CN101418531A - Method for preparing eucalyptus and poplar mixture material bleached chemical thermomechanical pulp - Google Patents
Method for preparing eucalyptus and poplar mixture material bleached chemical thermomechanical pulp Download PDFInfo
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- CN101418531A CN101418531A CNA2008102382429A CN200810238242A CN101418531A CN 101418531 A CN101418531 A CN 101418531A CN A2008102382429 A CNA2008102382429 A CN A2008102382429A CN 200810238242 A CN200810238242 A CN 200810238242A CN 101418531 A CN101418531 A CN 101418531A
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Abstract
The invention belongs to the technical field of preparing bleached chemical thermomechanical pulp and in particular relates to a process method for preparing the bleached chemical thermomechanical pulp from eucalyptus and poplar. The process method adopts the eucalyptus and the poplar as raw materials to prepare the bleached chemical thermomechanical pulp; through the addition of a pulp grinding accelerant, the process reduces energy consumption of pulp grinding by 10 to 15 percent compared with the prior process for the bleached chemical thermomechanical pulp, reduces production cost, saves energy and simultaneously reduces the content of pulping fasciculus.
Description
Technical field
The invention belongs to preparation bleached chemical thermomechanical pulp technical field, particularly a kind of process for preparing the bleached chemical thermomechanical pulp by Eucalyptus, poplar.
Background technology
Along with domestic paper and cardboard production capacity increase, the paper making raw material shortage problem becomes increasingly conspicuous, and wood pulp fibre has to depend on a large amount of imports, and cost of material is limited by international vendor, has a strong impact on business economic benefit, restriction industry development.Traditional chemical slurry producd fibers yield only 50%-55%, and bleached chemical thermomechanical pulping technique, the fiber yield can reach more than 85%, improve about 70% than traditional chemical slurry wood utilization efficient, therefore, exploitation bleached chemical thermomechanical pulping technique, for alleviating present high-quality lumber fibre resource scarcity situation, expand and be fit to fine paper production wood raw material kind, improve raw material availability, adjust and optimization high-grade culture paper material structure, reducing production costs significantly has important and practical meanings, is the important topic of present pulping and paper-making industry.
In existing the production, bleached chemical thermomechanical pulp production technology, generally adopt single hop or two sections APMP and BCTMP technology, its pulping process key is extruding, tear and flood, adopt single-screw or double helix extruding and tearing machine, carry out squeezing extrusion, main by the raw material wood chip that loosens effectively, improve the soup osmotic effect, because this kind equipment is all the mechanism of macroscopic view to the processing procedure of raw material, though can obviously improve infiltration and the assimilation effect of soup in raw material inside, but still can not effectively improve plant fiber cells for the absorption of chemicals with utilize effect, therefore, be helpless to chemical reagent such as NaOH and enter fiber finer cell wall S rapidly
1, S
2Layer is finished the course of reaction to cellulose macromolecule in its cell membrane, can cause pulp fiber thick, and fibre bundle is many, and whiteness is low, and high-grade culture paper is not suitable for manufacturing paper with pulp.Based on the problems referred to above, not only to pay attention to fully extruding and tear, also need to adopt more directly chemical treatment means effectively, better improve dipping effect, particularly improve NaOH, H
2O
2The effect that fully absorbs Deng reagent and cellulose macromolecule.
At present, bleached chemical thermomechanical pulp pulping technique, the subject matter that exists in actual production is that refining energy consumption is higher, accounts for production cost about 1/3 usually, is unfavorable for that enterprise reduces cost, energy savings.
The bleached chemical thermomechanical pulp generally is raw material with the poplar, and poplar is mostly at northern area, and growth cycle is long, and the stock number deficiency can not satisfy the wilderness demand of paper industry to wood raw material.Owing to be grown in the place that rainfall is plentiful, south by wood, its growth is fast, and the cycle is short, the resource abundance, but its material color is dark, and the pulp fiber whiteness is low, is used for preparing the quality requirement that slurry is difficult to reach fine paper separately.
But because aspen fibers by using silicon is thin relatively, wall is thin, fiber softening in actual production; The Eucalyptus fiber is thick relatively, wall thickness, and fiber is hard, the defibrination process is difficult to control squeezing extrusion degree, two kinds of timber also differ greatly to the soup absorption rate simultaneously, can cause pulping fibre bundle content higher, so it is mixed with the bigger difficulty of bleached chemical thermomechanical pulp existence.
