CN101899795A - Method for improving utilization ratio of chemi-mechanical pulp bleaching filtrate - Google Patents

Method for improving utilization ratio of chemi-mechanical pulp bleaching filtrate Download PDF

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CN101899795A
CN101899795A CN2010102542463A CN201010254246A CN101899795A CN 101899795 A CN101899795 A CN 101899795A CN 2010102542463 A CN2010102542463 A CN 2010102542463A CN 201010254246 A CN201010254246 A CN 201010254246A CN 101899795 A CN101899795 A CN 101899795A
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bleaching
slurry
filtrate
consumption
leaching
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沈葵忠
房桂干
施英乔
丁来保
盘爱享
韩善明
梁芳敏
金莉
李萍
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Institute of Chemical Industry of Forest Products of CAF
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Institute of Chemical Industry of Forest Products of CAF
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Abstract

The invention relates to a method for improving the utilization ratio of a chemi-mechanical pulp bleaching filtrate. The method comprises the following steps of: preparing a chemi-mechanical pulp by processes of log barking, chemically dipping and pulping, screening and concentrating, bleaching, washing and concentrating, and pulp storing; directly recycling a leaching filtrate extracted from a pulp, which is discharged from the bleaching process and is concentrated from 10 to 30 weight percent to 20 to 45 weight percent, to the leaching process; uniformly mixing the leaching filtrate, leaching chemical medicaments and the pulp in a brown pulp mixer to obtain a mixture; and bleaching the mixture in a leaching reactor. After the leaching, a leaching filtrate extraction device is arranged and recycles the leaching filtrate in place of clear water or white water to save the leaching chemical medicaments and reduce the clear water consumption of factories. The method for improving the utilization ratio of the chemi-mechanical pulp bleaching filtrate has the advantages of reducing 0.64 to 2 tons of water used for making each ton of pulp, saving the consumption of the chemical medicaments, and improving leaching effect and slurry cleanliness; and compared with a conventional process, the pulp leaching whiteness can be improved by 2 to 6.5 percent under the condition of the same leaching chemical consumption.

Description

A kind of method that improves the chemi-mechanical pulp bleaching filtrate utilization rate
Technical field
The present invention relates to the short flow process reuse method of a kind of chemi-mechanical pulp bleaching filtrate, belonging to machine slurry production field.
Background technology
China's papermaking enterprise ton slurry paper integrated water consumption is high.According to China's paper industry cleaner production standard-required, the comprehensive water withdrawal of ton slurry paper requires to be lower than 50 tons.At present China is except that minority enterprise or part producing line are reached advanced world standards, and most of enterprise comprehensive water withdrawal of average ton slurry paper still is in a high position of 103 tons; In implementing the Strategy of Clean Production process, reducing water resources consumption is the urgent task of China's paper industry.
The key position that paper mill reduces water consumption is a bleachery.Modern paper factory, general implementation the reuse of process water adverse current, water-use efficiency promotes significantly.The existing BCTMP plant water circulatory system as shown in Figure 1.The bleaching disposed slurry uses paper machine white water or clear water to wash, float the back washings and import white water loop tank or jar, be used as slurry screening, dilution, slurry after being pumped to defibrination again, unnecessary process water can be pumped to the slurrying circulating water chennel or jar is used for wood chip washing, chemical impregnation washing or the peeling of log wet method.Save the bleaching process water and help reducing full factory clear water consumption and watering balance.
Change machine slurry hydrogen peroxide bleaching uses H 2O 2, NaOH, Na 2SiO 3, bleaching such as DTPA medicament, need remaining certain amount of H in its bleach residue 2O 2, to reach the expection bleaching effect, bleach residue also has other residue chemistry medicine NaOH, Na simultaneously 2SiO 3, DTPA.If these residue chemistry medicines obtain recycling, can save the bleaching medicament.
Former bleacher water circulation reclaiming system flow process is longer, bleaching filtrate be back to use BCTMP factory defibrination after slurry washing water mixes after natural color pulp screen washing procedure, exist reuse point near shortcomings such as the flow process of flow process upstream, reuse bleaching filtrate are long, and bleach residue has passed through the dilution of washings, the shortcoming that the service efficiency of the bleaching residue chemistry medicine in the filtrate is not fully utilized.
