CN105568740B - Low whiteness sulfate leaf wood pulpboard of a kind of high intensity and preparation method thereof - Google Patents
Low whiteness sulfate leaf wood pulpboard of a kind of high intensity and preparation method thereof Download PDFInfo
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- CN105568740B CN105568740B CN201410542998.8A CN201410542998A CN105568740B CN 105568740 B CN105568740 B CN 105568740B CN 201410542998 A CN201410542998 A CN 201410542998A CN 105568740 B CN105568740 B CN 105568740B
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- 239000002023 wood Substances 0.000 title claims abstract description 255
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 title claims abstract description 108
- 238000002360 preparation method Methods 0.000 title claims abstract description 34
- 229920001131 Pulp (paper) Polymers 0.000 claims abstract description 315
- 239000002002 slurry Substances 0.000 claims abstract description 304
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 262
- 239000001301 oxygen Substances 0.000 claims abstract description 262
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 262
- 238000009835 boiling Methods 0.000 claims abstract description 144
- 238000000034 method Methods 0.000 claims abstract description 107
- 230000008569 process Effects 0.000 claims abstract description 94
- 238000004061 bleaching Methods 0.000 claims abstract description 71
- 239000007844 bleaching agent Substances 0.000 claims abstract description 45
- 239000003086 colorant Substances 0.000 claims abstract description 43
- 239000011121 hardwood Substances 0.000 claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 claims abstract description 28
- 239000000123 paper Substances 0.000 claims abstract description 24
- 238000012216 screening Methods 0.000 claims description 139
- 238000010790 dilution Methods 0.000 claims description 127
- 239000012895 dilution Substances 0.000 claims description 127
- 229920002472 Starch Polymers 0.000 claims description 126
- 239000008107 starch Substances 0.000 claims description 126
- 235000019698 starch Nutrition 0.000 claims description 126
- 238000005406 washing Methods 0.000 claims description 116
- 239000007788 liquid Substances 0.000 claims description 103
- 238000010025 steaming Methods 0.000 claims description 96
- 238000007598 dipping method Methods 0.000 claims description 93
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 90
- 230000029087 digestion Effects 0.000 claims description 48
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 40
- 238000005470 impregnation Methods 0.000 claims description 40
- 239000000284 extract Substances 0.000 claims description 39
- 238000004140 cleaning Methods 0.000 claims description 35
- 239000000243 solution Substances 0.000 claims description 31
- 239000003795 chemical substances by application Substances 0.000 claims description 26
- 239000004155 Chlorine dioxide Substances 0.000 claims description 20
- 235000019398 chlorine dioxide Nutrition 0.000 claims description 20
- 238000002803 maceration Methods 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 18
- 230000008676 import Effects 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 14
- 239000003513 alkali Substances 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 10
- 238000010411 cooking Methods 0.000 claims description 9
- 238000002386 leaching Methods 0.000 claims description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- 238000007493 shaping process Methods 0.000 claims description 8
- 238000005056 compaction Methods 0.000 claims description 6
- 230000002411 adverse Effects 0.000 claims description 5
- 230000018044 dehydration Effects 0.000 claims description 5
- 238000006297 dehydration reaction Methods 0.000 claims description 5
- 239000011259 mixed solution Substances 0.000 claims description 5
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 5
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 5
- 238000010026 decatizing Methods 0.000 claims description 2
- 244000166124 Eucalyptus globulus Species 0.000 claims 1
- 238000009826 distribution Methods 0.000 claims 1
- 229910021653 sulphate ion Inorganic materials 0.000 abstract description 5
- 238000004537 pulping Methods 0.000 abstract description 2
- 241000219927 Eucalyptus Species 0.000 description 30
- 239000000706 filtrate Substances 0.000 description 26
- 239000007789 gas Substances 0.000 description 22
- 239000002893 slag Substances 0.000 description 17
- 239000000126 substance Substances 0.000 description 17
- 238000001035 drying Methods 0.000 description 16
- 238000005507 spraying Methods 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 11
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000007664 blowing Methods 0.000 description 8
- 238000007872 degassing Methods 0.000 description 8
- 239000002027 dichloromethane extract Substances 0.000 description 8
- 239000012535 impurity Substances 0.000 description 8
- 239000002699 waste material Substances 0.000 description 8
- 241000220479 Acacia Species 0.000 description 7
- 235000010643 Leucaena leucocephala Nutrition 0.000 description 7
- 238000007865 diluting Methods 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- 238000001914 filtration Methods 0.000 description 6
- 229920005610 lignin Polymers 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 5
- 241000146433 Jacquinia keyensis Species 0.000 description 4
- 238000005520 cutting process Methods 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 3
- 230000026535 de-etiolation Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 150000002896 organic halogen compounds Chemical class 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000004076 pulp bleaching Methods 0.000 description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241001672694 Citrus reticulata Species 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000011111 cardboard Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011440 grout Substances 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000011087 paperboard Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Paper (AREA)
Abstract
The application belongs to pulping and paper-making field, more particularly to low whiteness sulfate leaf wood pulpboard of a kind of high intensity and preparation method thereof.The preparation method of the low whiteness sulphate wood pulp plate of high intensity provided by the invention comprises the following steps：A), broad-leaved wood chip is stocked up；B) wood chip boiling in white night after stocking up, obtains yellow slurry；C), the yellow slurry passes through oxygen delignification, obtains primary colors wood pulp；D), the primary colors wood pulp passes through a certain degree of controlled bleaching, obtains sulfate hardwood pulp；The dosage of bleaching agent is 10~15kg/adt in the bleaching process；E), the sulfate hardwood pulp obtains the low whiteness sulfate leaf wood pulpboard of high intensity by manufacturing paper with pulp.The preparation method of sulfate leaf wood pulpboard provided by the invention can produce the low whiteness sulfate leaf wood pulpboard of high intensity that whiteness is 75~87.5%ISO, tensile index >=60.0N.m/g, moisture are 9~13wt%.
Description
Technical field
The invention belongs to pulping and paper-making field, more particularly to a kind of low whiteness sulfate leaf wood pulpboard of high intensity and its system
Preparation Method.
Background technology
According to statistics, the total output of China's paper and cardboard has reached 86,400,000 tons at present, and total quantity consumed reaches 85,690,000 tons,
China has become the production and consumption big country of qualified paper and paper product.However, with international community in recent years and I
Attention of the state to environment and climatic issues, today that paper industry grows to even greater heights in protection of resources and ecological protection cry is by more
A large amount of freshwater resources will be consumed during more concerns, especially papermaking pulp bleaching, containing in the bleaching effluent given off can
Absorbing the hazardous contaminants such as organohalogen compounds can pollute to ecological environment, thus receive much attention.Therefore, papermaking wood pulp
Low whitenessization increasingly paid close attention to by knowledgeable people inside and outside industry.
It is well known that the bleaching of wood pulp is exactly using such as chlorine, hypochlorite, chlorine dioxide, hydrogen peroxide, ozone oxygen
Agent or sulfur dioxide, even the reproducibility bleaching agent such as diformazan sodium sulphate and wood pulp carry out chemical action, remove remaining wood in wood pulp
The process of element and chromophoric group., in use all can remaining or with cellulose etc. regardless of whether be oxidant or reducing agent
Reaction generates other kinds of harmful substance, so as to be polluted to environment.Therefore, bleachingization is reduced during pulp bleaching
The dosage of product, it can not only save the cost of bleaching chemical, moreover it is possible to reduce further issuable in bleaching process
Micro organohalogen compounds discharge, reduces environmental pollution.
The low whitenessization of certain wood pulp is not simple to pursue the more low better low whiteness wood pulp of production whiteness, but scientifically
" low drift " is carried out by the adjustment to sulphate cook technique to wood pulp using the method for environmental protection to handle, production meets low whiteness life
Apply flexibly page, the culture of low whiteness is used and the low whiteness wood pulp of low whiteness wrapping paper whiteness requirement.Although low whiteness wood pulp compared to
High brightenss bleach that in the market generally uses slurry is more environmentally-friendly, but at present the occupation rate of market of low whiteness wood pulp than relatively low, on
The research of low whiteness wood-pulp board preparation method is relatively fewer, particularly the preparation side of the low whiteness sulfate hardwood pulp of high intensity
Method, it yet there are no report.
The content of the invention
In view of this, it is an object of the invention to provide a kind of low whiteness sulfate leaf wood pulpboard of high intensity and its preparation
Method, preparation method provided by the invention can prepare the low whiteness sulfate leaf wood pulpboard of high intensity.
The invention provides a kind of low whiteness sulfate leaf wood pulpboard of high intensity, the low whiteness sulfate of the high intensity is wealthy
The whiteness of leaf wood-pulp board is 75~87.5%ISO, tensile index >=60.0N.m/g, and grammes per square metre is 850~1270g/m2, tear refers to
Number is in 6.6mN.m2/ more than g, burst index is in 4.0kPa.m2/ more than g, dichloromethane extract is in below 0.6wt%, dust
Degree is in 2.0mm2/m2Hereinafter, moisture is 9~13wt%.
The invention provides a kind of preparation method of the low whiteness sulfate leaf wood pulpboard of high intensity, comprise the following steps：
A), broad-leaved wood chip is stocked up；
B) wood chip boiling in white liquor after, stocking up, obtains yellow slurry；
The white liquor is NaOH and Na2S mixed solution；
C), the yellow slurry passes through oxygen delignification, obtains primary colors wood pulp；
D), the primary colors wood pulp obtains sulfate hardwood pulp by bleaching；
The dosage of bleaching agent is 10~15kg/adt in the bleaching process；
E), the sulfate hardwood pulp obtains sulfate leaf wood pulpboard by manufacturing paper with pulp.
Preferably, in step a), the broad-leaved wood chip is yearning between lovers wood chip, Eucalyptus piece and one kind or more in hardwood piece
Kind.
Preferably, in step a), thickness is that accounting of the 13~45mm wood chip in total wood chip is big in the wood chip after stock
In equal to 55wt%.
Preferably, in step b), NaOH concentration is 125~145g/L in the white liquor, and the sulphidity of the white liquor is
30~35%.
Preferably, the step b) specifically includes following steps：
B1 the wood chip after), stocking up obtains impregnating wood chip by dipping；
The temperature of the dipping is 80~110 DEG C；
B2), the dipping wood chip is slightly starched in white liquor mesohigh boiling；
The temperature of the autoclaving is 140~160 DEG C；The pressure of the autoclaving is 0.5~0.7MPa；The height
The liquid ratio for pressing boiling is 1.5~7m3/bdt；
B3), the thick slurry obtains yellow slurry by washing；
The dilution gfactor of the washing is 1.5~2.5m3/adt；The kappa value of the yellow slurry is 16.0~20.0.
Preferably, the step c) specifically includes following steps：
C1), the yellow slurry passes through one section of oxygen delignification, obtains one section of oxygen delignification wood pulp；
The concentration of entering to starch of one section of oxygen delignification is 10~12wt%, and pulp concentration is 10~12wt%, the time 20
~25min；Pressure is 600~800kPa, and temperature is 90~95 DEG C, and pH value is 10.8~11.5, and flow of oxygen is 10~20kg/
Adt, oxygen delignification agent dosage are 15~26kg/adt；
C2), one section of oxygen delignification wood pulp passes through two sections of oxygen delignifications, obtains two sections of oxygen delignification wood pulps；
The concentration of entering to starch of two sections of oxygen delignifications is 10~12wt%, and pulp concentration is 10~12wt%, the time 40
~45min；Pressure is 300~600kPa, and temperature is 98~110 DEG C, and pH value is 10~11, and flow of oxygen is 5~10kg/adt,
Oxygen delignification agent dosage is 0~5kg/adt；
C3), two sections of oxygen delignification wood pulps obtain primary colors wood pulp by washing；
The dilution gfactor of the washing is 2~2.5m3/adt；The kappa value of the primary colors wood pulp is 8.5~11.5.
Preferably, the step d) specifically includes following steps：
D1), the primary colors wood pulp obtains one section of bleached wood pulp by one section of bleaching；
The bleaching agent used in one section of bleaching process is chlorine dioxide, and the dosage of the bleaching agent is 9~13kg/
adt；
D2 delignification wood pulp), is obtained to one section of bleached wood pulp delignification using oxygen and alkali；
The dosage of the oxygen is less than 5kg/adt, and the dosage of the alkali is 12~13kg/adt；
D3), the delignification wood pulp passes through second stage bleaching, obtains sulfate hardwood pulp；
The bleaching agent used during the second stage bleaching is chlorine dioxide, and the dosage of the bleaching agent is 1~2kg/
adt。
Preferably, the delignification wood pulp carries out tri-stage bleaching after second stage bleaching；
The bleaching agent used during the tri-stage bleaching is chlorine dioxide or hydrogen peroxide, and the dosage of the bleaching agent is small
In 0.5kg/adt.
Preferably, the yellow slurry carries out oxygen delignification after except section, screening and washing.
Preferably, it is described except section specifically includes following steps：
The yellow slurry carries out one section except section, one section enter screening process except the good slurry that section obtains, and one section except the tailings warp of section
Carry out two sections except section after crossing dilution, two sections enter screening process except the good slurries of section, two sections of tailings except section by dilution, clean and
Cooking process is returned after dehydration.
Preferably, the described one section concentration of entering to starch for removing section is 3.0~4.3wt%, and it is 190~220kPa to enter to starch pressure, row
Slag rate is 5~21%, except section pressure difference is 10~40kPa；Described two sections are 3.0~4.3wt% except the concentration of entering to starch of section, enter slurry pressure
Power is 190~220kPa, and ash-retention efficiency is 5~24%, except section pressure difference is 10~40kPa.