Summary of the invention
It is raw material by Eucalyptus and poplar that technical problem to be solved by this invention provides a kind of, the process of preparation bleached chemical thermomechanical pulp, this technology is by adding defibrination promoter, compare with bleached chemical thermomechanical sizing process, effectively reduce refining energy consumption 10%-15%, and reduced production cost, energy savings has also reduced pulping fibre bundle content simultaneously.
In order to reach above purpose, the technical solution adopted in the present invention is:
A kind of process for preparing the bleached chemical thermomechanical pulp by Eucalyptus, poplar mixed material, concrete steps comprise: pretreatment of raw material, pre-steam, squeezing extrusion, soup dipping, a secondary extrusion are discongested, secondary soup dipping, high consistency refining, cyclonic separation, bleaching, press dewatering, disappear dive handle, low dense defibrination, screening, filtering and concentrating, shove make the finished product slurry after concentrating, discongest in the operation in squeezing extrusion operation and secondary extrusion, add defibrination promoter respectively.
Described pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be that 40%-85%:60%-15% mixes by weight ratio, send into the wood chip storage warehouse, adding concentration is 30-32%, to over dry wood chip weight to be 1-2% NaOH, reaction 15-20min, after adding water washing again, enter and transfer dense groove,, wood chip moisture is controlled at 40-65% through the inclined screw dehydration.
Described pre-steaming: steam in advance in the storehouse, adding concentration is 30-32%, to over dry wood chip weight to be 0.5-2% NaOH, mixes, and temperature is controlled at 85-90 ℃, steams 15-20min in advance.
A described squeezing extrusion operation adds clear water with the wood chip after steaming in advance, and liquor ratio is 1:2-2.5, after mixing, adds respectively:
Defibrination promoter, consumption are with to over dry wood chip weight 0.2-0.3%;
H
2O
2, consumption is with to over dry wood chip weight 2-2.7%;
NaOH, consumption are with to over dry wood chip weight 5%;
DTPA, consumption are with to over dry wood chip weight 0.2-0.25%;
Na
2SiO
3, consumption is with to over dry wood chip weight 4%;
MgSO
4, consumption is with to over dry wood chip weight 0.08-0.1%,
Temperature is controlled at 70-90 ℃, reaction 3min.
Described soup dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 10-30min promptly finishes the soup dipping one time.
Described secondary extrusion is discongested, and the wood chip after a soup is flooded adds respectively:
Defibrination promoter, consumption are with to over dry wood chip weight 0.2-0.5%;
H
2O
2, consumption is with to over dry wood chip weight 5%;
NaOH, consumption are with to over dry wood chip weight 4%;
DTPA, consumption are with to over dry wood chip weight 0.25-0.28%;
Na
2SiO
3, its consumption is with to over dry wood chip weight 2.5-3%;
MgSO
4, its consumption is with to over dry wood chip weight 0.08-0.1%,
Temperature is controlled at 70-90 ℃, reaction 1-3min.
Described secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, and dipping 10-30min promptly finishes secondary soup dipping.
Described high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 1-3%, temperature is controlled at 110-145 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.0-1.5kg/cm
2, refining concentration is controlled between 35%-45%, and the slurry freedom is controlled at 150-400CSF.
Described cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively:
H
2O
2, consumption is with to over dry slurry weight 2-5%;
NaOH, consumption are with to over dry slurry weight 1.0-1.8%;
DTPA, consumption are with to over dry slurry weight 0.15-0.2%;
Na
2SiO
3, consumption is with to over dry slurry weight 0.2-0.3%;
MgSO
4, consumption is with to over dry wood chip weight 0.05-0.08%,
After cyclonic separation is finished, add water, dilute, slurry concentration after the dilution, changes bleaching tower 20-30% over to.
Described bleaching: in the bleaching tower, temperature is controlled at 80-99 ℃, bleaching 50-80min.
Described press dewatering: the slurry after will bleaching, add water, dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 3-5%.
The described processing of diving that disappears: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 3-5%, and temperature is controlled at 60-70 ℃, and the 30-60min that dives disappears.
Described low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled between 3-5%, the pulping freedom is controlled at 80-250CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%.