Summary of the invention
Bleach the inefficient problem of remaining soup reuse in order to solve the existing whitening machine slurry factory of floating, a kind of method that improves the chemi-mechanical pulp bleaching filtrate utilization rate is provided, by extracting bleaching filtrate and reuse, give full play to the usefulness of residue chemistry medicine in the bleaching process filtrate, reduce bleachery waste water use amount, the service efficiency of remaining soup is bleached in performance simultaneously, has improved the wash degree of slurry, realizes the target of factory's water saving.
Technical scheme of the present invention is: a kind of method that improves the chemi-mechanical pulp bleaching filtrate utilization rate, according to log debarking, chemical impregnation and defibrination, screening concentrate, preparing machine slurry after the bleaching, washing concentrating, storage slurry process, the concentration that bleachery is come out is that the slurry of 10～30%wt is concentrated into bleaching filtrate direct reuse that slurry concentration 20～45%wt extracts to bleachery, enters in the Bleaching reactor after mixing with bleached chemical medicine, slurry in the slurry blender before floating again and bleaches.
Hydrogen peroxide bleaching, H are used in described bleaching 2O 2Consumption is 0.5 ~ 10% of an over dry slurry mass fraction, DTPA consumption 0.05 ~ 0.2%, Na 2SiO 3Consumption is 1 ~ 3%, NaOH consumption and H 2O 2Mass ratio be 0.25 ~ 1.25,60 ~ 95 ℃ of treatment temperatures, 60 ~ 180 minutes time.
Add MgSO in the bleaching soup 4, MgCO 3, Mg (CH 3COO) 2, Mg (OH) 2, Mg (NO 3) 2In any one; Addition is 0 ~ 0.05%wt of over dry stock quality.
Compare with original BCTMPization machine slurry plant water reuse method, the short flow process reuse method of bleaching filtrate of the present invention has following beneficial effect:
1. reduced bleachery clear water use amount by a relatively large margin, the ton slurry reduces 0.6 ~ 3 ton of clear water use amount;
2. improved the washing cleanliness factor of bleaching slurry.Improve detersive efficiency 40%～47%; The slurry bleaching yield improves 1 ~ 2%;
3. saved the use amount of bleachery chemicals.Reach identical slurry bleaching whiteness, DTPA, Na 2SiO 3, MgSO 4Deng bleaching auxiliary chemicals consumption is 50% of former process;
4. when using identical bleaching dosing, can improve slurry terminal point bleaching whiteness.Compare the short flow process reuse of bleach residue, identical H with original technology 2O 2The bleaching agent consumption, the slurry bleaching whiteness can improve 2 ~ 6.5%ISO.
Description of drawings
Fig. 1ization machine slurry factory production system water circulation flow chart;
Fig. 2 production system water circulation of the present invention flow chart;
The short flow process reuse of Fig. 3 CTMP slurry bleaching filtrate flow chart;
The short flow process reuse of Fig. 4 BCTMP factory bleaching filtrate flow chart.
The specific embodiment
Below in conjunction with accompanying drawing the present invention is elaborated:
The present invention is by setting up filtrate recycle tank or jar under bleach residue extraction equipment and the machine behind the bleaching tower, extract bleaching filtrate direct reuse before bleaching tower, the long flow process reuse route of bleaching filtrate is changed into short flow process reuse route, as bleaching action material liquid phase part, shorten bleaching filtrate recycle path greatly, can give full play to the effect of bleaching residue chemistry product, the water consumption of saving bleaching system has simultaneously improved the utilization rate of chemi-mechanical pulp bleaching filtrate.