Preferably, the screening specifically includes following steps：
Except the yellow slurry after section carries out one section of screening, one section is screened obtained good slurry and enters washing procedure, the tail of one section of screening
Slag carries out two sections of screenings after dilution, and the good slurry of two sections of screenings returns to one section of screening process, and the tailings of two sections of screenings passes through
Three sections of screenings are carried out after dilution, the good slurry of three sections of screenings returns to two sections of screening process, and the tailings of three sections of screenings is after dilution
Four sections of screenings are carried out, the good slurry of four sections of screenings returns to three sections of screening process.
Preferably, the concentration of entering to starch of one section of screening is 2.0~2.5wt%, and it is 200~300kPa to enter to starch pressure, sieve
It is 10~60kPa to select pressure difference；The concentration of entering to starch of two sections of screenings is 1.6~1.8wt%, and it is 100~200kPa to enter to starch pressure,
Screening pressure difference is 10~60kPa；It is described three sections screening concentration of entering to starch be 0.8~1.0wt%, enter to starch pressure be 100~
200kPa, screening pressure difference are 10~60kPa；The concentration of entering to starch of four sections of screenings is 0.8~1.0wt%, enters to starch pressure for 100
~200kPa, screening pressure difference are 10~60kPa.
Preferably, the step e) specifically includes following steps：
The sulfate hardwood pulp by fine screen choosing, wood pulp streaming, shaping, squeezing and is dried successively, obtains sulfate
Leaf wood pulpboard.
Preferably, the fine screen choosing specifically includes following steps：
The sulfate hardwood pulp carries out one section of screening, and one section is screened obtained good slurry and sent after dilution into wood pulp stream
Process, one section is screened obtained tailings and two sections of screenings is carried out after dilution, and two sections are screened obtained good slurry and return to one section of screening
Process, the tailings of two sections of screenings carry out one section of slagging-off after dilution, and one section of obtained good slurry that removes the gred returns to two sections of screening process,
One section of obtained tailings that removes the gred carries out two sections of slagging-off after dilution, and two sections of obtained good slurries that remove the gred return to one section of slagging-off process.
Preferably, the concentration of entering to starch of one section of screening is 2.8~3.2wt%, and it is 0.4~0.8MPa to enter to starch pressure；Institute
The concentration of entering to starch for stating two sections of screenings is 2.0~2.3wt%, and it is 0.15~0.35MPa to enter to starch pressure；Slurry is entered in one section of slagging-off
Concentration is 1.1~1.3wt%；The concentration of entering to starch of two sections of slagging-off is 0.5wt%.
Preferably, during the wood pulp stream is sent, the flow of wood pulp is 9500~24500L/min；Wood pulp concentration is 1.6
~2.2wt%.
Preferably, the squeezing specifically includes following steps：
Wood pulp after shaping obtains wet wood-pulp board successively by double net squeezings and heavy squeezing；
Press felt tension force is 4~8N/mm in double net expressing process；Press felt in the heavy expressing process
Tension force is 3~3.5N/mm.
Compared with prior art, the present invention is to provide a kind of low whiteness sulphate wood pulp plate of high intensity and its preparation side
Method.The preparation method of the low whiteness sulphate wood pulp plate of high intensity provided by the invention comprises the following steps：A), broad-leaved wood chip is carried out
Stock；B) wood chip boiling in white night after, stocking up, obtains yellow slurry；C), the yellow slurry passes through oxygen delignification, obtains primary colors wood
Slurry；D), the primary colors wood pulp obtains sulfate hardwood pulp by bleaching；The dosage of bleaching agent is 10 in the bleaching process
~15kg/adt；E), the sulfate hardwood pulp obtains sulfate leaf wood pulpboard by manufacturing paper with pulp.Height provided by the invention
The preparation method of low intensity whiteness sulphate wood pulp plate can produce whiteness for 75~87.5%ISO, tensile index >=
60.0N.m/g, grammes per square metre are 850~1270g/m2, tear index is in 6.6mN.m2/ more than g, burst index is in 4.0kPa.m2/ g with
On, dichloromethane extract is in below 0.6wt%, and dirt count is in 2.0mm2/m2Hereinafter, moisture is the high-strength of 9~13wt%
Spend low whiteness sulfate leaf wood pulpboard.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is the required accompanying drawing used in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
The embodiment of invention, for those of ordinary skill in the art, on the premise of not paying creative work, can also basis
The accompanying drawing of offer obtains other accompanying drawings.
Fig. 1 is the production technological process of the low whiteness sulfate leaf wood pulpboard of high intensity provided in an embodiment of the present invention.
Embodiment
The technical scheme in the embodiment of the present invention is clearly and completely described below, it is clear that described embodiment
Only part of the embodiment of the present invention, rather than whole embodiments.Based on the embodiment in the present invention, the common skill in this area
The every other embodiment that art personnel are obtained under the premise of creative work is not made, belong to the model that the present invention protects
Enclose.
The invention provides a kind of preparation method of the low whiteness sulfate leaf wood pulpboard of high intensity, comprise the following steps：
A), broad-leaved wood chip is stocked up；
B) wood chip boiling in white liquor after, stocking up, obtains yellow slurry；
The white liquor is NaOH and Na2S mixed solution；
C), the yellow slurry passes through oxygen delignification, obtains primary colors wood pulp；
D), the primary colors wood pulp obtains sulfate hardwood pulp by bleaching；
The dosage of bleaching agent is 10~15kg/adt in the bleaching process；
E), the sulfate hardwood pulp obtains sulfate leaf wood pulpboard by manufacturing paper with pulp.
In the present invention, broad-leaved wood chip carries out step a) first.The step a) is：Broad-leaved wood chip is stocked up.It is described
The process that broad-leaved wood chip is stocked up is specially：Broad-leaved wood chip is sieved.The broad-leaved wood chip is yearning between lovers wood chip, Eucalyptus piece
With the one or more in hardwood piece, preferably yearning between lovers wood chip and Eucalyptus piece.The mass ratio of the yearning between lovers wood chip and Eucalyptus piece
Preferably 0.5~2:1, more preferably 1:1.The water content of the broad-leaved wood chip is preferably 35~50wt%.Obtained after screening
The wood chip being of the required size is delivered to cooking process；The wood chip that the size obtained after screening is more than given size is crushed,
Screening process is returned after crushing to be screened again；The size obtained after screening, which is less than outside the wood chip i.e. wood chip of given size, arranges.
In the present invention, the wood chip of outer row can be used for fluidized-bed combustion boiler as fuel.The compaction degree of wood chip after stock is preferably 10~
15%；The stack density of wood chip after stock is preferably 160~230kg/m3.Bark and/or rotten material exist in wood chip after stock
Accounting in total wood chip is preferably smaller than equal to 1wt%；Thickness is less than 3mm wood chip accounting in total wood chip in wood chip after stock
Than being preferably smaller than equal to 1wt%；Thickness is that accounting of the 3~7mm wood chip in total wood chip is preferably smaller than in wood chip after stock
Equal to 6wt%；Thickness is that accounting of the 8~12mm wood chip in total wood chip is preferably smaller than equal to 8wt% in wood chip after stock；
Thickness is that accounting of the 13~45mm wood chip in total wood chip is preferably greater than or equal to 55wt% in wood chip after stock；After stock
Accounting of wood chip of the thickness more than 45mm in total wood chip is preferably smaller than equal to 2wt% in wood chip.
Wood chip after stock obtains yellow slurry by step b).The step b) is：Wood chip boiling in white liquor after stock,
Obtain yellow slurry；The white liquor is NaOH and Na2S mixed solution.The boiling in white liquor of wood chip after stock obtains the mistake of yellow slurry
Journey specifically includes following steps：
B1 the wood chip after), stocking up obtains impregnating wood chip by dipping；
The temperature of the dipping is 80~110 DEG C；
B2), the dipping wood chip is slightly starched in white liquor mesohigh boiling；
The temperature of the autoclaving is 140~160 DEG C；The pressure of the autoclaving is 0.5~0.7MPa；The height
The liquid ratio for pressing boiling is 1.5~7m3/bdt；
B3), the thick slurry obtains yellow slurry by washing；
The dilution gfactor of the washing is 1.5~2.5m3/adt；The kappa value of the yellow slurry is 16.0~20.0.
In the present invention, the wood chip after stock first passes around step b1) obtain impregnating wood chip.The step b1) be：Stock
Wood chip afterwards obtains impregnating wood chip by dipping.The maceration extract of the dipping is that boiling caused by white liquor and/or autoclaving is black
Liquid.The temperature of the dipping is preferably 80~110 DEG C.Arranged during chip impregnation outside caused dipping black liquor.In the present invention,
The dipping black liquor arranged outside preferred pair is recycled, and the dipping black liquor of outer row can obtain dense after filtering and evaporation
Contracting black liquor, the concentrated black liquor can be as the raw materials of production white liquor.To institute before chip impregnation of the present invention preferably after stock
State the wood chip after stock and carry out decatize.In the present invention, the decatize refers to the wood chip after stock being placed in high-temperature steam atmosphere
In；The high-temperature steam is preferably vapours caused by maceration extract in dipping process.
In the present invention, the decatize and dipping are preferably carried out in tower is impregnated, and the dipping tower includes upper and lower two layers of knot
Structure, upper strata are decatize section, and lower floor is impregnation stage.
In the present invention, the wood chip after stock carries out decatize in decatize section first, and decatizing steam comes from impregnation stage leaching
Upflowing vapor caused by stain liquid.Wood chip after decatize falls into impregnation stage, and wood chip is impregnated in impregnation stage.The impregnation stage is set
There is extracting sieve plate, for extracting caused dipping black liquor in dipping process.After the dipping black liquor is extracted by extracting sieve plate
Filtered, the filtrate being filtrated to get obtains concentrated black liquor after pervaporation, and the filter residue being filtrated to get enters autoclaving process.
The filtering of the black liquor is carried out preferably in black liquor filter, and the evaporation of filtrate is carried out preferably in vaporising device.
Step b1) obtained dipping wood chip passes through step b2) slightly starched.The step b2) be：The dipping wood chip exists
White liquor mesohigh boiling, is slightly starched.
In the present invention, the dipping wood chip preferably delivers to autoclaving process by current-carrying liquid.The current-carrying liquid is preferably
Maceration extract is used in dipping process.In the present invention, the dipping wood chip preferably passes through device for discharging, high pressure feeder and separation
Device delivers to autoclaving process.
In the present invention, the dipping wood chip for impregnating to obtain enters the device for discharging full of current-carrying liquid, Ran Housui from impregnation stage
Current-carrying liquid enters high pressure feeder, and high pressure feeder will impregnate wood chip and current-carrying liquid is delivered to separator, impregnate wood chip and current-carrying
Liquid separates in the separator, and isolated current-carrying liquid recycling, isolated dipping wood chip enters autoclaving process.
In autoclaving process, dipping wood chip is mixed into horizontal high voltage boiling with white liquor and slightly starched.The white liquor is
NaOH and Na2S mixed solution.NaOH concentration is preferably 125~145g/L in the white liquor；The sulphidity of the white liquor is excellent
Elect 30~35% as.The temperature of the autoclaving is preferably 140~160 DEG C.The pressure of the autoclaving is preferably 0.5~
0.7MPa.The liquid ratio of the autoclaving is preferably 1.5~7m3/bdt.In the present invention, it is preferred to first dipping wood chip is carried out
One section of autoclaving obtains one section of boiling wood pulp, and then carrying out two sections of autoclavings to one section of boiling wood pulp again is slightly starched.Institute
State dipping wood chip and carry out the processes of one section of autoclaving and two sections of autoclavings and be specially：Dipping wood chip mixes progress one with white liquor
Section autoclaving.The temperature of one section of autoclaving is preferably 140~160 DEG C, and pressure is preferably 0.5~0.7MPa, liquid material
Than being preferably 3.5~7m3/bdt.One section of black digestion liquid discharge digestion system caused by one section of autoclaving.In the present invention, it is excellent
Select and one section of black digestion liquid for discharging digestion system is recycled, the one section of black digestion liquid for discharging digestion system can be with
Dipping process is returned as maceration extract；The conveying for impregnating wood chip can also be used for as current-carrying liquid；It may also pass through filtering and steam
Concentrated black liquor is obtained after hair, the concentrated black liquor can be as the raw material of production white liquor.Wood chip is impregnated after one section of autoclaving
Obtain one section of boiling wood pulp.One section of boiling wood pulp mixes with white liquor carries out two sections of autoclavings.Two sections of autoclavings
Temperature be preferably 140~160 DEG C, pressure is preferably 0.5~0.7MPa, and liquid ratio is preferably 3.5~7m3/bdt.Two sections of height
Press two sections of black digestion liquid discharge digestion systems caused by boiling.In the present invention, it is preferred to two sections of steamings using discharge digestion system
Boil black liquor and exchanged heat with being introduced into the white liquor of digestion system, to reclaim the heat of two sections of black digestion liquids.In the present invention, it is preferred to
Two sections of black digestion liquids after heat exchanging are recycled, and two after the heat exchange section black digestion liquid can pass through filtering and evaporation
After obtain concentrated black liquor, the concentrated black liquor can be as the raw material of production white liquor.
