuric acid of the caustic soda and 3kg/admt that account for air dried pulp weight 3.0% is added into the slurry after wash engine washing concentrating
Magnesium is sent into first segment medium-consistency pulp mixer after low-pressure steam is heated to 95 DEG C, and 25kg/ is added in dense mixer in the first paragraph
Admt oxygen mix uniformly enters lifting/lowering streaming reaction tube afterwards, and residence time of the slurry in lifting/lowering streaming reaction tube be
10min；
A2) two sections of delignification bleachings：
The slurry come out from first segment downflow tower is sent into second segment medium-consistency pulp mixer after middle pressure steam is heated to 100 DEG C,
It is uniform that 25kg/admt oxygen mix is added in second segment medium-consistency pulp mixer, send to upflow tower and stops 80min, slurry is flowing up
After top of tower pressure reaches 600kPa, spurts to oxygen and take off in blow bin, it is spare；
B, it washs for the first time：
The slurry that step a is obtained is spare after wash engine washing concentrating；
C, the ClO 2 bleaching under strong acid condition：
Dense standpipe in being sent into after the pulp concentration obtained after step b washings, is then added sulfuric acid, and it is 3.0 to adjust pH value,
Then slurry is heated to steam being sent into medium-consistency pulp mixer after 75~85 DEG C, 10kg/ is then added into medium-consistency pulp mixer
Admt, a concentration of 10.0g/l ClO 2 solution and be uniformly mixed, then slurry enters in upflow tower, from up-flow tower top
Portion's overflow to downflow tower, slurry is 150min in the residence time of upflow tower and downflow tower；
D, it washs for second：
Slurry is drawn to wash engine from downflow tower and is washed, concentrates, spare；
E, bleach boosters are added：
The model AP8138 that the slurry obtained after step d washings is produced in the addition Bark Mann of wash engine stern notch
Bleach boosters stoste, control bleach boosters additive amount be 0.3kg/admt, temperature be 80 DEG C, pH value 12.0；
F, hydrogen peroxide and oxygen boosting alkali density：
Caustic soda, hydrogen peroxide and oxygen is added in wash engine stern notch in the slurry obtained after step d washings, adjusts pH value 11.5
Medium-consistency pulp mixer is sent into after~12 to be uniformly mixed, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower,
Slurry is 70min in the residence time of upflow tower and downflow tower, and temperature is 85 DEG C；
G, third time is washed：
Slurry after step e, f is sent to wash engine washing concentrating, spare；
H, sulfuric acid is added in wash engine stern notch in the slurry obtained after step g washings, it is dense mixed in being sent into after adjusting pH value 4.5
Clutch, into medium-consistency pulp mixer be added 1kg/admt, a concentration of 10.0g/l ClO 2 solution and be uniformly mixed, then starch
Material enters in upflow tower, and from upflow tower top overflow to downflow tower, slurry is in the residence time of upflow tower and downflow tower
300min, temperature are 85 DEG C；
When slurry is extracted out from bleaching action tower bottom, 2kg/admt, a concentration of 120g/l hypo solutions is added, in
The complete residual chlorine with unreacted in slurry；
I, the 4th washing：
Slurry after step h is sent to wash engine washing concentrating, spare；
J, enzymatic treatment is brightened：
The model that the slurry obtained after step i washings is produced in the addition Bark Mann of wash engine stern notch
BUZYME3500's brightens proenzyme liquid, and it is 0.16kg/admt, dense tower during then slurry is delivered to, control that enzyme additive amount is brightened in control
Temperature processed is 62 DEG C, pH value 5.55, and the slurry after brightening enzymatic treatment is delivered to the storage of finished pulp tower, spare
Finally it should be noted that above example is only used to illustrate the technical scheme of the present invention rather than is protected to the present invention
The limitation of range, although being explained in detail to the present invention with reference to preferred embodiment, those skilled in the art should manage
Solution, technical scheme of the present invention can be modified or replaced equivalently, without departing from technical solution of the present invention essence and
Range.