Described screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening.
Described filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 8-15%.
Described shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 20-30%, makes the finished product slurry.
Described defibrination promoter, a kind of in swelling agent, the bleeding agent.
Described defibrination promoter is mixing of two kinds of swelling agent and bleeding agents, and weight proportion is: swelling agent 30-50%: bleeding agent 70%-30%.
Described swelling agent is Mg (OH)
2, KOH and ZnCl
2In a kind of.
Described swelling agent is preferably ZnCl
2
Described bleeding agent, a kind of in aliphatic alcohol polyoxyvinethene phosphate, alkyl phosphate, sulfosuccinate ester salt, polyoxyethylene ether compound and the sodium butylnaphthalenesulfonate.
Described bleeding agent is preferably a kind of in aliphatic alcohol polyoxyvinethene phosphate, the alkyl phosphate.
Described defibrination promoter is swelling agent ZnCl
2, bleeding agent aliphatic alcohol polyoxyvinethene phosphate or alkyl phosphate mixing, weight proportion is: swelling agent ZnCl
240-45%: bleeding agent aliphatic alcohol polyoxyvinethene phosphate or alkyl phosphate 60-55%.
Eucalyptus, the poplar mixture material bleached chemical thermomechanical pulp of the inventive method preparation, index is as follows:
| Whiteness (ISO) | ≥82％ | Dirt count | ≤60mm 2/m 2 |
| Become the pulp fibres yield | ≥85％ | Bulk | ≥2.5cm 3/g |
| Tensile index | ≥20N·m/g | Tear index | ≥3.5N·mm 2/g |
| Opacity | ≥92％ | Fibre bundle content | ≤0.1％ |
| Folding strength | 〉=30 times |
The present invention is a raw material by choosing poplar and Eucalyptus, and mixed pulp can remedy that the eucalyptus pulp whiteness is low, the mass defect of poplar slurry bulk difference, and effectively solves timber resources quantity not sufficient, the particularly paper industry wilderness demand to the poplar material.
The present invention is in pre-steaming process, by adding a certain amount of NaOH, wood chip is soaked softening, and, strengthen the fast fully infiltration of soup to wood chip inside by adding defibrination promoter, effectively reduce the separating difficulty of wood chip fiber, reach the purpose of effective reduction machine utilization, make high dense mill power be reduced to 780-800kwh by 900-950kwh of former technology, ton slurry power consumption reduces more than the 100kwh, has significantly reduced Eucalyptus, poplar mixture material bleached chemical thermomechanical pulp slurrying energy consumption.
Technology of the present invention, through pre-steam add alkali wood chip is flooded softening after, again by add swelling agent and (or) have a bleeding agent alkaline-resisting, high temperature resistant, biodegradable characteristic, can effectively accelerate the infiltration of pulp liquor, improve the fibre swelling ability, reduce the fiber separation difficulty, make the relative littler active force of defibrination process utilization can reach the purpose that fiber effectively separates, and unnecessary that fiber is rubbed is more broken and shorter, and the abundant infiltration softening and soup of wood chip simultaneously helps promoting fibrous inside fibrillating and outside wire-dividing broom purification.Can effectively be lowered into pulp fibres Shu Hanliang after adopting the present invention, improve the physical characteristic of bleached chemical thermomechanical pulp, the pulping folding strength is brought up to for 6-8 times more than 30 times by former technology, and stock quality indexs such as bulk, tensile index, tear index are greatly improved.
Eucalyptus, poplar mixture material bleached chemical thermomechanical pulp fibre bundle content under table (one) different technology conditions are the fibre classifier of 0.15mm through sieve plate sieve seam, the fibre bundle content data contrast of detection:
Table (one):
| The test set number | 1 | 2 | 3 | 4 |
| Traditional handicraft | 1.38％ | 1.16％ | 1.28％ | 1.15％ |
| The pre-steaming adds the alkali immersion | 0.72％ | 0.57％ | 0.65％ | 0.74％ |
| Pre-steaming adds defibrination promoter after adding the alkali immersion again | 0.09％ | 0.08％ | 0.09％ | 0.07％ |
Above data comparing result shows: the pre-steaming and soup dipping operation, matching with adding defibrination promoter effectively to be lowered into pulp fibres Shu Hanliang.