One section of boiling wood pulp is slightly starched after two sections of autoclavings.The thick slurry passes through step b3) obtain yellow slurry.Institute
State step b3) be：Thick slurry obtains yellow slurry by washing.The dilution gfactor of the washing is preferably 1.2~2.5m3/adt.It is described
The kappa value of Huang slurry is preferably 16.0~20.0.Scrub raffinate caused by washing discharges washing system.In the present invention, it is preferred to make
Exchanged heat with the scrub raffinate of discharge washing system with the white liquor with being introduced into digestion system, to reclaim the heat of scrub raffinate
Amount.In the present invention, it is preferred to which the scrub raffinate after heat exchanging is recycled, the scrub raffinate after the heat exchange can pass through
Concentrated black liquor is obtained after filtering and evaporation, the concentrated black liquor can be as the raw material of production white liquor.
In the present invention, separation, one section of autoclaving, two sections of autoclavings and the thick slurry of the dipping wood chip and current-carrying liquid
Washing is preferably carried out in boiling tower.The boiling tower includes separator, upper steaming stage, lower steaming stage and washing section, described point
It is distributed from top to bottom along boiling tower vertical direction from device, upper steaming stage, lower steaming stage and washing section.The separator is arranged at steaming
Boil top of tower.The upper steaming stage and lower steaming stage extract sieve plate by top and separated.The lower steaming stage and washing section pass through
Bottom extracting sieve plate separates.
In the present invention, the dipping wood chip and current-carrying deliver into the separation of boiling top of tower by high pressure feeder
Device, separator separate to dipping wood chip and current-carrying, and isolated current-carrying liquid returns to device for discharging, high pressure feeder or leaching
Stain tower impregnation stage；Isolated dipping wood chip enters upper steaming stage.Upper steaming stage is provided with white liquor import, and white liquor passes through white liquor
Import enters upper steaming stage.Impregnate wood chip and white liquor and mix one section of autoclaving of progress in upper steaming stage.One section of autoclaving
One section of black digestion liquid caused by journey extracts sieve plate by top and extracts boiling tower.The one section of black digestion liquid extracted can
Device for discharging is returned as current-carrying；Also maceration extract can be used as to return to dipping tower impregnation stage；Black liquor filter, mistake can also be delivered to
Filter obtained filtrate and be delivered to vaporising device, the filter residue being filtrated to get is delivered to discharger.The one section of boiling extracted is black
Liquid preferably exchanges heat before black liquor filter is entered with being introduced into the white liquor of boiling tower.Wood chip is impregnated after one section of autoclaving
Obtain one section of boiling wood pulp.One section of boiling wood pulp enters lower steaming stage.Lower steaming stage is again provided with white liquor import, white liquor
Lower steaming stage is entered by white liquor import.One section of boiling wood pulp and white liquor mix in lower steaming stage carries out two sections of autoclavings.Two
Two sections of black digestion liquids extract sieve plate by bottom and extract boiling tower caused by during section autoclaving.Described two extracted
Section black digestion liquid is preferably delivered to black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device, and the filter residue being filtrated to get is defeated
Deliver to discharger.The two sections of black digestion liquids extracted are before black liquor filter is entered preferably with being introduced into the white of boiling tower
Liquid exchanges heat.
Steaming stage is slightly starched after carrying out two sections of autoclavings under one section of boiling wood pulp.The thick slurry enters washing section.Institute
State cleaning solution import in washing section and be arranged on washing section bottom, enter boiling tower washing section from cleaning solution import after cleaning solution supercharging
Countercurrent washing is carried out to thick slurry, scrub raffinate caused by washing extracts sieve plate by bottom and extracts boiling tower, the institute extracted
Black liquor filter can be delivered to by stating scrub raffinate, and the filtrate being filtrated to get is delivered to vaporising device, and the filter residue being filtrated to get is defeated
Deliver to discharger.The scrub raffinate extracted preferably changes before black liquor filter is entered with being introduced into the white liquor of boiling tower
Heat.Wood pulp obtains yellow slurry after washing, and Huang slurry is discharged from boiling tower thick liquid discharge mouth.In the present invention, in order to ensure boiling tower arrange
Starch the yellow slurry temperature degree at mouth and be less than 90 DEG C, the temperature that cleaning solution enters boiling tower is preferably shorter than 80 DEG C.In the present invention, control is passed through
The temperature of thick liquid discharge mouth Huang slurry processed can make the yellow strength character starched maintain a preferably level, while can prevent yellow slurry from existing
Flashed during discharge.
In the present invention, the yellow slurry of the boiling tower discharge is preferably stored in digestion blowing pot, the digestion blowing pot top
Portion is provided with normal pressure diffuser, for further being washed to Huang slurry.During diffuser normal operation, Huang slurry warp
The blow bin for spurting pot bottom is fallen into after crossing the washing of normal pressure diffuser；During diffuser failure, Huang slurry is directly entered spray
Put groove.Huang slurry is transported to follow-up workshop section after being diluted in blow bin.
The yellow slurry that step b) is obtained obtains primary colors wood pulp by step c).The step c) is：The yellow slurry takes off through peroxide
Lignin, obtain primary colors wood pulp.The process that the yellow slurry obtains primary colors wood pulp by oxygen delignification specifically includes following steps：
C1), the yellow slurry passes through one section of oxygen delignification, obtains one section of oxygen delignification wood pulp；
The concentration of entering to starch of one section of oxygen delignification is 10~12wt%, and pulp concentration is 10~12wt%, the time 20
~25min；Pressure is 600~800kPa, and temperature is 90~95 DEG C, and pH value is 10.8~11.5, and flow of oxygen is 10~20kg/
Adt, oxygen delignification agent dosage are 15~26kg/adt；
C2), one section of oxygen delignification wood pulp passes through two sections of oxygen delignifications, obtains two sections of oxygen delignification wood pulps；
The concentration of entering to starch of two sections of oxygen delignifications is 10~12wt%, and pulp concentration is 10~12wt%, the time 40
~45min；Pressure is 300~600kPa, and temperature is 98~110 DEG C, and pH value is 10~11, and flow of oxygen is 5~10kg/adt,
Oxygen delignification agent dosage is 0~5kg/adt；
C3), two sections of oxygen delignification wood pulps obtain primary colors wood pulp by washing；
The dilution gfactor of the washing is 2~2.5m3/adt；The kappa value of the primary colors wood pulp is 8.5~11.5.
In the present invention, the yellow slurry that boiling obtains passes through oxygen delignification, obtains primary colors wood pulp.The oxygen delignification refers to Huang
Starch the lignin dissolved in being starched in the presence of oxygen and oxygen delignification agent except de-etiolation.The purity of the oxygen is preferably greater than 93%；
The oxygen delignification agent is white liquor or NaOH.
In the present invention, the yellow slurry first passes around step c1) obtain one section of oxygen delignification wood pulp.The step c1) be：
The yellow slurry passes through one section of oxygen delignification, obtains one section of oxygen delignification wood pulp.The yellow slurry obtains one by one section of oxygen delignification
Section oxygen delignification wood pulp process be specially：Huang slurry, oxygen delignification agent and oxygen mix carry out one section of oxygen delignification.Described one section
The concentration of entering to starch of oxygen delignification is preferably 10~12wt%；Pulp concentration is preferably 10~12wt%；Time is preferably 20~
25min；Pressure is preferably 600~800kPa；Temperature is preferably 90~95 DEG C；PH value is preferably 10.8~11.5；Flow of oxygen
Preferably 10~20kg/adt；Oxygen delignification agent dosage is preferably 15~26kg/adt.The present invention is preferably in Huang slurry, oxygen delignification
Huang is starched before agent and oxygen mix and carries out degasification, the gas in being starched except de-etiolation.After one section of oxygen delignification terminates, obtain one section of oxygen and take off
Lignin wood pulp.
One section of oxygen delignification wood pulp passes through step c2) obtain two sections of oxygen delignification wood pulps.The step c2 is：It is described
One section of oxygen delignification wood pulp passes through two sections of oxygen delignifications, obtains two sections of oxygen delignification wood pulps.One section of oxygen delignification wood pulp warp
Crossing the process that two sections of oxygen delignifications obtain two sections of oxygen delignification wood pulps is specially：One section of oxygen delignification wood pulp, oxygen delignification agent and
Oxygen mix carries out two sections of oxygen delignifications.The concentration of entering to starch of two sections of oxygen delignifications is preferably 10~12wt%；Pulp concentration
Preferably 10~12wt%；Time is preferably 40~45min；Pressure is preferably 300~600kPa；Temperature is preferably 98~110
℃；PH value is preferably 10~11；Flow of oxygen is preferably 5~10kg/adt；Oxygen delignification agent dosage is preferably 0~5kg/adt.
The present invention carries out degasification preferably before one section of oxygen delignification wood pulp, oxygen delignification agent and oxygen mix to one section of oxygen delignification, removes
The gas gone in one section of oxygen delignification wood pulp.After two sections of oxygen delignifications terminate, two sections of oxygen delignification wood pulps are obtained.
Two sections of oxygen delignification wood pulps pass through step c3) obtain primary colors wood pulp.The step c3) be：Two sections of oxygen
Delignification wood pulp obtains primary colors wood pulp by washing.The present invention preferably takes off before two sections of oxygen delignification wood pulps wash to two sections of oxygen
Lignin wood pulp carries out degasification, removes the gas in two sections of oxygen delignification wood pulps.The dilution gfactor of the washing is preferably 2~
2.5m3/adt.The kappa value of the primary colors wood pulp is preferably 8.5~11.5.
In the present invention, yellow slurry preferably carries out oxygen delignification in the system of following device composition, including：Oxygen takes off feeding
Groove, in dense pump, first gas blender, the first chemical mixer, one section of oxygen delignification tower, second gas blender, second
Chemical mixer, two sections of oxygen delignification towers, oxygen delignification spraying pot and wash engine.The oxygen takes off feeding trough outlet dense pump with
Inlet is connected, in dense pump leakage fluid dram be connected with first gas blender inlet, first gas blender leakage fluid dram and first
Chemical mixer inlet is connected, and the first chemical mixer leakage fluid dram is connected with one section of oxygen delignification bottom of towe endfeed mouth,
One section of oxygen delignification tower top brings out material mouth and is connected with second gas blender inlet, second gas blender liquid outlet and second
Chemical mixer inlet is connected, and the second chemical mixer liquid outlet is connected with two sections of oxygen delignification bottom of towe endfeed mouths,
Two sections of oxygen delignification tower tops bring out material mouth and are connected with oxygen delignification spraying pot charging aperture, oxygen delignification spraying pot discharging opening and pulp washing
Machine inlet is connected.
In the present invention, the yellow slurry is transported to the de- feeding trough of oxygen, and oxygen takes off yellow slurry dense pump pumping in feeding trough
To one section of oxygen delignification tower charging aperture.In connection feeding trough oxygen delignification agent dog-house, oxygen are provided with the pipeline of dense pump
Delignification agent is added in yellow slurry by the dog-house, and the addition of oxygen delignification agent is according to the pH of slurries in one section of oxygen delignification tower
Value is adjusted, and keeps one section of oxygen delignification tower slurry pH value 10.8~11.5.Dense pump is equipped with off gas system in described, uses
Gas in being starched except de-etiolation.During in Huang slurry, dense pump is pumped to one section of oxygen delignification tower charging aperture in, Huang slurry is successively
By first gas blender and the first chemical mixer.The first gas blender is provided with oxygen air inlet and steam enters
Gas port, oxygen are added in yellow slurry by oxygen air inlet, and middle pressure steam is added in yellow slurry by steam inlet.Medium pressure is steamed
Vapour is used to improve yellow slurry temperature degree, and the addition of middle pressure steam is adjusted according to slurry temperature degree is entered, kept into slurry temperature degree 90~95
℃.First chemical mixer is used for oxygen delignification agent and yellow slurry is well mixed.When central dense pump is closed down, to prevent Huang
Slurry is back to oxygen from pipeline and takes off feeding trough, to close the liquid in-out valve of chemical mixer.It is mixed with oxygen and oxygen delignification
The slurries of agent enter one section of oxygen delignification tower by one section of oxygen delignification tower charging aperture.One section of oxygen delignification tower is provided with two
Individual pressure sensor, with measurement oxygen delignification tower internal pressure, oxygen delignification top of tower normal pressure is 600~800kPa.
Huang slurry in one section of oxygen delignification tower reaction terminate after, from one section of oxygen delignification tower top bring out material mouth discharge, into second gas
Blender inlet.One section of oxygen delignification tower top end discharge gate is provided with device for discharging, and the device for discharging, which is equipped with, to be removed
Gas system.In the present invention, degasification is carried out to the yellow slurry after one section of oxygen delignification and is advantageous to improve yellow slurry in two sections of oxygen delignifications
Delignification effect in tower.
Huang slurry in one section of oxygen delignification tower reaction terminate after, obtain one section of oxygen delignification wood pulp.The de- wood of one section of oxygen
The discharging opening discharge at plain wood pulp from one section of oxygen delignification tower top end is delivered to second gas blender inlet.The second gas
Blender is provided with oxygen air inlet and steam inlet, and the oxygen adds one section of oxygen delignification wood pulp by oxygen air inlet
In, middle pressure steam is added in one section of oxygen delignification wood pulp by steam inlet.The addition of medium pressure steam according to enter slurry
Temperature is adjusted, and is kept into slurry temperature degree at 98~110 DEG C.One section of oxygen delignification wood pulp goes out liquid from second gas blender
Mouth discharge, into the second chemical mixer.In the second gas blender and the connecting line of the second chemical mixer
On be provided with oxygen delignification agent dog-house, oxygen delignification agent is added in one section of oxygen delignification wood pulp by the dog-house, the de- wood of oxygen
The addition of plain agent is adjusted according to the pH value of slurries in two sections of oxygen delignification towers, keeps two sections of oxygen delignification tower slurry pH values
10~11.One section of oxygen delignification wood pulp and oxygen delignification agent mix in the second chemical mixer, pass through after well mixed
The charging aperture at two sections of oxygen delignification bottom of towe ends enters two sections of oxygen delignification towers.Two sections of oxygen delignification towers are provided with two pressure
Sensor, with measurement oxygen delignification tower internal pressure, oxygen delignification top of tower normal pressure is 300~600kPa.One section of oxygen
Delignification wood pulp reacts in two sections of oxygen delignification towers terminate after obtain two sections of oxygen delignification wood pulps, two sections of oxygen delignification wood
Slurry brings out material mouth discharge from two sections of oxygen delignification tower tops, into oxygen delignification spraying pot.