In bleaching system, enter the preceding slurry concentration of bleaching tower and be generally 30-45%wt, after mixing with bleaching soup and plain boiled water, the bleaching slurry concentration is controlled to be 20～30%wt in the bleaching tower.In the present invention, a kind of method that improves the chemi-mechanical pulp bleaching filtrate utilization rate, according to log debarking, chemical impregnation and defibrination, screening concentrate, preparing machine slurry after the bleaching, washing concentrating, storage slurry process, it is preceding to Bleaching reactor (or bleaching tower) that the concentration that bleachery is come out is that the slurry of 10～30%wt is concentrated into the bleaching filtrate direct reuse that concentration 20～45%wt produces, and enters after mixing with bleached chemical medicine, slurry in the slurry blender before floating again and carry out bleaching action in the bleaching tower.Hydrogen peroxide bleaching, H are used in described bleaching 2O 2Consumption is 2 ~ 10% of an over dry slurry mass fraction, DTPA consumption 0.05 ~ 0.2%, Na 2SiO 3Consumption is 1 ~ 3%, NaOH consumption and H 2O 2Ratio be 0.25 ~ 1.25,60 ~ 95 ℃ of treatment temperatures, 60 ~ 180 minutes time.Can add magnesium salts in the bleaching soup, also can not add, can add MgSO if add 4, MgCO 3, Mg (CH 3COO) 2, Mg (OH) 2, Mg (NO 3) 2In any one; Addition is 0 ~ 0.05%wt of over dry stock quality.During concrete enforcement, as long as behind bleaching tower, set up the slurry concentrator that from slurry, extracts bleaching filtrate, for example screw machine pulp grinder or two net concentrator and attached bleaching filtrate recycle tank or jar, the equipment of setting up indicates with the thick line among Fig. 2, the production system miscellaneous equipment is not done any change, can effectively improve the utilization rate of chemi-mechanical pulp bleaching filtrate.
Following mask body 2 is further detailed in conjunction with the accompanying drawings:
(1) is used for the reuse that filtrate is bleached by CTMPization machine slurry factory.Before floating disposed slurry washing and concentrator, set up the slurry concentrator behind the bleaching tower, extract concentrator as Var-nip press or other slurries, be used to extract bleach residue, bleach residue reuse tank is set under the extraction equipment.Bleaching filtrate is without the dilution of slurry washing water, direct reuse is preceding to Bleaching reactor (or bleaching tower), substitute clear water or paper machine white water, it is dense to normal concentration to enter bleaching tower adjusting slurry after mixing in the high dense blender of slurry with slurry and fresh bleaching soup;
(2) slurry concentrator import slurry concentration is 10-30%wt, and the outlet slurry concentration is 20-45%wt, and the ton slurry extract scale of construction is 0.83 ~ 4.17 ton;
(3) the bleaching filtrate that Ti Qus substitutes to enter after clear water or plain boiled water mix with bleached chemical medicine, slurry in the slurry blender before floating and carries out hydrogen peroxide bleaching in the bleaching tower; The alternative amount of ton slurry clear water or plain boiled water is the 0.6-3 ton;
(4) use H 2O 2Slurry is bleached H 2O 2Consumption is 2 ~ 10% of an over dry slurry mass fraction, DTPA consumption 0.05 ~ 0.2%, Na 2SiO 3Consumption is 1 ~ 3%, and Mg salt consumption is 0 ~ 0.05%, NaOH consumption and H 2O 2Ratio be 0.25 ~ 1.25, treatment temperature 60 ~ 95 OC, 60 ~ 180 minutes time;
(5) remaining H in the bleaching filtrate that Ti Qus 2O 2Amount is H 2O 210～30% of addition contains a certain amount of DTPA, Na simultaneously 2SiO 3And MgSO 4Deng bleaching stibilizer, require or production status according to slurry products target whiteness, can replenish a certain proportion of bleaching stibilizer during slurry bleaching, to realize bleaching effect; The additional amount of bleaching stibilizer is to account for 0 ~ 50% of former bleaching stibilizer addition.Bleach main chemicals usage such as H during slurry bleaching 2O 2, NaOH remains unchanged or reduce 10 ~ 30%, the auxiliary bleaching chemicals is bleaching stibilizer such as DTPA, Na 2SiO 3, MgSO 4Deng, reducing 50%, the slurry bleaching quality remains unchanged substantially or improves.
Magnesium salts can be added in the bleaching soup and also magnesium salts can be do not added; The magnesium salts that adds can be MgSO 4, MgCO 3, Mg (CH 3COO) 2, Mg (OH) 2And Mg(NO 3) 2Addition is 0 ~ 0.05%.