The specific embodiment
Embodiment 1
(1) be swelling agent ZnCl with weight proportion
240%: bleeding agent aliphatic alcohol polyoxyvinethene phosphate 60%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 40%:60% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 30%, to over dry wood chip weight to be 1% NaOH, reaction 15min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 45%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 30%, to over dry wood chip weight to be 0.5% NaOH, mixes, and temperature is controlled at 85 ℃, steams 15min in advance;
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.5, after mixing, adds respectively: add respectively more again: defibrination promoter, consumption are with to over dry wood chip weight 0.2%; H
2O
2, consumption is with to over dry wood chip weight 2%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.2%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.08%; Temperature is controlled at 70 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 10min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded adds respectively: the defibrination promoter of step (1) preparation, consumption: to over dry wood chip weight 0.2%; H
2O
2, consumption: to over dry wood chip weight 5%; NaOH, consumption: to over dry wood chip weight 4%; DTPA, consumption: to over dry wood chip weight 0.25%; Na
2SiO
3, consumption: to over dry wood chip weight 2.5%; MgSO
4, consumption: to over dry wood chip weight 0.1%; Temperature is controlled at 70 ℃, reaction 3min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 10min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 1%, temperature is controlled at 110 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.0kg/cm
2, refining concentration is controlled at 35%, and the slurry freedom is controlled at 150CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, consumption is to over dry slurry weight 2%; NaOH, consumption are to over dry slurry weight 1.0%; DTPA, consumption are to over dry slurry weight 0.15%; Na
2SiO
3, consumption is to over dry slurry weight 0.2%; MgSO
4, consumption is to over dry wood chip weight 0.05%, after cyclonic separation is finished, adds water and dilutes, slurry concentration after the dilution, changes bleaching tower 20% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 99 ℃, bleaching 50min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 5%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 3%, and temperature is controlled at 60 ℃, and the 60min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 3%, the pulping freedom is controlled at 80CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 8%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 20%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 82.36％ | Dirt count | 55mm 2/m 2 |
| Become the pulp fibres yield | 85.7％ | Fibre bundle content | 0.09％ |
| Tensile index | 23.4N·m/g | Tear index | 3.81N·mm 2/g |
| Opacity | 93.75％ | Bulk | 2.75cm 3/g |
| Folding strength | 32 times |
Embodiment 2
(1) be swelling agent ZnCl with weight proportion
248%: bleeding agent sodium butylnaphthalenesulfonate 52%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 50%:50% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 31%, to over dry wood chip weight to be 1.2% NaOH, reaction 20min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 40%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 31%, to over dry wood chip weight to be 0.6% NaOH, mixes, and temperature is controlled at 90 ℃, steams 20min in advance;
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, consumption are with to over dry wood chip weight 0.3%; H
2O
2, consumption is with to over dry wood chip weight 2.7%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.25%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.1%; Temperature is controlled at 90 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 30min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded adds respectively: the defibrination promoter of step (1) preparation, and consumption is to over dry wood chip weight 0.2%; H
2O
2, consumption is to over dry wood chip weight 5%; NaOH, consumption are to over dry wood chip weight 4%; DTPA, consumption are to over dry wood chip weight 0.25%; Na
2SiO
3, consumption is to over dry wood chip weight 2.5%; MgSO
4, consumption is to over dry wood chip weight 0.1%, temperature is controlled at 70 ℃, reaction 3min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 10min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 3%, temperature is controlled at 145 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.5kg/cm
2, refining concentration is controlled at 45%, and the slurry freedom is controlled at 400CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, its consumption: to over dry slurry weight 5%, NaOH, its consumption: to over dry slurry weight 1.8%, DTPA, its consumption: to over dry slurry weight 0.2%, Na
2SiO
3, its consumption: to over dry slurry weight 0.3%, and MgSO
4, its consumption: to over dry wood chip weight 0.08%, after cyclonic separation is finished, add water and dilute, slurry concentration after the dilution, changes bleaching tower 30% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 80 ℃, bleaching 80min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 3%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 5%, and temperature is controlled at 70 ℃, and the 30min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 5%, the pulping freedom is controlled at 250CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 15%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 30%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 83.60％ | Dirt count | 41mm 2/m 2 |