Two sections of oxygen delignification wood pulps in oxygen delignification spraying pot are discharged from spraying pot discharging opening, are delivered to wash engine.
Off gas system is equipped with the connecting line of oxygen delignification spraying pot and wash engine, for removing in two sections of oxygen delignification wood pulps
Gas.In the present invention, the wash engine is preferably DD wash engines.DD wash engines are a kind of pressure drum pulp washings of two sections of washings
Machine.In two sections of oxygen delignification wood pulp washing process, the concentration of entering to starch of DD wash engines is preferably 10~11wt%, and pulp concentration is preferred
For 11~12wt%, dilution gfactor is preferably 2~2.5m3/ adt, it is preferably 30~50kPa to enter to starch pressure, and rotating speed is preferably 1.0
~2.0rpm, filtrate electrical conductivity are preferably 0~1000us/cm.After washing terminates, primary colors wood pulp is obtained.
In the present invention, the yellow slurry carries out oxygen delignification preferably through except section, screening and after washing.
Wherein, it is described except section specifically includes following steps：
The yellow slurry carries out one section except section, one section enter screening process except the good slurry that section obtains, and one section except the tailings warp of section
Carry out two sections except section after crossing dilution, two sections enter screening process except the good slurries of section, two sections of tailings except section by dilution, clean and
Cooking process is returned after dehydration.
In the present invention, the yellow slurry enters one section except section process after dilution.Described one section is entered to starch concentration except section
Preferably 3.0~4.3wt%；It is preferably 190~220kPa to enter to starch pressure；Ash-retention efficiency is preferably 5~21%, more preferably
21%；Except section pressure difference is preferably 10~40kPa.One section enters screening process except the good slurry of section, and one section except the tailings of section is by dilute
Enter two sections after releasing except section process.So one section is preferably carried out except section in one section of knotter, one section of knotter is preferably
It is made up of 3 knotters in parallel.One section except section tailings is carried out after dilution two sections except section, described two sections except save enter to starch it is dense
Degree is preferably 3.0~4.3wt%, more preferably 4.0wt%；It is preferably 190~220kPa to enter to starch pressure, more preferably
200kPa；Ash-retention efficiency is preferably 5~24%, and more preferably 24%；Operation pressure is preferably 10~40kPa, more preferably
30kPa.Two sections enter screening process except the good slurry of section, and two sections return except the tailings of section after diluting, clean, cleaning and being dehydrated
Cooking process, the dipping process being preferably returned in cooking process.In the present invention, the described two sections tailings for removing section can also pass through
Stored after dilution, removal of impurities, cleaning and dehydration without returning to cooking process.So two sections are removed section in preferably two sections of knotters
Carry out.
In certain embodiments of the present invention, two sections of tailings for removing section are diluted and washed section described in preferred pair, after washing section
Good slurry enter screening process, wash section after tail slurry return to cooking process after diluting, cleaning and be dehydrated, be preferably returned to boiling
Dipping process in process.The section of washing preferably is carried out in section machine is washed, it is described wash section machine enter to starch concentration be preferably 0.5~
1.0wt%, tail slurry concentration of emission are preferably 28~30wt%.Described wash in section machine is provided with screen drum, and screen drum is interior to be provided with spiral, two sections
It is delivered up, is dehydrated in course of conveying by hole sizer, cleaning solution by spiral except the tailings dilution of section enters after screen drum
It is sprayed onto from upset end on the tailings after dehydration, so as to separate the fiber in tailings, is dehydrated the tail slurry after washing from screen drum top
Discharge in portion.Wash during section, good slurry enters screening process through sieve aperture.
Huang slurry is screened after except section, and the screening specifically includes following steps：
Except the yellow slurry after section carries out one section of screening, one section is screened obtained good slurry and enters washing procedure, the tail of one section of screening
Slag carries out two sections of screenings after dilution, and the good slurry of two sections of screenings returns to one section of screening process, and the tailings of two sections of screenings passes through
Three sections of screenings are carried out after dilution, the good slurry of three sections of screenings returns to two sections of screening process, and the tailings of three sections of screenings is after dilution
Four sections of screenings are carried out, the good slurry of four sections of screenings returns to three sections of screening process.
In the present invention, the yellow slurry except after section carries out one section of screening after dilution.Slurry is entered in one section of screening
Concentration is preferably 2.0~2.5wt%, and it is preferably 200~300kPa to enter to starch pressure, and screening pressure difference is preferably 10~60kPa.One section
Screen obtained good slurry and enter washing procedure, the tailings of one section of screening carries out two sections of screenings after dilution.Two sections of screenings
Concentration of entering to starch be preferably 1.6~1.8wt%, it is preferably 100~200kPa to enter to starch pressure, screening pressure difference is preferably 10~
60kPa.The good slurry of two sections of screenings returns to one section of screening process, and the tailings of two sections of screenings carries out three sections of screenings after dilution.Institute
The concentration of entering to starch for stating three sections of screenings is preferably 0.8~1.0wt%, and it is preferably 100~200kPa to enter to starch pressure, and screening pressure difference is preferred
For 10~60kPa.The good slurry of three sections of screenings returns to two sections of screening process, and the tailings of three sections of screenings carries out four sections of sieves after dilution
Choosing.In the present invention, the tailings of two sections of screenings preferably first carries out desanding after dilution, and the good slurry after desanding carries out three again
Section screening.The desanding is carried out in desander.The desander is a centrifugal purification device, and the tailings of two sections of sieves is through dilute
Desander is entered with tangential direction after releasing, rotated at a high speed in desander, the larger grains of sand of proportion fall into desanding in rotary course
Device lower end, subsequently into supplementary set device, the less slurry of proportion exits into three sections of screening process at the top of desander.Three sections of screenings
Tailings carried out after dilution four sections screening, it is described four sections screening concentration of entering to starch be preferably 0.8~1.0wt%, enter slurry pressure
Power is preferably 100~200kPa, and screening pressure difference is preferably 10~60kPa.
The good slurry of four sections of screenings returns to three sections of screening process, is arranged outside the tailings of four sections of screenings.Four sections of sieves of preferred pair of the present invention
The tailings of the outer row of choosing is squeezed, and is arranged outside the tailings done after squeezing, and the filtrate recovery for squeezing to obtain is standby.The squeezing preferably exists
Carried out in pressafiner.
In certain embodiments of the present invention, the tailings of four sections of screenings of preferred pair is diluted, washery slag.Washery slag obtains good
Starch and return to four sections of screening process, arranged outside the tailings after washery slag.Washery slag is preferably carried out in washery slag machine, the washery slag machine enter to starch it is dense
Degree is preferably 0.5~1.0wt%, more preferably 0.8~1.0wt%.The temperature of the cleaning solution used during washery slag is preferably
70~90 DEG C.The construction and operation principle of the washery slag machine are identical with the section machine of washing, and just repeat no more herein.
In the present invention, the screening of the yellow slurry is carried out in pressurized screen.The pressurized screen in screen drum and screen drum by turning
Son composition, wood pulp liquid to be screened enter at the top of screen drum, and good slurry is discharged through screen drum, tailings from screen drum bottom.Pressurized screen is run
During can be judged by the pressure difference of stock inlet and grout outlet pressurized screen operation it is whether normal, the normal operation pressure difference of pressurized screen is
10~60kPa, as screen drum is begun to block up, then pressure differential increase, slurry stream reduces., can be by reducing into slurry as screen drum blocks
Amount alleviates blockage.
Huang slurry is washed after screening, and the washing specifically includes following steps：
Yellow slurry after screening enters oxygen delignification process after carrying out first wash and second wash.
Yellow slurry after screening carries out first wash first, and the dilution gfactor of the first wash is preferably 0.8~2.0m3/
adt.First wash obtains first wash wood pulp and second wash is carried out after dilution, first wash waste liquid caused by first wash
Outer row.In the present invention, the source of the cleaning solution used first wash is not particularly limited, preferably caused by second wash
Second wash waste liquid.In the present invention, it is preferred to which the first wash waste liquid externally arranged is recycled, described one section of outer row is washed
Wash waste liquid and can return to cleaning solution of the cooking process as thick plasm scouring.The first wash is carried out in washing facility, described to wash
It is preferably 3 double roller wash engines in parallel to wash equipment.The concentration of entering to starch of the double roller wash engine is preferably 3.0~4.2wt%, is gone out
It is preferably 26~30wt% to starch concentration.
The first wash wood pulp that first wash obtains carries out second wash after dilution.The dilution of the second wash because
Son is preferably 0.8~2.0m3/adt.The second wash wood pulp that second wash obtains enters oxygen delignification process after dilution,
Arranged outside second wash waste liquid caused by second wash.The source of the cleaning solution used in the present invention second wash is not special
Limit, scrub raffinate preferably caused by two sections of oxygen delignification wood pulp washings.In the present invention, it is preferred to the second wash externally arranged
Waste liquid is recycled, and the second wash waste liquid of outer row can return to first wash work as the cleaning solution of first wash
Sequence.The second wash is carried out in washing facility, and the washing facility is preferably 2 double roller wash engines in parallel.It is described double
The concentration of entering to starch of roller wash engine is preferably 3.0~4.2wt%, and pulp concentration is preferably 26~30wt%.What second wash obtained
Second wash wood pulp enters oxygen delignification process after dilution, and the wood pulp concentration after dilution is preferably 10~12wt%.
The primary colors wood pulp obtained by step c) obtains sulfate hardwood pulp by step d).The step d) is：It is described
Primary colors wood pulp obtains sulfate hardwood pulp by bleaching.The primary colors wood pulp obtains sulfate hardwood pulp by bleaching
Process specifically includes following steps：
D1), the primary colors wood pulp obtains one section of bleached wood pulp by one section of bleaching；
The bleaching agent used in one section of bleaching process is chlorine dioxide, and the dosage of the bleaching agent is 9~13kg/
adt；
D2), one section of bleached wood pulp passes through delignification, obtains delignification wood pulp；
The delignification agent used during the delignification is oxygen and alkali, the dosage of the oxygen be less than 5kg/adt,
The dosage of the alkali is 12~13kg/adt；
D3), the delignification wood pulp passes through second stage bleaching, obtains sulfate hardwood pulp；
The bleaching agent used during the second stage bleaching is chlorine dioxide, and the dosage of the bleaching agent is 1~2kg/
adt。
The primary colors wood pulp first passes around step d1) obtain one section and drift wood pulp.The step d1) be：The primary colors wood
Slurry obtains one section of bleached wood pulp by one section of bleaching.The primary colors wood pulp obtains the mistake of one section of bleached wood pulp by one section of bleaching
Journey is specially：Primary colors wood pulp with drift agent mix progress one section drift.The bleaching agent is preferably chlorine dioxide, the bleaching agent
Dosage be preferably 9~13kg/adt.The whiteness of one section of bleached wood pulp is preferably 60~68%ISO.One section of bleaching
Purpose be to reduce the lignin content of primary colors wood pulp to a certain extent in order to follow-up bleaching.
One section of bleached wood pulp passes through step d2) obtain delignification wood pulp.The step d2) be：Use oxygen and alkali
To one section of bleached wood pulp delignification, delignification wood pulp is obtained.The dosage of the oxygen is preferably less than 5kg/adt, and the alkali is excellent
Elect NaOH as, the dosage of the alkali is preferably 12~13kg/adt.The kappa value of the delignification wood pulp is preferably 1.8~2.0；
The whiteness of the delignification wood pulp is preferably 75~80%ISO.Wood pulp after one section of bleaching still contains a small amount of wood pulp, one section of bleaching
The purpose that wood pulp carries out delignification is the lignin in further removing wood pulp, increases the whiteness of wood pulp.
The delignification wood pulp passes through step d3) obtain sulfate hardwood pulp.The step d3) be：The delignification
Wood pulp passes through second stage bleaching, obtains sulfate hardwood pulp.The delignification wood pulp obtains sulfate broad-leaved by second stage bleaching
The detailed process of wood pulp is：Delignification wood pulp mixes with bleaching agent carries out second stage bleaching.The bleaching agent is preferably chlorine dioxide,
The dosage of the bleaching agent is 1~2kg/adt.The whiteness of the sulfate wood pulp is preferably 80~87.5%ISO.Described two sections
The purpose of bleaching is the whiteness of further increase wood pulp.
The delignification wood pulp is preferred after second stage bleaching in certain embodiments of the present invention carries out tri-stage bleaching；Institute
It is chlorine dioxide or hydrogen peroxide to state the bleaching agent used during tri-stage bleaching, and the dosage of the bleaching agent is to be less than more than 0
0.5kg/adt.After tri-stage bleaching, the present invention also can obtain 87.5~89%ISO of whiteness sulfate wood pulp.