Embodiment 1
CTMP pulp preparation Eucalyptus (the leaflet eucalyptus has another name called gallery edge eucalyptus, Eucalyptus exserta) wood chip takes from Guangxi, cutting into slices in the original producton location is transported to the laboratory, places freezer 0～4 oC preserves standby down.Wood chip at room temperature was soaked in water about 12 hours, sent into decatize storehouse normal pressure presteaming 10 ~ 15 minutes, used extruder (Andritz company) to push, and the extruding compression ratio is 1:4.Extruding back material uses alkaline sodium sulfite to carry out the chemical impregnation preliminary treatment, and chemical presoaking stain condition is: NaOH consumption 1%, Na 2SO 3Consumption 2%, DTPA consumption 0.2%, pre-preg time 15min, temperature 50 oC, dipping material concentration 22%wt.Use homemade fiberizer (machinery subsidiary factory of Jilin Paper Mill, unit type GNM300) defibrination under normal pressure, control different defibrination energy inputs, regulate paper pulp freedom to 450 ~ 500 ml CSF.The mill disposed slurry disappears and dives and screening, and latent condition disappears: 2% slurry concentration, 90 oC disappears and dived 15 minutes.Slurry characteristic parameter: freedom 465 ml CSF, bulk 3.40 cm 3/ g, whiteness 51.9 %ISO, burst index 0..26kPam 2∕ g, tear index 0.94mNm 2/ g, tensile index 8.9mN.m 2∕ g.
Bleach residue reuse simulation factory conditions of bleaching, carry out the short flow process reuse bleaching of bleach residue, in the two net concentrator principles of laboratory simulation, use filter screen to extract bleaching filtrate from floating disposed slurry by squeezing, input concentration is 20%, extracting filtrate disposed slurry mass dryness fraction is 30% ~ 45%, bleaches filtrate recycle experiment (see figure 3) then.Initial journey starts bleaching, uses clear water and slurry, bleaching soup to mix and be placed on constant temperature water bath, uses following conditions of bleaching---H 2O 2Consumption 2%, NaOH consumption are 3%, 80 ℃ of temperature, time 120min, Na 2SiO 3Consumption 2%, DTPA0.1%, bleaching slurry concentration 20%; The slurry bleaching whiteness is 81.9%ISO, and the slurry bleaching yield is 96.3%.During the residual liquid recycling bleaching, use clear water during except preparation bleaching soup, other waters all substitute with bleach residue, and slurry per ton reduces clear water (or paper machine white water) 3 tons, other conditions of bleaching---H during the residual liquid recycling bleaching 2O 2Consumption 2%, NaOH consumption are 3%, temperature 80 OC, time 120min, Na 2SiO 3Consumption 1%, DTPA consumption 0.05%, MgSO 4Consumption is 0.025%, bleaching slurry concentration 20%, wherein, bleaching H 2O 2Stabilizing agent dosage (Na 2SiO 3, DTPA, MgSO 4Deng) be 50% of normal use amount.Be the continuous production status of simulation factory, carry out 1-7 residual liquid recycling bleaching, make bleaching water systematic parameter index reach poised state, to press close to the plant produced actual state.Result of the test is, the bleaching pulp brightness is 81.7 ~ 82.2%ISO, and the slurry bleaching yield is 98..0 ~ 98.5%, reduces bleaching assistant (Na 2SiO 3, DTPA, MgSO 4) consumption 0～50%, the bleaching pulp yield improves 1 ~ 2%, and whiteness increases by 2% ~ 3%ISO, and ton slurry reuse bleaching filtrate is 2 tons during bleaching.
Specific implementation method is as follows:
1. use laboratory slurry concentrator, Eucalyptus CTMP slurry mass dryness fraction is concentrated to 35% ~ 45%, use for bleaching;
2.NaOH, Na 2SiO 3, DTPA uses clear water to be mixed with liquid to use H 2O 2(27% mass fraction concentration) is directly used;
3. use bleaching filtrate to substitute clear water (or paper machine white water) and mix with slurry, bleached chemical medicine, ton slurry bleaching filter use amount is 3 tons, bleaches then;
4. controlling following bleaching drug dosage and temperature, time and slurry concentration bleaches: H 2O 2Consumption 2%, NaOH consumption are 3%, temperature 80 OC, time 120min, Na 2SiO 3Consumption 1%, DTPA consumption 0.05%, bleaching slurry concentration 20%, wherein, bleaching H 2O 2Stabilizing agent dosage (Na 2SiO 3, DTPA) be 50% of normal use amount;
5. bleaching finish to use slurry concentrator (the laboratory filtrate extraction elements of the two net concentrators of simulation factory) to extract bleaching filtrate, the bleaching filtrate recycle of extraction to bleaching before with do not bleach slurry and chemicals mixes, carry out continuous bleaching;
6. the simulation working condition bleaching results of carrying out the continuous reuse of filtrate 1-7 time: the bleaching whiteness of slurry is 81.7 ~ 82.2%ISO, slurry bleaching yield 98..0 ~ 98.5%.