| Become the pulp fibres yield | 87.5％ | Fibre bundle content | 0.08％ |
| Tensile index | 24.3N·m/g | Tear index | 3.68N·mm 2/g |
| Opacity | 92.10％ | Bulk | 2.52cm 3/g |
| Folding strength | 41 times |
Embodiment 3
(1) be swelling agent ZnCl with weight proportion
245%: bleeding agent alkyl phosphate 55%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 60%:40% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 32%, to over dry wood chip weight to be 1.5% NaOH, reaction 16min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 45%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 32%, to over dry wood chip weight to be 0.9% NaOH, mixes, and temperature is controlled at 86 ℃, steams 17min in advance;
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.1, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, consumption are with to over dry wood chip weight 0.21%; H
2O
2, consumption is with to over dry wood chip weight 2.1%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.21%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.09%; Temperature is controlled at 80 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 20min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded, add the defibrination promoter of step (1) preparation respectively, and consumption is to over dry wood chip weight 0.3%; H
2O
2, consumption is to over dry wood chip weight 5%; NaOH, consumption are to over dry wood chip weight 4%; DTPA, consumption are to over dry wood chip weight 0.26%; Na
2SiO
3, consumption is to over dry wood chip weight 2.6%; MgSO
4, consumption is to over dry wood chip weight 0.1%, temperature is controlled at 75 ℃, reaction 2min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 15min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 2%, temperature is controlled at 115 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.1kg/cm
2, refining concentration is controlled at 36%, and the slurry freedom is controlled at 200CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, consumption is to over dry slurry weight 3%; NaOH, consumption are to over dry slurry weight 1.2%; DTPA, consumption are to over dry slurry weight 0.16%; Na
2SiO
3, consumption is to over dry slurry weight 0.22%; MgSO
4, consumption is to over dry wood chip weight 0.06%; After cyclonic separation is finished, add water and dilute, slurry concentration after the dilution, changes bleaching tower 23% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 90 ℃, bleaching 70min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 3.6%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 5%, and temperature is controlled at 62 ℃, and the 35min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 3.5%, the pulping freedom is controlled at 100CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 9%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 22%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 82.84％ | Dirt count | 55mm 2/m 2 |
| Become the pulp fibres yield | 87.1％ | Fibre bundle content | 0.07％ |
| Tensile index | 23.9N·m/g | Tear index | 3.67N·mm 2/g |
| Opacity | 92.81％ | Bulk | 2.58cm 3/g |
| Folding strength | 33 times |
Embodiment 4
(1) with weight proportion is: swelling agent Mg (OH)
250%: bleeding agent sodium butylnaphthalenesulfonate 50%, mix and make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 85%:15% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 30%, to over dry wood chip weight to be 1.6% NaOH, reaction 17min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 55%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 31%, to over dry wood chip weight to be 1.0% NaOH, mixes, and temperature is controlled at 87 ℃, steams 16min in advance;
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.4, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, consumption are with to over dry wood chip weight 0.22%; H
2O
2, consumption is with to over dry wood chip weight 2.2%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.22%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.1%; Temperature is controlled at 78 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 12min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded adds respectively: the defibrination promoter of step (1) preparation, and consumption is to over dry wood chip weight 0.2%; H
2O
2, consumption is to over dry wood chip weight 5%; NaOH, consumption are to over dry wood chip weight 4%; DTPA, consumption are to over dry wood chip weight 0.27%; Na
2SiO
3, consumption is to over dry wood chip weight 2.9%; MgSO
4, consumption is to over dry wood chip weight 0.08%; Temperature is controlled at 84 ℃, reaction 2min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 12min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 2.5%, temperature is controlled at 132 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.3kg/cm
2, refining concentration is controlled at 41%, and the slurry freedom is controlled at 320CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, consumption is to over dry slurry weight 3.6%; NaOH, consumption are to over dry slurry weight 1.6%; DTPA, consumption are to over dry slurry weight 0.17%; Na
2SiO
3, consumption is to over dry slurry weight 0.28%; MgSO