The sulfate hardwood pulp that step d) is obtained obtains sulfate leaf wood pulpboard, the step e) by step e)
For：The sulfate hardwood pulp obtains sulfate leaf wood pulpboard by manufacturing paper with pulp.The sulfate hardwood pulp is by manufacturing paper with pulp
The process for obtaining sulfate leaf wood pulpboard specifically includes following steps：
The sulfate hardwood pulp after streaming, shaping, squeezing and drying through screening, wood pulp, obtains sulfuric acid successively
Salt leaf wood pulpboard.
Wherein, it is described to specifically include following steps through screening：
The sulfate hardwood pulp carries out one section of screening, and one section is screened obtained good slurry and sent after dilution into wood pulp stream
Process, one section is screened obtained tailings and two sections of screenings is carried out after dilution, and two sections are screened obtained good slurry and return to one section of screening
Process, the tailings of two sections of screenings carry out one section of slagging-off after dilution, and one section of obtained good slurry that removes the gred returns to two sections of screening process,
One section of obtained tailings that removes the gred carries out two sections of slagging-off after dilution, and two sections of obtained good slurries that remove the gred return to one section of slagging-off process.
The sulfate hardwood pulp carries out one section of screening first, one section of screening enter to starch concentration be preferably 2.8~
3.2wt%, it is preferably 0.6MPa to enter to starch pressure.One section is screened obtained good slurry and send process into wood pulp stream after dilution, and one
The tailings that section screening obtains carries out two sections of screenings after dilution.One section of screening is preferably carried out in first pressure sieve, institute
The slurry ability of entering for stating first pressure sieve is preferably 512adt/d.One section is screened obtained tailings and enters two sections of sieves after dilution
Choosing, the concentration of entering to starch of two sections of screenings are preferably 2.0~2.3wt%, and it is preferably 0.15~0.35MPa to enter to starch pressure, pulp
Concentration is preferably 1.1~1.3wt%.Two sections are screened obtained good slurry and return to one section of screening, and the tailings of two sections of screenings is by dilution
One section of slagging-off is carried out afterwards.Two sections of screenings are preferably carried out in second pressure sieve, and it is excellent that what the second pressure was sieved enters slurry ability
Elect 192adt/d as, pulp ability is preferably 152adt/d.The tailings of two sections of screenings carries out one section of slagging-off, institute after dilution
The concentration of entering to starch for stating one section of slagging-off is preferably 1.1~1.3wt%, and pulp concentration is preferably 1~1.2wt%.One section of slagging-off obtains
Good slurry return two sections screening, one section slagging-off tailings is carried out after dilution two sections remove the gred.One section of slagging-off is preferably at 8
Carried out in scummer in parallel, the slurry ability of always entering of 8 scummers in parallel is preferably 48adt/d, and total pulp ability is excellent
Elect 37adt/d as.The tailings of one section of slagging-off carries out two sections of slagging-off after dilution, described two sections remove the gred enter to starch concentration and be preferably
0.5wt%, two sections of obtained good slurries that remove the gred return to one section of slagging-off, arranged outside the tailings of two sections of slagging-off.Two sections of slagging-off are preferably 2
Carried out in individual scummer in parallel, the slurry ability of always entering of 2 scummers in parallel is preferably 12adt/d.
Wood pulp is by after screening, carrying out wood pulp streaming, during the wood pulp stream is sent, the flow of wood pulp is preferably 9500
~24500L/min；Wood pulp concentration is preferably 1.6~2.2wt%.The wood pulp streaming is carried out preferably in head box, the stream
Slurry case is preferably to close high turbulent flow design.The wood pulp of streaming is ejected on forming net first to be shaped, and is squeezed, obtained after shaping
Wet wood-pulp board.The squeezing specifically includes following steps：
Wood pulp after shaping obtains wet wood-pulp board successively by double net squeezings and heavy squeezing；
Press felt tension force is 4~8N/mm in double net expressing process；Press felt in the heavy expressing process
Tension force is 3~3.5N/mm.The mass dryness fraction of the wet wood-pulp board is preferably greater than 45%.
In the present invention, the wood pulp after the shaping carries out double net squeezings first, net tension force in double net expressing process
Preferably 4~8N/mm, double net squeezings are carried out preferably in twin wire press.The net of the twin wire press is a width of
3750mm, working width 3600mm, spacer screen grow 24100~24200mm, the long 24100~24200mm of top net.
Wood pulp carries out heavy squeezing after double net squeezings, and the tension force of press felt is preferably in the heavy expressing process
3~3.5N/mm.The heavy squeezing is preferably carried out in heavy squeezer, and the heavy squeezer includes two transmissions and squeezed
Roller, the squeezing roller surface is covered with soft rubber, and the soft rubber thickness is preferably 22.5mm, and the hardness of the soft rubber is preferred
For 8~10.The pressure roller are preferably dimensioned to be 1200 × 3700mm of Ф.The heavy squeezer working width is 3600mm,
Woollen blanket breadth is 3750mm, pushes up the long 13500mm of blanket, the long 13500mm of bottom blanket.
The wet wood-pulp board obtained after wood pulp squeezing is dried, and obtains the low whiteness sulfate leaf wood pulpboard of high intensity.Institute
State drying to carry out preferably in drying baker, the operation speed of machine of the drying baker is preferably 60~140m/min.
Using the preparation method of the low whiteness sulfate leaf wood pulpboard of high intensity provided by the invention, can produce whiteness is
In 60.0N.m/g, grammes per square metre is 850~1270g/m for 75~87.5%ISO, >=tensile index2, tear index is in 6.6mN.m2/ g with
On, burst index is in 4.0kPa.m2/ more than g, dichloromethane extract is in below 0.6wt%, and dirt count is in 2.0mm2/m2With
Under, moisture is the 9~13wt% low whiteness sulfate leaf wood pulpboard of high intensity.It is low white using this method production high intensity
The yield for spending sulfate leaf wood pulpboard is 48.5~52%.The low whiteness sulfate leaf wood pulpboard of high intensity provided by the invention
Preparation method reduce the chemicals usage of pulp bleaching process, bleaching chemical cost can be saved, while reduce bleaching
The issuable micro organohalogen compounds discharge of process.
The invention provides a kind of low whiteness sulfate leaf wood pulpboard of high intensity, the low whiteness sulfate of the high intensity is wealthy
The whiteness of leaf wood-pulp board is 75~87.5%ISO, tensile index >=60.0N.m/g, and grammes per square metre is 850~1270g/m2, tear refers to
Number is in 6.6mN.m2/ more than g, burst index is in 4.0kPa.m2/ more than g, dichloromethane extract is in below 0.6wt%, dust
Degree is in 2.0mm2/m2Hereinafter, moisture is 9~13wt%.
The low whiteness sulfate leaf wood pulpboard whiteness of high intensity provided by the invention is moderate, and tensile index is in 60.0N.m/g
More than, tear index is in 6.6mN.m2/ more than g, burst index is in 4.0kPa.m2/ more than g, it can be used for producing low whiteness life
With paper, low whiteness cultural paper or low whiteness package paper.
The preparation method of the low whiteness sulfate leaf wood pulpboard of high intensity provided by the invention is carried out below in conjunction with the accompanying drawings
It is discussed in detail, participates in Fig. 1, Fig. 1 is the production work of the low whiteness sulfate leaf wood pulpboard of high intensity provided in an embodiment of the present invention
Skill flow chart, its step are：
Wood chip expects to be sieved in device in sieve first, and the accepted chips for sieving to obtain enters chip impregnation tower leaching stain, sieve
The wood chip got is delivered to fluidized-bed combustion boiler burning.Accepted chips is impregnated in chip impregnation tower, the dipping after dipping
Wood chip is delivered to boiling tower by discharger and high pressure feeder, impregnates caused dipping black liquor and is delivered to black liquor filter, soaks
Stain black liquor is filtered in black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device evaporation, is concentrated after evaporation
Black liquor.The discharger and high pressure feeder need the conveying dipping wood chip under current-carrying effect, and the current-carrying is maceration extract.
Dipping wood chip delivers into boiling tower with current-carrying, the boiling tower include separator, upper steaming stage, lower steaming stage and
Washing section.Dipping wood chip and current-carrying separate in boiling column separator, and the dipping wood chip after separation enters upper steaming stage, after separation
Current-carrying liquid return to high pressure feeder, discharger or chip impregnation tower.Impregnate wood chip and carry out boiling in upper steaming stage, boiling obtains
One section of boiling wood pulp enter lower steaming stage, one section of black digestion liquid caused by boiling is by being arranged on the upper extracting sieve plate of upper steaming stage
Boiling tower is extracted, one extracted section black digestion liquid can return to discharger or chip impregnation tower as upper extracting black liquor,
Black liquor filter can be entered.One section of boiling wood pulp that epimere boiling obtains enters lower steaming stage, and one section of boiling wood pulp is in lower steaming
Boil section and carry out boiling, two sections of boiling wood pulps that boiling obtains enter washing section.Two sections of boiling wood pulps wash in boiling tower washing section
After obtain yellow slurry, Huang slurry is delivered to digestion blowing pot.Washed caused by two sections of black digestion liquids caused by lower steaming stage and washing section
Waste liquid extracts boiling tower by the lower extracting sieve plate being arranged between lower steaming stage and scrubbing section, two extracted section black digestion liquid
Enter black liquor filter as lower extracting black liquor with scrub raffinate.
Huang slurry is delivered to 3 parallel connections, one section of knotter after digestion blowing pot is diluted to suitable concn, one section of knotter
Good slurry is delivered to 3 in parallel one section pressurized screens, enters two sections of knotters after the tailings dilution of one section of knotter.Two sections of knotters
Good slurry be delivered to 3 parallel connections, one section of pressurized screen, the tailings of two sections of knotters enters heavy seeds scummer after dilution.Weight is miscellaneous
The good slurry of matter scummer enters scalping, and the tailings of heavy seeds scummer is delivered to bits collecting bin.The good slurry of heavy seeds scummer
Washed and be dehydrated in scalping, obtain more dry knot, the more dry knot returns to chip impregnation tower or is delivered to section
Sub- collecting bin.
The good slurry of above-mentioned one section of knotter is screened in 3 in parallel one section pressurized screens, the good slurry of one section of pressurized screen
3 in parallel one section double roller wash engines are delivered to after dilution, the tailings of one section of pressurized screen is delivered to two sections of pressures after dilution
Power is sieved.The good slurry of two sections of pressurized screens returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens enters three sections after dilution
Pressurized screen.The good slurry of three sections of pressurized screens returns to two sections of pressurized screen charging apertures, and the tailings of three sections of pressurized screens enters four after dilution
Section pressurized screen.The good slurry of four sections of pressurized screens enters three sections of pressurized screen charging apertures, and the tailings of four sections of pressurized screens enters pressafiner.
The tailings of four sections of pressurized screens is squeezed in pressafiner, and the dry slag for squeezing to obtain is delivered to bits storehouse, squeezes what is obtained
Filtrate is delivered to filtrate storage tank.
The good slurry of above-mentioned one section of pressurized screen is washed in 3 parallel connections, one section of double roller wash engine, is produced in washing process
Scrub raffinate return to boiling tower as the cleaning solution of boiling tower washing section, good slurry after washing enters 2 simultaneously after dilution
Two sections of double roller wash engines of connection.Scrub raffinate caused by two sections of double roller wash engines returns as the cleaning solution of one section of double roller wash engine
One section of double roller wash engine, the good slurry that two sections of double roller wash engines wash to obtain are delivered to one section of oxygen delignification tower.
The good slurry that above-mentioned two sections of double roller wash engines wash to obtain carries out one section of oxygen delignification in one section of oxygen delignification tower, obtains
To one section of oxygen delignification wood pulp.One section of oxygen delignification wood pulp is delivered to two sections of oxygen delignification towers and carries out two sections of oxygen delignifications, two sections
Two sections of oxygen delignification wood pulps are obtained after oxygen delignification.Two sections of oxygen delignification wood pulps are delivered to DD wash engines, enter in DD wash engines
Row washing.Scrub raffinate returns to two sections of double roller pulp washings as the cleaning solution of two sections of double roller wash engines caused by the washing of DD wash engines
Machine.Wood pulp obtains primary colors wood pulp after the washing of DD wash engines, and primary colors wood pulp is delivered to one section of bleaching tower.
Above-mentioned primary colors wood pulp obtains one section of bleached wood pulp after one section of bleaching tower is bleached, and one section of bleached wood pulp is in delignification tower
Middle delignification, delignification wood pulp is obtained, delignification wood pulp is bleached in second stage bleaching tower, obtains sulfate hardwood pulp.
The sulfate hardwood pulp is delivered to paddle board and manufactured paper with pulp machine, is manufactured paper with pulp in paddle board manufactures paper with pulp machine, obtains the low whiteness sulfate of high intensity
Leaf wood pulpboard.
For the sake of becoming apparent from, it is described in detail below by following examples.
Embodiment 1
The low whiteness sulfate pure phase of high intensity thinks the preparation of wood-pulp board
35~50wt% of moisture yearning between lovers wood chip expects to be sieved in device in sieve, obtains accepted chips.The conjunction
Compaction degree 10~15%, the 160~190kg/m of stack density of erythrophloeum ferdii piece3.Bark and/or rotten material are total in the accepted chips
Accounting in wood chip is less than or equal to 1wt%；Accounting of wood chip of the thickness less than 3mm in total wood chip is less than or equal to 1wt%；Thickness
It is less than or equal to 6wt% for 3~7mm accounting of the wood chip in total wood chip；Thickness is 8~12mm wood chip accounting in total wood chip
Than less than or equal to 8wt%；Thickness is that accounting of the 13~45mm wood chip in total wood chip is more than or equal to 55wt%；Thickness is more than
Accounting of the 45mm wood chip in total wood chip is less than or equal to 2wt%.