Embodiment 2
The preparation poplar CTMP slurry of CTMP slurry is taken from Shandong commercial running machine slurry production line, slurry characteristic parameter: freedom 470 ml CSF, bulk 2.53 cm 3/ g, whiteness 51.9 %ISO, burst index 0..67kPam 2∕ g, tear index 1.60mNm 2/ g, tensile index 14.9mN.m 2∕ g.
Use the pilot scale slurry to extract the concentrated factory's bleaching tower outlet bleaching slurry of taking from of equipment (Var-nip press, feature: import slurry concentration 10 ~ 30%, discharging slurry concentration 20% ~ 45%), extract bleaching filtrate.Bleaching filtrate feature: H 2O 23.64g/L, contain Na in the bleaching soup 2SiO 3, DTPA and MgSO 4Deng H 2O 2Stabilizing agent.Bleaching back ton slurry filtrate generating capacity is 3.5 tons of/ton slurries, and bleaching filtrate extracted amount is 2 tons of/ton slurries, uses for slurry bleaching.Factory's short flow process reuse flow process of bleaching filtrate is seen Fig. 4.
The bleaching filtrate recycle is simulated factory's conditions of bleaching in the laboratory, use clear water during preparation bleaching soup, and other waters all substitute with bleach residue, and slurry per ton uses 2 tons of remaining soups of bleaching (wherein to contain 7.26 kg H approximately 2O 2), to bleach behind fresh bleaching liquor, the remaining soup of bleaching and the slurry mixing mixing, following conditions of bleaching---H is used in bleaching 2O 2Consumption 6%, NaOH consumption are 4%, Na 2SiO 3Consumption 1.5%, DTPA consumption 0.05%, MgSO 4Consumption 0.05%, bleaching slurry concentration 25%, temperature 60 OC, time 180min, wherein, bleaching stibilizer (Na during bleaching 2SiO 3, DTPA and MgSO 4) consumption is 50% of conventional bleaching consumption.The bleaching pulp brightness is 79.5%ISO.
Implementation result bleaching pulp brightness improves 3.5 ~ 6.5%ISO(and floats back recycle-water flow process relatively with former, and contrasting bleaching experiment simultaneously, to float the disposed slurry whiteness be 73 ~ 76.5%ISO); The bleaching back increases a slurry concentration extraction equipment and a filtrate collecting tank, and the slurry wash degree improves, newly-increased detersive efficiency 40～45%.
Specific implementation method is as follows:
1. use laboratory slurry concentrator (two roller pulp thickener), poplar CTMP slurry mass dryness fraction is concentrated to 35% ~ 45%, use for bleaching;
2.NaOH, Na 2SiO 3, DTPA, MgSO 4Use clear water to be mixed with liquid and use H 2O 2(27% mass fraction) directly uses;
3. use bleaching filtrate to substitute clear water (or paper machine white water) and mix with the slurry bleaching chemicals, the residual filter use amount of ton slurry bleaching is 2 tons, bleaches then;
4. controlling following bleaching drug dosage and temperature, time and slurry concentration bleaches: H 2O 2Consumption 6%, NaOH consumption are 4%, temperature 60 oC, time 180min, Na 2SiO 3Consumption 1.5%, DTPA consumption 0.05%, MgSO 4Consumption 0.05%., bleaching slurry concentration 25%, wherein, bleaching H 2O 2Stabilizing agent dosage (Na 2SiO 3, DTPA and MgSO 4) be 50% of normal use amount;
5. bleaching finishes to set up slurry concentrator (import slurry concentration 10% ~ 30%, export slurry concentration 20% ~ 45%) and the filtrate collection tank extracts, collection bleaching filtrate, the bleaching filtrate recycle that extracts and is not bleached slurry and chemicals and is mixed then and bleach before the slurry bleaching.