4, consumption is to over dry wood chip weight 0.07%, after cyclonic separation is finished, adds water and dilutes, slurry concentration after the dilution, changes bleaching tower 28% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 95 ℃, bleaching 62min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 4.7%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 4.8%, and temperature is controlled at 66 ℃, and the 51min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 3.4%, the pulping freedom is controlled at 230CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 11%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 25%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 83.0％ | Dirt count | 45mm 2/m 2 |
| Become the pulp fibres yield | 87.2％ | Fibre bundle content | 0.09％ |
| Tensile index | 22.9N·m/g | Tear index | 3.69N·mm 2/g |
| Opacity | 93.11％ | Bulk | 2.63cm 3/g |
| Folding strength | 39 times |
Embodiment 5
(1) with weight proportion be: swelling agent KOH 35%: bleeding agent sulfosuccinate ester salt 65%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 80%:20% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 30%, to over dry wood chip weight to be 1.7% NaOH, reaction 19min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 62%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 32%, to over dry wood chip weight to be 1.2% NaOH, mixes, and temperature is controlled at 88 ℃, steams 17min in advance;
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.1, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, consumption are with to over dry wood chip weight 0.23%; H
2O
2, consumption is with to over dry wood chip weight 2.3%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.24%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.08%; Temperature is controlled at 70-90 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 13min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded adds respectively: the defibrination promoter of step (1) preparation, consumption: to over dry wood chip weight 0.27%; H
2O
2, consumption: to over dry wood chip weight 5%; NaOH, consumption: to over dry wood chip weight 4%; DTPA, consumption: to over dry wood chip weight 0.26%; Na
2SiO
3, consumption: to over dry wood chip weight 2.7%; MgSO
4, consumption: to over dry wood chip weight 0.1%, temperature is controlled at 83 ℃, reaction 3min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 13min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 1.8%, temperature is controlled at 120 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.49kg/cm
2, refining concentration is controlled at 37%, and the slurry freedom is controlled at 360CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, consumption is to over dry slurry weight 4.5%; NaOH, consumption are to over dry slurry weight 1.7%; DTPA, consumption are to over dry slurry weight 0.16%; Na
2SiO
3, consumption is to over dry slurry weight 0.22%; MgSO
4, consumption is to over dry wood chip weight 0.06%, after cyclonic separation is finished, adds water and dilutes, slurry concentration after the dilution, changes bleaching tower 25% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 97 ℃, bleaching 60min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 4.6%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 3.5%, and temperature is controlled at 64 ℃, and the 58min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 4.2%, the pulping freedom is controlled at 90CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 9%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 26%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 82.9％ | Dirt count | 51mm 2/m 2 |
| Become the pulp fibres yield | 87.8％ | Fibre bundle content | 0.08％ |
| Tensile index | 23.5N·m/g | Tear index | 3.72N·mm 2/g |
| Opacity | 93.27％ | Bulk | 2.59cm 3/g |
| Folding strength | 37 times |
Embodiment 6
(1) with weight proportion is: swelling agent ZnCl
246%: bleeding agent sodium butylnaphthalenesulfonate 54%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 70%:30% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 31%, to over dry wood chip weight to be 1.9% NaOH, reaction 17min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 46%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 30%, to over dry wood chip weight to be 1.8% NaOH, mixes, and temperature is controlled at 86 ℃, steams 18min in advance
(4) squeezing extrusions: wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.1, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, consumption are with to over dry wood chip weight 0.29%; H
2O
2, consumption is with to over dry wood chip weight 2.6%; NaOH, consumption are with to over dry wood chip weight 5%; DTPA, consumption are with to over dry wood chip weight 0.25%; Na
2SiO
3, consumption is with to over dry wood chip weight 4%; MgSO
4, consumption is with to over dry wood chip weight 0.1%; Temperature is controlled at 74 ℃, reaction 3min;
(5) soups dipping: change the wood chip behind squeezing extrusion over to the 1# reaction warehouse, dipping 21min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded adds respectively: the defibrination promoter of step (1) preparation, and consumption is to over dry wood chip weight 0.45%; H
2O
2, consumption is to over dry wood chip weight 5%; NaOH, consumption are to over dry wood chip weight 4%; DTPA, consumption are to over dry wood chip weight 0.27%; Na
2SiO
3, consumption is to over dry wood chip weight 2.6%; MgSO
4, consumption is to over dry wood chip weight 0.09%, temperature is controlled at 87 ℃, reaction 2min;