Accepted chips enters chip impregnation tower decatize section after wood chip buffer and wood chip meter, impregnates tower impregnation stage
Upflowing vapor caused by the liquid of interior boiling carries out decatize and degasification to wood chip.Wood chip after decatize is in dipping tower impregnation stage leaching
Stain, dipping temperature are 80~110 DEG C.In dipping process, caused dipping black liquor is extracted by the extracting sieve plate inside dipping tower,
The dipping black liquor extracted is delivered to black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device, and filtrate is in vaporising device
In be evaporated, obtain concentrated black liquor；The filter residue being filtrated to get is delivered to discharger, is finally delivered to boiling tower.
Dipping wood chip and maceration extract after dipping are delivered to the separation of boiling top of tower by discharger and high pressure feeder
Device.Wood chip and maceration extract separation, isolated maceration extract return to discharger in top separator；Isolated impreg
Piece enters steaming stage on boiling tower.Dipping wood chip mixes in upper steaming stage with white liquor, and NaOH concentration 125 in the white liquor~
145g/L, the sulphidity 30~35% of the white liquor.The white liquor adds upper steaming stage by the white liquor import of upper steaming stage.On
The liquid ratio of steaming stage is controlled in 3.5~7m3/bdt.Impregnate wood chip and carry out one section of autoclaving, autoclaving in upper steaming stage
Temperature control at 140~160 DEG C, the Stress control of autoclaving is in 0.5~0.7MPa.One section caused by one section of autoclaving
Black digestion liquid extracts boiling tower by upper extracting sieve plate.Added by detecting residual alkali concentration in one section of black digestion liquid to adjust white liquor
Enter amount.The one section of black liquor part extracted is delivered to discharger, and a part is delivered to chip impregnation tower, and a part is delivered to black
Liquid filter.
Dipping wood chip is delivered to lower steaming stage in one section of boiling wood pulp that the progress boiling of upper steaming stage obtains.One section of boiling wood
Slurry mixes in lower steaming stage with white liquor.The white liquor adds lower steaming stage by the white liquor import of lower steaming stage, lower steaming stage
Liquid ratio is controlled in 1.5~3m3/bdt.One section of boiling wood pulp carries out two sections of autoclavings, the temperature of autoclaving in lower steaming stage
Degree control is at 140~160 DEG C, and the Stress control of autoclaving is in 0.5~0.7MPa.One section of boiling wood pulp is carried out in lower steaming stage
Two sections of boiling wood pulps that two sections of autoclavings obtain are delivered to washing section.Two sections of boiling wood pulps connect in washing section and cleaning solution adverse current
Touch.The dilution gfactor of washing is controlled in 1.2~2.5m3/adt.Wash obtained yellow slurry and be delivered to digestion blowing pot.Two sections of high pressures
Scrub raffinate caused by two sections of black digestion liquids caused by boiling and washing extracts boiling tower by lower extracting sieve plate, extracts
Two sections of black digestion liquids and scrub raffinate after being introduced into the white liquor heat exchange of boiling tower with being delivered to black liquor filter.
The normal pressure diffuser at the top of spraying pot is delivered to from the yellow slurry of boiling tower discharge, Huang slurry expands by normal pressure
Dissipate and the blow bin of spraying pot bottom is fallen into after washer washing, after the yellow slurry concentration in blow bin is diluted to 3.0~4.3wt%
It is delivered to 3 parallel connections, one section of knotter.
Huang slurry is except section in one section of knotter, and the pressure of entering to starch for setting knotter is 190~200kPa, operation pressure 10
~30kPa, ash-retention efficiency are 5~21%, and preferably one section of ash-retention efficiency is 21%.The good slurry of one section of knotter is delivered to after dilution
3 in parallel one section pressurized screens, the tailings of one section of knotter are diluted to concentration to enter two after 3.0~4.3wt% tailings liquid
Section knotter.The tailings of one section of knotter continues, except section, to set entering for knotter after being diluted to tailings liquid in two sections of knotters
Slurry pressure is 190~200kPa, and operation is 10~30kPa except section pressure difference；Ash-retention efficiency is that 5~24%, preferably two sections ash-retention efficiencies are
24%.The good slurry of two sections of knotters is delivered to 3 in parallel one section pressurized screens, enters weight after the tailings dilution in two sections of knotters
Impurity scummer.The good slurry of heavy seeds scummer enters scalping, and the tailings of heavy seeds scummer is delivered to bits collecting bin.Weight is miscellaneous
The good slurry of matter scummer is washed and is dehydrated in scalping, obtains more dry knot, and knot returns to chip impregnation tower or conveying
To knot collecting bin.
Enter 3 in parallel one section pressurized screens after good slurry dilution in one section of knotter.One section of pressurized screen enters to starch concentration
For 2.0~2.5wt%, it is 200~300kPa to enter to starch pressure, and operation pressure is 10~60kPa.The good slurry concentration of one section of pressurized screen
It is diluted to 1.0~1.2wt% and is delivered to 3 in parallel one section double roller wash engines afterwards, the tailings of one section of pressurized screen is by dilution
After be delivered to two sections of pressurized screens.The concentration of entering to starch of two sections of pressurized screens is 1.6~1.8wt%, and it is 100~200kPa to enter to starch pressure,
Operation pressure is 10~60kPa.The good slurry of two sections of pressurized screens returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens passes through
Enter desander after dilution.Arranged outside the impurity that desander is isolated, desander enters three sections of pressurized screens after obtaining good slurry dilution.Three
The concentration of entering to starch of section pressurized screen is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.Three
The good slurry of section pressurized screen returns to two sections of pressurized screen charging apertures, and the tailings of three sections of pressurized screens enters four sections of pressurized screens after dilution.
The concentration of entering to starch of four sections of pressurized screens is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.
The good slurry of four sections of pressurized screens enters three sections of pressurized screen charging apertures, and the tailings of four sections of pressurized screens enters pressafiner.Four sections of pressure
The tailings of sieve is squeezed in pressafiner, and the dry slag for squeezing to obtain is delivered to bits storehouse, squeezes obtained filtrate conveying
To filtrate storage tank.
The good slurry concentration dilution of one section of pressurized screen is delivered to 3 in parallel one section double roller pulp washings afterwards to 1.0~1.2wt%
Machine, slurries are washed in one section of double roller wash engine.The pulp concentration of one section of double roller wash engine is 12~14wt%, and one section double
The vacuum of roller wash engine operation is not less than -30kPa, and running speed is 1.0~2.0rpm.Caused washing is useless in washing process
Liquid returns to boiling tower as the cleaning solution of boiling tower washing section, good slurry concentration dilution after washing to 1.0~1.2wt% it is laggard
Enter 2 in parallel two section double roller wash engines.The pulp concentration of two sections of double roller wash engines is 12~14wt%, two sections of double roller wash engines
The vacuum of motion is not less than -30kPa, and running speed is 1.0~2.0rpm.Scrub raffinate caused by two sections of double roller wash engines is made
One section of double roller wash engine is returned to for the cleaning solution of one section of double roller wash engine, the good slurry that two sections of double roller wash engines wash to obtain is delivered to
One section of oxygen delignification tower.
The good slurry that two sections of double roller wash engines wash to obtain carries out one section of oxygen delignification in one section of oxygen delignification tower.One section of oxygen
Flow of oxygen is 10~20kg/adt during delignification, and NaOH dosages are 15~26kg/adt, and the pH value of reaction system maintains
10.8~11.5, pressure maintains 600~800kPa, and temperature maintains 90~95 DEG C, and pulp concentration is arranged to 10~
12wt%, residence time of the wood pulp in one section of oxygen delignification tower are arranged to 20~25min.One section is obtained after one section of oxygen delignification
Oxygen delignification wood pulp.One section of oxygen delignification wood pulp is delivered to two sections of oxygen delignification towers and carries out two sections of oxygen delignifications.The de- wood of two sections of oxygen
Flow of oxygen is 5~10kg/adt during element, and NaOH dosages are 0~5kg/adt, the pH value of reaction system maintains 10~
11, pressure maintains 300~600kPa, and temperature maintains 98~110 DEG C, and pulp concentration is arranged to 10~12wt%, and wood pulp exists
Residence time in two sections of oxygen delignification towers is arranged to 40~45min.Two sections of oxygen delignification wood pulps are obtained after two sections of oxygen delignifications.
Two sections of oxygen delignification wood pulps are delivered to DD wash engines, are washed in DD wash engines.DD wash engines enter to starch concentration for 10~
11wt%, pulp concentration are 11~12wt%, and dilution gfactor is 2~2.5m3/ adt, it is 30~50kPa to enter to starch pressure, and operation turns
Speed is 1.0~2.0rpm.Obtained primary colors wood pulp is delivered to one section of bleaching tower after the washing of DD wash engines, caused by washing process
Scrub raffinate returns to two sections of double roller wash engines as the cleaning solution of two sections of double roller wash engines.
Primary colors wood pulp is bleached in one section of bleaching tower, and the bleaching agent used is chlorine dioxide, the dosage of bleaching agent for 9~
13kg/adt.One section of bleached wood pulp is obtained after one section of bleaching, the whiteness of one section of bleached wood pulp is 68%ISO.
One section of bleached wood pulp is delivered to delignification tower and carries out delignification, using NaOH and oxygen to the de- wood of one section of bleached wood pulp
Element, NaOH dosages are 12~13kg/adt, and flow of oxygen is less than 5kg/adt.Delignification wood pulp, delignification are obtained after delignification
The kappa value of wood pulp is 1.8~2.0, and whiteness is 75~80%ISO.
Is bleached in delignification wood pulp conveying second stage bleaching tower, the bleaching agent used is chlorine dioxide, the use of bleaching agent
Measure as 1.2kg/adt.Sulfate yearning between lovers wood pulp is obtained after second stage bleaching, the whiteness of sulfate yearning between lovers wood pulp is 80~87.5%
ISO。
Obtain sulfate yearning between lovers wood pulp and be delivered to paddle board manufacturing paper with pulp machine.Paddle board manufacture paper with pulp machine by one section of pressurized screen, two sections of pressurized screens,
One section of scummer, two sections of scummers, head box, wet end, twin wire press, heavy squeezer and drying baker composition.Sulfate phase
Think to enter one section of pressurized screen after wood pulp dilutes first.The slurry ability of entering of one section of pressurized screen is 512adt/d, enter to starch concentration for 2.8~
3.2wt%, operating pressure 0.6MPa.The good slurry that one section of pressurized screen obtains enters head box, one section of pressurized screen after dilution
Tailings two sections of pressurized screens are carried out after dilution.The slurry ability of entering of two sections of pressurized screens is 192adt/d, enter to starch concentration for 2.0~
2.3wt%, pulp concentration are 1.1~1.3wt%, and operating pressure is 0.15~0.35MPa, and it is 152adt/d to go out good slurry ability.
The good slurry that two sections of pressurized screens obtain returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens enters 8 simultaneously after dilution
Join one section of scummer.The slurry ability of always entering of one section of scummer is 48adt/d, and it is 1.1~1.3wt% to enter to starch concentration, always goes out good slurry
Ability is 37adt/d, and pulp concentration is 1~1.2wt%.The good slurry that one section of scummer obtains returns to two sections of pressurized screen charging apertures,
The tailings of one section of slagging-off carries out 2 and the slagging-off of di- section after dilution.The slurry ability of always entering of two sections of scummers is preferably
12adt/d, it is 0.5wt% to enter to starch concentration.Good slurry that two sections of scummers obtain returns to one section of scummer charging aperture, two sections of slagging-off
Arranged outside tailings.
The good slurry that one section of pressurized screen obtains enters head box after dilution, the range of flow of head box for 9500~
24500L/min；Pulp concentration is 1.6~2.2wt%.Wood pulp is delivered to wet end by head box, wood pulp after net part forming successively
Into twin wire press and heavy squeezer, obtain mass dryness fraction and be more than 45% wet wood-pulp board.Wet wood-pulp board is delivered in drying baker and done
It is dry, obtain the low whiteness sulfate yearning between lovers wood-pulp board of high intensity.The operation speed of machine of drying baker is arranged to 60~140m/min.
The low whiteness sulfate yearning between lovers wood-pulp board of above-mentioned high intensity obtains paddle board finished product by cutting plate, packing.Trimmed size is：
900~1270g/m of grammes per square metre2, single bag weight 250kg, 5 × 685 × 800mm of pulpboard finished size；Iron wire specification used in pack thread：Ф
2.18th, Ф 2.3mm, tensile strength are respectively 980-1200N/mm2、1000-1250N/mm2。
The yield of the low whiteness sulfate yearning between lovers wood-pulp board of method production high intensity to being provided using the embodiment is counted
Calculate, be as a result 48.5~52%.The low whiteness sulfate yearning between lovers wood-pulp board of high intensity of production is detected, as a result for：Pulpboard
Whiteness is 75~87.5%ISO, tensile index >=60.0N.m/g, tear index >=6.6mN.m2/ g, burst index >=
4.0kPa.m2/ g, dichloromethane extract is below 0.6%, and dirt count is in 2.0mm2/m2Hereinafter, pulpboard grammes per square metre be 850~
1270g/m2, pulpboard moisture is 9~13wt%.