Embodiment 3
The preparation slurry characteristic parameter of poplar CTMP slurry: freedom 470 ml CSF, bulk 2.53 cm 3/ g, whiteness 51.9 %ISO, burst index 0..67kPam 2∕ g, tear index 1.60mNm 2/ g, tensile index 14.9mN.m 2∕ g.
Bleaching filtrate is set behind bleaching tower extracts equipment (Var-nip press or two net pulp thickener, feature: import slurry concentration 20 ~ 35%, discharging slurry concentration 30% ~ 45%) and bleaching filtrate collecting tank, extract and collect bleaching filtrate.Bleaching filtrate feature: H 2O 23.64g/L, contain Na in the bleaching filtrate 2SiO 3, DTPA and MgSO 4Deng H 2O 2Stabilizing agent.Bleaching back ton slurry filter amount generating capacity is 1.87 ~ 4 tons of/ton slurries, and the bleach residue extracted amount is 0.6 ~ 1.7 ton of/ton slurry, uses for slurry bleaching.Factory's short flow process reuse flow process of bleaching filtrate is seen Fig. 4.
When filtrate recycle is bleached by factory, use clear water during preparation bleaching soup, other waters all substitute with bleach residue, and 0.6 ~ 1.7 ton of bleaching of slurry use per ton filtrate (contains 3.13 kg H approximately in 1 ton of filtrate 2O 2), bleaching filtrate and fresh bleaching liquor, float with slurry mixings mixing after bleach, bleach use following conditions of bleaching---H 2O 2Consumption 10%, NaOH consumption are 6%, Na 2SiO 3Consumption 1.5%, DTPA consumption 0.05%, MgSO 4Consumption 0.05%, bleaching slurry concentration 25%, temperature 95 OC, time 60min, wherein, bleaching stibilizer (Na during bleaching 2SiO 3, DTPA and MgSO 4) consumption is 50% of conventional bleaching consumption.The bleaching pulp brightness is 83%ISO.
Implementation result bleaching pulp brightness improves 2%ISO; The bleaching back increases a slurry concentration extraction equipment and a filtrate collecting tank, newly-increased detersive efficiency 41%～47%.
Specific implementation method is as follows:
1. make concentrator (two roller pulp thickeners or two net pulp thickener), poplar CTMP slurry mass dryness fraction is concentrated to 35% ~ 45%, use for bleaching;
2.NaOH, Na 2SiO 3, DTPA, MgSO 4Use clear water to be mixed with liquid and use H 2O 2(27% mass fraction) directly uses;
3. use bleaching filtrate to substitute clear water (or paper machine white water) and mix with the slurry bleaching chemicals, ton slurry bleaching filtrate use amount is 1.7 tons, bleaches then;
4. controlling following bleaching drug dosage and temperature, time and slurry concentration bleaches: H 2O 2Consumption 10%, NaOH consumption are 6%, temperature 95 oC, time 60min, Na 2SiO 3Consumption 1.5%, DTPA consumption 0.05%, MgSO 4Consumption 0.05%., bleaching slurry concentration 25%, wherein, bleaching H 2O 2Stabilizing agent dosage (Na 2SiO 3, DTPA and MgSO 4) be 50% of normal use amount;
5. bleaching finishes to set up slurry concentrator (import slurry concentration 20% ~ 30%, export slurry concentration 30% ~ 45%) and the filtrate collection tank extracts, collection bleaching filtrate, the bleaching filtrate recycle that extracts and is not bleached slurry and chemicals and is mixed then and bleach before the slurry bleaching.
Comparative Examples 1
Certain papermaking enterprise uses poplar outsourcing wood chip to carry out BCTMP production, and the pulping bleaching water circulation adopts traditional approach, and the water circulation system flow chart is seen Fig. 1.Its slurry characteristic parameter is: freedom 470 ml CSF, bulk 2.53 cm 3/ g, whiteness 51.9 %ISO, burst index 0..67kPam 2∕ g, tear index 1.60mNm 2/ g, tensile index 14.9mN.m 2∕ g.