(7) the secondary soup floods: the wood chip after secondary extrusion is discongested changes the 2# reaction warehouse over to, dipping 27min;
(8) high consistency refining: change the wood chip behind the secondary soup dipping over to high-density paste mill, add H
2O
2, its consumption: to over dry wood chip weight 2.1%, temperature is controlled at 131 ℃, carries out high consistency refining, and the defibrination Pressure control is at 1.31kg/cm
2, refining concentration is controlled at 39%, and the slurry freedom is controlled at 265CSF;
(9) cyclonic separation: change the slurry behind the dense mill of height over to cyclone separator, add respectively: H
2O
2, consumption is to over dry slurry weight 3.7%; NaOH, consumption are to over dry slurry weight 1.4%; DTPA, consumption are to over dry slurry weight 0.2%; Na
2SiO
3, consumption is to over dry slurry weight 0.29%; MgSO
4, consumption is to over dry wood chip weight 0.07%, after cyclonic separation is finished, adds water and dilutes, slurry concentration after the dilution, changes bleaching tower 29% over to;
(10) bleaching: in the bleaching tower, temperature is controlled at 82 ℃, bleaching 66min;
(11) press dewatering: the slurry after will bleaching, add water and dilute, slurry concentration is controlled at 10%, after the dilution, carries out press dewatering, thin up again, slurry concentration is controlled at 3.3%;
(12) disappear and dive to handle: with the slurry behind the press dewatering, change the latent pond that disappears over to, slurry concentration is controlled at 4.1%, and temperature is controlled at 68 ℃, and the 44min that dives disappears;
(13) low dense defibrination: the slurry after handling of diving that will disappear, change low dense fiberizer over to after, refining concentration is controlled at 3.9%, the pulping freedom is controlled at 135CSF, after low dense defibrination is finished, enters the transition stock tank, thin up, slurry concentration is controlled at 2%;
(14) screening: will hang down the slurry behind the dense defibrination, through pressurized screen, screening;
(15) filtering and concentrating: the slurry after will screening, change disk filter over to, carry out filtering and concentrating, slurry concentration is controlled at 13%;
(16) shove concentrates: the slurry with after the filtering and concentrating, change Var-nip press over to, and carry out shove and concentrate, slurry concentration is concentrated into 21%, makes the finished product slurry.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 85％ | Dirt count | 51mm 2/m 2 |
| Become the pulp fibres yield | 87.8％ | Fibre bundle content | 0.08％ |
| Tensile index | 23.5N·m/g | Tear index | 3.72N·mm 2/g |
| Opacity | 93.27％ | Bulk | 2.59cm 3/g |
| Folding strength | 37 times |
Embodiment 7
(1) with weight proportion is: swelling agent ZnCl
240%: bleeding agent alkyl phosphate 60%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 75%:25% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 32%, to over dry wood chip weight to be 2% NaOH, reaction 18min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 63%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 30%, to over dry wood chip weight to be 2% NaOH, mixes, and temperature is controlled at 89 ℃, steams 16min in advance;
Present embodiment step (4)-(16) are identical with embodiment 6.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 85％ | Dirt count | 60mm 2/m 2 |
| Become the pulp fibres yield | 87.8％ | Fibre bundle content | 0.08％ |
| Tensile index | 24N·m/g | Tear index | 3.71N·mm 2/g |
| Opacity | 94％ | Bulk | 2.61cm 3/g |
| Folding strength | 38 times |
Embodiment 8
(1) with weight proportion is: swelling agent ZnCl
245%: bleeding agent aliphatic alcohol polyoxyvinethene phosphate 55%, mix, make defibrination promoter, standby;
(2) pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 41%:59% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 30%, to over dry wood chip weight to be 1.7% NaOH, reaction 20min, add water washing again after, enter and transfer dense groove, through the inclined screw dehydration, wood chip moisture is controlled at 59%;
(3) the pre-steaming: steam in advance in the storehouse, adding concentration is 30%, to over dry wood chip weight to be 1.7% NaOH, mixes, and temperature is controlled at 86 ℃, steams 19min in advance;
(4) squeezing extrusions: the wood chip after will steaming in advance adds clear water, and liquor ratio is 1:2.3, after mixing, adds respectively again: the defibrination promoter of step (1) preparation, and consumption is to over dry wood chip weight 0.5%; H
2O
2, consumption is to over dry wood chip weight 2.5%; NaOH, consumption are to over dry wood chip weight 5%; DTPA, consumption are to over dry wood chip weight 0.2%; Na
2SiO
3, consumption is to over dry wood chip weight 4%; MgSO
4, consumption is to over dry wood chip weight 0.08%, temperature is controlled at 90 ℃, reaction 3min;
(6) secondary extrusion is discongested: the wood chip after a soup is flooded, add the defibrination promoter of step (1) preparation respectively, and consumption is to over dry wood chip weight 0.4%; H
2O
2, consumption is to over dry wood chip weight 5%; NaOH, consumption are to over dry wood chip weight 4%; DTPA, consumption are to over dry wood chip weight 0.27%; Na
2SiO
3, consumption is to over dry wood chip weight 2.6%; MgSO
4, consumption is to over dry wood chip weight 0.08%, temperature is controlled at 88 ℃, reaction 3min;
Present embodiment step (5), (7)-(16) are identical with embodiment 1.