Embodiment 2
The low whiteness sulfate of high intensity mixes the preparation of eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood-pulp board
35~50wt% of moisture yearning between lovers wood chip and the Eucalyptus piece of moisture 35~50% are according to mass ratio 1:1 is mixed
Close, expect to be sieved in device in sieve, obtain accepted chips.Compaction degree 10~15%, the stack density 160 of the accepted chips
~190kg/m3.The accounting of bark and/or rotten material in total wood chip is less than or equal to 1wt% in the accepted chips；Thickness is less than
Accounting of the 3mm wood chip in total wood chip is less than or equal to 1wt%；Thickness is that accounting of the 3~7mm wood chip in total wood chip is less than
Equal to 6wt%；Thickness is that accounting of the 8~12mm wood chip in total wood chip is less than or equal to 8wt%；Thickness is 13~45mm wood
Accounting of the piece in total wood chip is more than or equal to 55wt%；Accounting of wood chip of the thickness more than 45mm in total wood chip is less than or equal to
2wt%.
Accepted chips enters chip impregnation tower decatize section after wood chip buffer and wood chip meter, impregnates tower impregnation stage
Upflowing vapor caused by the liquid of interior boiling carries out decatize and degasification to wood chip.Wood chip after decatize is in dipping tower impregnation stage leaching
Stain, dipping temperature are 80~110 DEG C.In dipping process, caused dipping black liquor is extracted by the extracting sieve plate inside dipping tower,
The dipping black liquor extracted is delivered to black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device, and filtrate is in vaporising device
In be evaporated, obtain concentrated black liquor；The filter residue being filtrated to get is delivered to discharger, is finally delivered to boiling tower.
Dipping wood chip and maceration extract after dipping are delivered to the separation of boiling top of tower by discharger and high pressure feeder
Device.Wood chip and maceration extract separation, isolated maceration extract return to discharger in top separator；Isolated impreg
Piece enters steaming stage on boiling tower.Dipping wood chip mixes in upper steaming stage with white liquor, and NaOH concentration 125 in the white liquor~
145g/L, the sulphidity 30~35% of the white liquor.The white liquor adds upper steaming stage by the white liquor import of upper steaming stage.On
The liquid ratio of steaming stage is controlled in 3.5~7m3/bdt.Impregnate wood chip and carry out one section of autoclaving, autoclaving in upper steaming stage
Temperature control at 140~160 DEG C, the Stress control of autoclaving is in 0.5~0.7MPa.One section caused by one section of autoclaving
Black digestion liquid extracts boiling tower by upper extracting sieve plate.Added by detecting residual alkali concentration in one section of black digestion liquid to adjust white liquor
Enter amount.The one section of black liquor part extracted is delivered to discharger, and a part is delivered to chip impregnation tower, and a part is delivered to black
Liquid filter.
Dipping wood chip is delivered to lower steaming stage in one section of boiling wood pulp that the progress boiling of upper steaming stage obtains.One section of boiling wood
Slurry mixes in lower steaming stage with white liquor.The white liquor adds lower steaming stage by the white liquor import of lower steaming stage, lower steaming stage
Liquid ratio is controlled in 1.5~3m3/bdt.One section of boiling wood pulp carries out two sections of autoclavings, the temperature of autoclaving in lower steaming stage
Degree control is at 140~160 DEG C, and the Stress control of autoclaving is in 0.5~0.7MPa.One section of boiling wood pulp is carried out in lower steaming stage
Two sections of boiling wood pulps that two sections of autoclavings obtain are delivered to washing section.Two sections of boiling wood pulps connect in washing section and cleaning solution adverse current
Touch.The dilution gfactor of washing is controlled in 1.2~2.5m3/adt.Wash obtained yellow slurry and be delivered to digestion blowing pot.Two sections of high pressures
Scrub raffinate caused by two sections of black digestion liquids caused by boiling and washing extracts boiling tower by lower extracting sieve plate, extracts
Two sections of black digestion liquids and scrub raffinate after being introduced into the white liquor heat exchange of boiling tower with being delivered to black liquor filter.
The normal pressure diffuser at the top of spraying pot is delivered to from the yellow slurry of boiling tower discharge, Huang slurry expands by normal pressure
Dissipate and the blow bin of spraying pot bottom is fallen into after washer washing, after the yellow slurry concentration in blow bin is diluted to 3.0~4.3wt%
It is delivered to 3 parallel connections, one section of knotter.
Huang slurry is except section in one section of knotter, and the pressure of entering to starch for setting knotter is 190~200kPa, operation pressure 10
~30kPa, ash-retention efficiency are that 5~21%, preferably one section ash-retention efficiencies are 21%.The good slurry of one section of knotter is delivered to after dilution
3 in parallel one section pressurized screens, the tailings of one section of knotter are diluted to concentration to enter two after 3.0~4.3wt% tailings liquid
Section knotter.The tailings of one section of knotter continues, except section, to set entering for knotter after being diluted to tailings liquid in two sections of knotters
Slurry pressure is 190~200kPa, and operation is 10~30kPa except section pressure difference；Ash-retention efficiency is that 5~24%, preferably two sections ash-retention efficiencies are
24%.The good slurry of two sections of knotters is delivered to 3 in parallel one section pressurized screens, enters weight after the tailings dilution in two sections of knotters
Impurity scummer.The good slurry of heavy seeds scummer enters scalping, and the tailings of heavy seeds scummer is delivered to bits collecting bin.Weight is miscellaneous
The good slurry of matter scummer is washed and is dehydrated in scalping, obtains more dry knot, and knot returns to chip impregnation tower or conveying
To knot collecting bin.
Enter 3 in parallel one section pressurized screens after good slurry dilution in one section of knotter.One section of pressurized screen enters to starch concentration
For 2.0~2.5wt%, it is 200~300kPa to enter to starch pressure, and operation pressure is 10~60kPa.The good slurry concentration of one section of pressurized screen
It is diluted to 1.0~1.2wt% and is delivered to 3 in parallel one section double roller wash engines afterwards, the tailings of one section of pressurized screen is by dilution
After be delivered to two sections of pressurized screens.The concentration of entering to starch of two sections of pressurized screens is 1.6~1.8wt%, and it is 100~200kPa to enter to starch pressure,
Operation pressure is 10~60kPa.The good slurry of two sections of pressurized screens returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens passes through
Enter desander after dilution.Arranged outside the impurity that desander is isolated, desander enters three sections of pressurized screens after obtaining good slurry dilution.Three
The concentration of entering to starch of section pressurized screen is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.Three
The good slurry of section pressurized screen returns to two sections of pressurized screen charging apertures, and the tailings of three sections of pressurized screens enters four sections of pressurized screens after dilution.
The concentration of entering to starch of four sections of pressurized screens is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.
The good slurry of four sections of pressurized screens enters three sections of pressurized screen charging apertures, and the tailings of four sections of pressurized screens enters pressafiner.Four sections of pressure
The tailings of sieve is squeezed in pressafiner, and the dry slag for squeezing to obtain is delivered to bits storehouse, squeezes obtained filtrate conveying
To filtrate storage tank.
The good slurry concentration dilution of one section of pressurized screen is delivered to 3 in parallel one section double roller pulp washings afterwards to 1.0~1.2wt%
Machine, slurries are washed in one section of double roller wash engine.The pulp concentration of one section of double roller wash engine is 12~14wt%, and one section double
The vacuum of roller wash engine operation is not less than -30kPa, and running speed is 1.0~2.0rpm.Caused washing is useless in washing process
Liquid returns to boiling tower as the cleaning solution of boiling tower washing section, good slurry concentration dilution after washing to 1.0~1.2wt% it is laggard
Enter 2 in parallel two section double roller wash engines.The pulp concentration of two sections of double roller wash engines is 12~14wt%, two sections of double roller wash engines
The vacuum of motion is not less than -30kPa, and running speed is 1.0~2.0rpm.Scrub raffinate caused by two sections of double roller wash engines is made
One section of double roller wash engine is returned to for the cleaning solution of one section of double roller wash engine, the good slurry that two sections of double roller wash engines wash to obtain is delivered to
One section of oxygen delignification tower.
The good slurry that two sections of double roller wash engines wash to obtain carries out one section of oxygen delignification in one section of oxygen delignification tower.One section of oxygen
Flow of oxygen is 10~20kg/adt during delignification, and NaOH dosages are 15~26kg/adt, and the pH value of reaction system maintains
10.8~11.5, pressure maintains 600~800kPa, and temperature maintains 90~95 DEG C, and pulp concentration is arranged to 10~
12wt%, residence time of the wood pulp in one section of oxygen delignification tower are arranged to 20~25min.One section is obtained after one section of oxygen delignification
Oxygen delignification wood pulp.One section of oxygen delignification wood pulp is delivered to two sections of oxygen delignification towers and carries out two sections of oxygen delignifications.The de- wood of two sections of oxygen
Flow of oxygen is 5~10kg/adt during element, and NaOH dosages are 0~5kg/adt, the pH value of reaction system maintains 10~
11, pressure maintains 300~600kPa, and temperature maintains 98~110 DEG C, and pulp concentration is arranged to 10~12wt%, and wood pulp exists
Residence time in two sections of oxygen delignification towers is arranged to 40~45min.Two sections of oxygen delignification wood pulps are obtained after two sections of oxygen delignifications.
Two sections of oxygen delignification wood pulps are delivered to DD wash engines, are washed in DD wash engines.DD wash engines enter to starch concentration for 10~
11wt%, pulp concentration are 11~12wt%, and dilution gfactor is 2~2.5m3/ adt, it is 30~50kPa to enter to starch pressure, and operation turns
Speed is 1.0~2.0rpm.Obtained primary colors wood pulp is delivered to one section of bleaching tower after the washing of DD wash engines, caused by washing process
Scrub raffinate returns to two sections of double roller wash engines as the cleaning solution of two sections of double roller wash engines.
Primary colors wood pulp is bleached in one section of bleaching tower, and the bleaching agent used is chlorine dioxide, the dosage of bleaching agent for 9~
13kg/adt.One section of bleached wood pulp is obtained after one section of bleaching, the whiteness of one section of bleached wood pulp is 68%ISO.
One section of bleached wood pulp is delivered to delignification tower and carries out delignification, using NaOH and oxygen to the de- wood of one section of bleached wood pulp
Element, NaOH dosages are 12~13kg/adt, and flow of oxygen is less than 5kg/adt.Delignification wood pulp, delignification are obtained after delignification
The kappa value of wood pulp is 1.8~2.0, and whiteness is 75~80%ISO.
Is bleached in delignification wood pulp conveying second stage bleaching tower, the bleaching agent used is chlorine dioxide, the use of bleaching agent
Measure as 1.2kg/adt.The low whiteness sulfate of high intensity is obtained after second stage bleaching and mixes eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood
Slurry, the whiteness that the low whiteness sulfate of high intensity mixes eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood pulp is 80~87.5%ISO.
The obtained low whiteness sulfate of high intensity mixes eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood pulp and is delivered to paddle board and copies
Make machine.Paddle board manufactures paper with pulp machine by one section of pressurized screen, two sections of pressurized screens, one section of scummer, two sections of scummers, head box, wet end, double nets
Squeezer, heavy squeezer and drying baker composition.Sulfate yearning between lovers wood pulp enters one section of pressurized screen after diluting first.One section of pressure
The slurry ability of entering of sieve is 512adt/d, and it is 2.8~3.2wt%, operating pressure 0.6MPa to enter to starch concentration.One section of pressurized screen obtains
Good slurry enter head box after dilution, the tailings of one section of pressurized screen carries out two sections of pressurized screens after dilution.Two sections of pressure
The slurry ability of entering of sieve is 192adt/d, and it is 2.0~2.3wt% to enter to starch concentration, and pulp concentration is 1.1~1.3wt%, operating pressure
For 0.15~0.35MPa, it is 152adt/d to go out good slurry ability.The good slurry that two sections of pressurized screens obtain returns to one section of pressurized screen charging
Mouthful, the tailings of two sections of pressurized screens enters 8 parallel connections, one section of scummer after dilution.The slurry ability of always entering of one section of scummer is
48adt/d, it is 1.1~1.3wt% to enter to starch concentration, and it is 37adt/d always to go out good slurry ability, and pulp concentration is 1~1.2wt%.One
The good slurry that section scummer obtains returns to two sections of pressurized screen charging apertures, and the tailings of one section of slagging-off carries out 2 and di- after dilution
Section slagging-off.The slurry ability of always entering of two sections of scummers is preferably 12adt/d, and it is 0.5wt% to enter to starch concentration.What two sections of scummers obtained
Good slurry returns to one section of scummer charging aperture, is arranged outside the tailings of two sections of slagging-off.
The good slurry that one section of pressurized screen obtains enters head box after dilution, the range of flow of head box for 9500~
24500L/min；Pulp concentration is 1.6~2.2wt%.Wood pulp is delivered to wet end by head box, wood pulp after net part forming successively
Into twin wire press and heavy squeezer, obtain mass dryness fraction and be more than 45% wet wood-pulp board.Wet wood-pulp board is delivered in drying baker
Dry, obtain the low whiteness sulfate of high intensity and mix eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood-pulp board.The work car of drying baker
Speed is arranged to 60~140m/min.
The low whiteness sulfate of above-mentioned high intensity mix eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood-pulp board by cutting plate, beat
Bag obtains paddle board finished product.Trimmed size is：900~1270g/m of grammes per square metre2, single bag weight 250kg, pulpboard finished size 5 × 685 ×
800mm；Iron wire specification used in pack thread：Ф 2.18, Ф 2.3mm, tensile strength are respectively 980-1200N/mm2、1000-
1250N/mm2。
The low whiteness sulfate of method production high intensity provided using the embodiment is mixed eucalyptus (50wt% Acacias-
50wt% Eucalyptus) yield of wood-pulp board is calculated, and it is as a result 48.5~52%.The low whiteness sulfate of high intensity of production is mixed
Eucalyptus (50wt% Acacia -50wt% Eucalyptus) wood-pulp board is detected, as a result for：Pulpboard whiteness is 75~87.5%ISO, anti-tensile
Index >=60.0N.m/g, tear index >=6.6mN.m2/ g, burst index >=in 4.0kPa.m2/ g, dichloromethane extract exist
Less than 0.6%, dirt count is in 2.0mm2/m2Hereinafter, pulpboard grammes per square metre is 850~1270g/m2, pulpboard moisture be 9~
13wt%.