Claims (7)
1. a kind of bleaching process of high whiteness bamboo pulp, it is characterised in that：Including following processing step：
A, two sections of delignification bleachings：
A1) one section of delignification bleaching：
The caustic soda and 1~3kg/admt for accounting for air dried pulp weight 2.0%~3.0% are added into the slurry after wash engine washing concentrating
Magnesium sulfate, after low-pressure steam is heated to 90~95 DEG C be sent into first segment medium-consistency pulp mixer, in the first paragraph in dense mixer
20~25kg/admt oxygen mix is added and uniformly enters lifting/lowering streaming reaction tube afterwards, slurry is in lifting/lowering streaming reaction tube
Residence time is 5~10min；
A2) two sections of delignification bleachings：
The slurry come out from first segment downflow tower is sent into second segment medium-consistency pulp mixer after middle pressure steam is heated to 95~102 DEG C,
It is uniform that 20~25kg/admt oxygen mix is added in second segment medium-consistency pulp mixer, send to upflow tower and stops 60~80min, slurry
Material is spurted to oxygen and is taken off in blow bin after upflow tower top pressure reaches 300~600kPa, spare；
B, it washs for the first time：
The slurry that step a is obtained is spare after wash engine washing concentrating；
C, the ClO 2 bleaching under strong acid condition：
Then sulfuric acid is added in dense standpipe during the slurry that step b is obtained is sent into, it is 2.0~3.0 to adjust pH value, then uses steam
Slurry is heated to be sent into medium-consistency pulp mixer after 75~85 DEG C, 6~10kg/admt, concentration are then added into medium-consistency pulp mixer
For 9.0~10.0g/l ClO 2 solution and be uniformly mixed, then slurry enters in upflow tower, overflows at the top of the upflow tower
It is flow to downflow tower, slurry is 120~150min in the residence time of upflow tower and downflow tower；
D, it washs for second：
Slurry is drawn to wash engine from downflow tower and is washed, concentrates, spare；
E, bleach boosters are added：
The drift for the model AP8138 that the slurry obtained after step d washings is produced in the addition Bark Mann of wash engine stern notch
White accelerating agent stoste, control bleach boosters additive amount are 0.2~0.3kg/admt, and temperature is 75~80 DEG C, pH value 11.5
~12.0；
F, hydrogen peroxide and oxygen boosting alkali density：
Caustic soda, hydrogen peroxide and oxygen is added in wash engine stern notch in the slurry obtained after step d washings, adjusts pH value 11.5~12
It is sent into medium-consistency pulp mixer afterwards to be uniformly mixed, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower, slurry
It is 60~70min in the residence time of upflow tower and downflow tower, temperature is 80~85 DEG C；
G, third time is washed：
Slurry after step e, f is sent to wash engine washing concentrating, spare；
H, ClO 2 bleaching：
Sulfuric acid is added in wash engine stern notch in the slurry obtained after step g washings, it is dense mixed in being sent into after adjusting pH value 3.5~4.5
It is equal that 1~3kg/admt, the ClO 2 solution of a concentration of 9.0~10.0g/l and mixing are added into medium-consistency pulp mixer for clutch
Even, then slurry enters in upflow tower, from upflow tower top overflow to downflow tower, stop of the slurry in upflow tower and downflow tower
Time is 250~300min, and temperature is 80~85 DEG C；
When slurry is extracted out from bleaching action tower bottom, 0.5~2kg/admt, a concentration of 100~120g/l sodium thiosulfate is added
Solution neutralizes the residual chlorine that unreacted is complete in slurry；
I, the 4th washing：
Slurry after step h is sent to wash engine washing concentrating, spare；
J, enzymatic treatment is brightened：
The model BUZYME3500 that the slurry obtained after step i washings is produced in the addition Bark Mann of wash engine stern notch
Brighten proenzyme liquid, it is 0.16~0.25kg/admt, dense tower during then slurry is delivered to, control temperature that enzyme additive amount is brightened in control
Degree is 47~65 DEG C, and pH value is 4.5~7.0, and the slurry after brightening enzymatic treatment is delivered to the storage of finished pulp tower, spare.
2. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step j, brighten
The additive amount of enzyme is 0.25kg/admt, dense tower during then slurry is delivered to, controlled at 50 DEG C, pH value 6.0.
3. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step j, brighten
The additive amount of enzyme is 0.20kg/admt, dense tower during then slurry is delivered to, controlled at 58 DEG C, pH value 5.0.
4. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step j, brighten
The additive amount of enzyme is 0.16kg/admt, dense tower during then slurry is delivered to, controlled at 62 DEG C, pH value 5.5.
5. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step e, bleaching
Accelerating agent additive amount is 0.25kg/admt, and temperature is 78 DEG C, pH value 11.8.
6. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step e, bleaching
Accelerating agent additive amount is 0.2kg/admt, and temperature is 75 DEG C, pH value 11.5.
7. a kind of bleaching process of high whiteness bamboo pulp according to claim 1, it is characterised in that：In the step e, bleaching
Accelerating agent additive amount is 0.3kg/admt, and temperature is 80 DEG C, pH value 12.0.
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| CN102154884A (en) * | 2011-03-31 | 2011-08-17 | 重庆理文造纸有限公司 | Improved bleaching process for bamboo wood dissolving pulp |
| CN104963230A (en) * | 2015-07-15 | 2015-10-07 | 重庆理文造纸有限公司 | Bleaching process for improving whiteness of paper pulp |
| CN104963229A (en) * | 2015-07-15 | 2015-10-07 | 重庆理文造纸有限公司 | Bleaching process of bamboo dissoluble pulp |
| CN204919193U (en) * | 2015-07-15 | 2015-12-30 | 重庆理文造纸有限公司 | Bleaching system who improves and stabilize pulp board whiteness |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102154884A (en) * | 2011-03-31 | 2011-08-17 | 重庆理文造纸有限公司 | Improved bleaching process for bamboo wood dissolving pulp |
| CN104963230A (en) * | 2015-07-15 | 2015-10-07 | 重庆理文造纸有限公司 | Bleaching process for improving whiteness of paper pulp |
| CN104963229A (en) * | 2015-07-15 | 2015-10-07 | 重庆理文造纸有限公司 | Bleaching process of bamboo dissoluble pulp |
| CN204919193U (en) * | 2015-07-15 | 2015-12-30 | 重庆理文造纸有限公司 | Bleaching system who improves and stabilize pulp board whiteness |
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