The bleached chemical thermomechanical pulp of present embodiment preparation, its index is as follows:
| Whiteness (ISO) | 82.9％ | Dirt count | 60mm 2/m 2 |
| Become the pulp fibres yield | 87.8％ | Fibre bundle content | 0.08％ |
| Tensile index | 23.5N·m/g | Tear index | 3.71N·mm 2/g |
| Opacity | 93.25％ | Bulk | 2.61cm 3/g |
| Folding strength | 37 times |
Claims (11)
1, the method for a kind of preparing eucalyptus, poplar mixture material bleached chemical thermomechanical pulp, its step includes: pretreatment of raw material, pre-steam, squeezing extrusion, soup dipping, a secondary extrusion are discongested, secondary soup dipping, high consistency refining, cyclonic separation, bleaching, press dewatering, disappear dive handle, low dense defibrination, screening, filtering and concentrating, shove make the finished product slurry after concentrating, it is characterized in that: discongest in the operation in squeezing extrusion operation and secondary extrusion, add defibrination promoter respectively.
2, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described pretreatment of raw material: with poplar sheet and Eucalyptus sheet, be 40%-85%:60%-15% by weight ratio, mix, send into the wood chip storage warehouse, adding concentration is 30-32%, to over dry wood chip weight to be 1-2% NaOH, reaction 15-20min, after adding water washing again, enter and transfer dense groove,, wood chip moisture is controlled at 40-65% through the inclined screw dehydration.
3, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described pre-steaming process, the pre-steaming in the storehouse, adding concentration is 30-32%, to over dry wood chip weight to be 0.5-2% NaOH, mix, temperature is controlled at 85-90 ℃, steams 15-20min in advance.
4, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: add defibrination promoter in the described squeezing extrusion operation, consumption is to 0.2-0.3% of over dry wood chip weight.
5, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described secondary extrusion is discongested and is added defibrination promoter in the operation, and consumption is to 0.2-0.5% of over dry wood chip weight.
6, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp is characterized in that: described defibrination promoter, a kind of in swelling agent, the bleeding agent.
7, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described defibrination promoter, be mixing of swelling agent and bleeding agent, weight proportion is: swelling agent 30-50%, bleeding agent 70%-30%.
8, according to the method for claim 6 or 7 described a kind of preparing eucalyptus, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described swelling agent is Mg (OH)
2, KOH and ZnCl
2In a kind of.
9, according to the method for claim 6 or 7 described a kind of preparing eucalyptus, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described swelling agent is ZnCl
2
10, according to the method for claim 6 or 7 described a kind of preparing eucalyptus, poplar mixture material bleached chemical thermomechanical pulp, it is characterized in that: described bleeding agent, a kind of in aliphatic alcohol polyoxyvinethene phosphate, alkyl phosphate, sulfosuccinate ester salt, polyoxyethylene ether compound and the sodium butylnaphthalenesulfonate.
11, the method for a kind of preparing eucalyptus according to claim 1, poplar mixture material bleached chemical thermomechanical pulp is characterized in that: described defibrination promoter is ZnCl
2With mixing of aliphatic alcohol polyoxyvinethene phosphate or alkyl phosphate, weight proportion is: ZnCl
240-45%, aliphatic alcohol polyoxyvinethene phosphate or alkyl phosphate 60-55%.
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