Slurry uses enterprise's circulation to come mixing water (containing bleaching washings, the preceding slurry condensed water of bleaching) to wash, screen, concentrate, and bleaches then with behind the fresh bleaching liquor mixing, and following conditions of bleaching---H is used in bleaching 2O 2Consumption 10%, NaOH consumption are 6%, Na 2SiO 3Consumption 3%, DTPA consumption 0.2%, MgSO 4Consumption 0.1%, bleaching slurry concentration 25%, temperature 85 OC, time 120min.The bleached pulp whiteness is 81%ISO.
In contrast, using Fig. 4 to bleach the short flow process reuse mode of filtrate bleaches same slurry.Bleaching filtrate extracting mode and bleaching filtrate feature are seen embodiment 3.Bleaching filtrate substitutes clear water or the paper machine white water use amount is 1.5 tons of/ton slurries (bleaching disposed slurry concentration is concentrated into slurry 40%wt by 25%wt).The conditions of bleaching of two kinds of bleaching filtrate cycle modes, bleaching stock quality and implementation result contrast are listed as follows:
Figure 455258DEST_PATH_IMAGE001

Claims (3)

1. method that improves the chemi-mechanical pulp bleaching filtrate utilization rate, according to log debarking, chemical impregnation and defibrination, screening concentrate, preparing machine slurry after the bleaching, washing concentrating, storage slurry process, it is characterized in that, with the bleachery concentration of coming out is that the slurry of 10～30%wt is concentrated into bleaching filtrate direct reuse that the slurry of concentration 20～45%wt extracts to bleachery, enters in the Bleaching reactor after mixing with bleached chemical medicine, slurry in the slurry blender before floating again and bleaches.
2. the method for raising chemi-mechanical pulp bleaching filtrate utilization rate as claimed in claim 1 is characterized in that, hydrogen peroxide bleaching, H are used in described bleaching 2O 2Consumption is 2 ~ 10% of an over dry slurry mass fraction, DTPA consumption 0.05 ~ 0.2%wt, Na 2SiO 3Consumption is 1 ~ 3%wt, NaOH consumption and H 2O 2Mass ratio be 0.25 ~ 1.25,60 ~ 95 ℃ of treatment temperatures, 60 ~ 180 minutes time.
3. the method for raising chemi-mechanical pulp bleaching filtrate utilization rate as claimed in claim 1 is characterized in that, adds MgSO in the bleaching soup 4, MgCO 3, Mg (CH 3COO) 2, Mg (OH) 2, Mg(NO 3) 2In any one; Addition is 0 ~ 0.05%wt of over dry stock quality.
CN2010102542463A 2010-08-16 2010-08-16 Method for improving utilization ratio of chemi-mechanical pulp bleaching filtrate Pending CN101899795A (en)

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CN104928963A (en) * 2015-05-08 2015-09-23 白博 Zero-discharge online high concentration extraction process for chemimechamical pulp pulping waste liquid
CN106120432A (en) * 2016-06-29 2016-11-16 江汉大学 Utilize the method that corn leafage one kettle way manufactures paper pulp
CN109098026A (en) * 2018-08-14 2018-12-28 中国林业科学研究院林产化学工业研究所 A kind of method of reinforcing fiber raw material bleaching medicinal liquid osmosis

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Cited By (6)

* Cited by examiner, † Cited by third party
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CN103031760A (en) * 2011-10-04 2013-04-10 安德里特斯公开股份有限公司 Method and device for dissolving fiber material by heating pump system with high efficiency and saved energy
CN104928963A (en) * 2015-05-08 2015-09-23 白博 Zero-discharge online high concentration extraction process for chemimechamical pulp pulping waste liquid
CN106120432A (en) * 2016-06-29 2016-11-16 江汉大学 Utilize the method that corn leafage one kettle way manufactures paper pulp
CN106120432B (en) * 2016-06-29 2018-08-17 江汉大学 The method for manufacturing paper pulp using corn leafage one kettle way
CN109098026A (en) * 2018-08-14 2018-12-28 中国林业科学研究院林产化学工业研究所 A kind of method of reinforcing fiber raw material bleaching medicinal liquid osmosis
CN109098026B (en) * 2018-08-14 2021-01-26 中国林业科学研究院林产化学工业研究所 Method for enhancing penetration of fiber raw material bleaching liquor

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