Embodiment 3
The preparation of the pure Eucalyptus pulpboard of the low whiteness sulfate of high intensity
35~50wt% of moisture Eucalyptus piece expects to be sieved in device in sieve, obtains accepted chips.It is described qualified
Compaction degree 10~15%, the 160~190kg/m of stack density of wood chip3.Bark and/or rotten material are in hammer butt in the accepted chips
Accounting in piece is less than or equal to 1wt%；Accounting of wood chip of the thickness less than 3mm in total wood chip is less than or equal to 1wt%；Thickness is
Accounting of the 3~7mm wood chip in total wood chip is less than or equal to 6wt%；Thickness is accounting of the 8~12mm wood chip in total wood chip
Less than or equal to 8wt%；Thickness is that accounting of the 13~45mm wood chip in total wood chip is more than or equal to 55wt%；Thickness is more than 45mm
Accounting of the wood chip in total wood chip be less than or equal to 2wt%.
Accepted chips enters chip impregnation tower decatize section after wood chip buffer and wood chip meter, impregnates tower impregnation stage
Upflowing vapor caused by the liquid of interior boiling carries out decatize and degasification to wood chip.Wood chip after decatize is in dipping tower impregnation stage leaching
Stain, dipping temperature are 80~110 DEG C.In dipping process, caused dipping black liquor is extracted by the extracting sieve plate inside dipping tower,
The dipping black liquor extracted is delivered to black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device, and filtrate is in vaporising device
In be evaporated, obtain concentrated black liquor；The filter residue being filtrated to get is delivered to discharger, is finally delivered to boiling tower.
Dipping wood chip and maceration extract after dipping are delivered to the separation of boiling top of tower by discharger and high pressure feeder
Device.Wood chip and maceration extract separation, isolated maceration extract return to discharger in top separator；Isolated impreg
Piece enters steaming stage on boiling tower.Dipping wood chip mixes in upper steaming stage with white liquor, and NaOH concentration 125 in the white liquor~
145g/L, the sulphidity 30~35% of the white liquor.The white liquor adds upper steaming stage by the white liquor import of upper steaming stage.On
The liquid ratio of steaming stage is controlled in 3.5~7m3/bdt.Impregnate wood chip and carry out one section of autoclaving, autoclaving in upper steaming stage
Temperature control at 140~160 DEG C, the Stress control of autoclaving is in 0.5~0.7MPa.One section caused by one section of autoclaving
Black digestion liquid extracts boiling tower by upper extracting sieve plate.Added by detecting residual alkali concentration in one section of black digestion liquid to adjust white liquor
Enter amount.The one section of black liquor part extracted is delivered to discharger, and a part is delivered to chip impregnation tower, and a part is delivered to black
Liquid filter.
Dipping wood chip is delivered to lower steaming stage in one section of boiling wood pulp that the progress boiling of upper steaming stage obtains.One section of boiling wood
Slurry mixes in lower steaming stage with white liquor.The white liquor adds lower steaming stage by the white liquor import of lower steaming stage, lower steaming stage
Liquid ratio is controlled in 1.5~3m3/bdt.One section of boiling wood pulp carries out two sections of autoclavings, the temperature of autoclaving in lower steaming stage
Degree control is at 140~160 DEG C, and the Stress control of autoclaving is in 0.5~0.7MPa.One section of boiling wood pulp is carried out in lower steaming stage
Two sections of boiling wood pulps that two sections of autoclavings obtain are delivered to washing section.Two sections of boiling wood pulps connect in washing section and cleaning solution adverse current
Touch.The dilution gfactor of washing is controlled in 1.2~2.5m3/adt.Wash obtained yellow slurry and be delivered to digestion blowing pot.Two sections of high pressures
Scrub raffinate caused by two sections of black digestion liquids caused by boiling and washing extracts boiling tower by lower extracting sieve plate, extracts
Two sections of black digestion liquids and scrub raffinate after being introduced into the white liquor heat exchange of boiling tower with being delivered to black liquor filter.
The normal pressure diffuser at the top of spraying pot is delivered to from the yellow slurry of boiling tower discharge, Huang slurry expands by normal pressure
Dissipate and the blow bin of spraying pot bottom is fallen into after washer washing, after the yellow slurry concentration in blow bin is diluted to 3.0~4.3wt%
It is delivered to 3 parallel connections, one section of knotter.
Huang slurry is except section in one section of knotter, and the pressure of entering to starch for setting knotter is 190~200kPa, operation pressure 10
~30kPa, ash-retention efficiency are 5~20%.The good slurry of one section of knotter is delivered to 3 in parallel one section pressurized screens after dilution,
The tailings of one section of knotter enters two sections of knotters after being diluted to the tailings liquid that concentration is 3.0~4.3wt%.One section of knotter
Tailings continues except section after being diluted to tailings liquid in two sections of knotters, and the pressure of entering to starch for setting knotter is 190~200kPa, fortune
Row pressure difference is 10~30kPa, and ash-retention efficiency is 5~20%.The good slurry of two sections of knotters is delivered to 3 in parallel one section pressurized screens,
Enter heavy seeds scummer after tailings dilution in two sections of knotters.The good slurry of heavy seeds scummer enters scalping, and heavy seeds remove
The tailings of slag device is delivered to bits collecting bin.The good slurry of heavy seeds scummer is washed and is dehydrated in scalping, is obtained more dry
Knot, the more dry knot returns to chip impregnation tower or is delivered to knot collecting bin.
Enter 3 in parallel one section pressurized screens after good slurry dilution in one section of knotter.One section of pressurized screen enters to starch concentration
For 2.0~2.5wt%, it is 200~300kPa to enter to starch pressure, and operation pressure is 10~60kPa.The good slurry concentration of one section of pressurized screen
It is diluted to 1.0~1.2wt% and is delivered to 3 in parallel one section double roller wash engines afterwards, the tailings of one section of pressurized screen is by dilution
After be delivered to two sections of pressurized screens.The concentration of entering to starch of two sections of pressurized screens is 1.6~1.8wt%, and it is 100~200kPa to enter to starch pressure,
Operation pressure is 10~60kPa.The good slurry of two sections of pressurized screens returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens passes through
Enter desander after dilution.Arranged outside the impurity that desander is isolated, desander enters three sections of pressurized screens after obtaining good slurry dilution.Three
The concentration of entering to starch of section pressurized screen is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.Three
The good slurry of section pressurized screen returns to two sections of pressurized screen charging apertures, and the tailings of three sections of pressurized screens enters four sections of pressurized screens after dilution.
The concentration of entering to starch of four sections of pressurized screens is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.
The good slurry of four sections of pressurized screens enters three sections of pressurized screen charging apertures, and the tailings of four sections of pressurized screens enters pressafiner.Four sections of pressure
The tailings of sieve is squeezed in pressafiner, and the dry slag for squeezing to obtain is delivered to bits storehouse, squeezes obtained filtrate conveying
To filtrate storage tank.
The good slurry concentration dilution of one section of pressurized screen is delivered to 3 in parallel one section double roller pulp washings afterwards to 1.0~1.2wt%
Machine, slurries are washed in one section of double roller wash engine.The pulp concentration of one section of double roller wash engine is 12~14wt%, and one section double
The vacuum of roller wash engine operation is not less than -30kPa, and running speed is 1.0~2.0rpm.Caused washing is useless in washing process
Liquid returns to boiling tower as the cleaning solution of boiling tower washing section, good slurry concentration dilution after washing to 1.0~1.2wt% it is laggard
Enter 2 in parallel two section double roller wash engines.The pulp concentration of two sections of double roller wash engines is 12~14wt%, two sections of double roller wash engines
The vacuum of motion is not less than -30kPa, and running speed is 1.0~2.0rpm.Scrub raffinate caused by two sections of double roller wash engines is made
One section of double roller wash engine is returned to for the cleaning solution of one section of double roller wash engine, the good slurry that two sections of double roller wash engines wash to obtain is delivered to
One section of oxygen delignification tower.
The good slurry that two sections of double roller wash engines wash to obtain carries out one section of oxygen delignification in one section of oxygen delignification tower.One section of oxygen
Flow of oxygen is 10~20kg/adt during delignification, and NaOH dosages are 15~26kg/adt, and the pH value of reaction system maintains
10.8~11.5, pressure maintains 600~800kPa, and temperature maintains 90~95 DEG C, and pulp concentration is arranged to 10~
12wt%, residence time of the wood pulp in one section of oxygen delignification tower are arranged to 20~25min.One section is obtained after one section of oxygen delignification
Oxygen delignification wood pulp.One section of oxygen delignification wood pulp is delivered to two sections of oxygen delignification towers and carries out two sections of oxygen delignifications.The de- wood of two sections of oxygen
Flow of oxygen is 5~10kg/adt during element, and NaOH dosages are 0~5kg/adt, the pH value of reaction system maintains 10~
11, pressure maintains 300~600kPa, and temperature maintains 98~110 DEG C, and pulp concentration is arranged to 10~12wt%, and wood pulp exists
Residence time in two sections of oxygen delignification towers is arranged to 40~45min.Two sections of oxygen delignification wood pulps are obtained after two sections of oxygen delignifications.
Two sections of oxygen delignification wood pulps are delivered to DD wash engines, are washed in DD wash engines.DD wash engines enter to starch concentration for 10~
11wt%, pulp concentration are 11~12wt%, and dilution gfactor is 2~2.5m3/ adt, it is 30~50kPa to enter to starch pressure, and operation turns
Speed is 1.0~2.0rpm.Obtained primary colors wood pulp is delivered to one section of bleaching tower after the washing of DD wash engines, caused by washing process
Scrub raffinate returns to two sections of double roller wash engines as the cleaning solution of two sections of double roller wash engines.
Primary colors wood pulp is bleached in one section of bleaching tower, and the bleaching agent used is chlorine dioxide, the dosage of bleaching agent for 9~
13kg/adt.One section of bleached wood pulp is obtained after one section of bleaching, the whiteness of one section of bleached wood pulp is 68%ISO.
One section of bleached wood pulp is delivered to delignification tower and carries out delignification, using NaOH and oxygen to the de- wood of one section of bleached wood pulp
Element, NaOH dosages are 12~13kg/adt, and flow of oxygen is less than 5kg/adt.Delignification wood pulp, delignification are obtained after delignification
The kappa value of wood pulp is 1.8~2.0, and whiteness is 75~80%ISO.
Is bleached in delignification wood pulp conveying second stage bleaching tower, the bleaching agent used is chlorine dioxide, the use of bleaching agent
Measure as 1.2kg/adt.The low whiteness sulfate eucalyptus pulp of high intensity, the low whiteness sulfate eucalyptus pulp of high intensity are obtained after second stage bleaching
Whiteness be 80~87.5%ISO.
The obtained low whiteness sulfate eucalyptus pulp of high intensity is delivered to paddle board and manufactured paper with pulp machine.Paddle board manufactures paper with pulp machine by one section of pressure
Sieve, two sections of pressurized screens, one section of scummer, two sections of scummers, head box, wet end, twin wire press, heavy squeezer and drying baker
Composition.Sulfate yearning between lovers wood pulp enters one section of pressurized screen after diluting first.The slurry ability of entering of one section of pressurized screen is 512adt/d, is entered
Slurry concentration is 2.8~3.2wt%, operating pressure 0.6MPa.The good slurry that one section of pressurized screen obtains is by diluting the laggard slurry that becomes a mandarin
Case, the tailings of one section of pressurized screen carry out two sections of pressurized screens after dilution.The slurry ability of entering of two sections of pressurized screens is 192adt/d, is entered
Slurry concentration is 2.0~2.3wt%, and pulp concentration is 1.1~1.3wt%, and operating pressure is 0.15~0.35MPa, goes out good slurry energy
Power is 152adt/d.The good slurry that two sections of pressurized screens obtain returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens is by dilute
Enter 8 parallel connections, one section of scummer after releasing.The slurry ability of always entering of one section of scummer is 48adt/d, enter to starch concentration for 1.1~
1.3wt%, it is 37adt/d always to go out good slurry ability, and pulp concentration is 1~1.2wt%.The good slurry that one section of scummer obtains returns to two
Section pressurized screen charging aperture, the tailings of one section of slagging-off carry out 2 and the slagging-off of di- section after dilution.Two sections of scummers always enter slurry
Ability is preferably 12adt/d, and it is 0.5wt% to enter to starch concentration.The good slurry that two sections of scummers obtain returns to one section of scummer charging aperture,
Arranged outside the tailings of two sections of slagging-off.
The good slurry that one section of pressurized screen obtains enters head box after dilution, the range of flow of head box for 9500~
24500L/min；Pulp concentration is 1.6~2.2wt%.Wood pulp is delivered to wet end by head box, wood pulp after net part forming successively
Into twin wire press and heavy squeezer, obtain mass dryness fraction and be more than 45% wet wood-pulp board.Wet wood-pulp board is delivered in drying baker and done
It is dry, obtain the pure Eucalyptus pulpboard of the low whiteness sulfate of high intensity.The operation speed of machine of drying baker is arranged to 60~140m/min.
The low pure Eucalyptus pulpboard of whiteness sulfate of above-mentioned high intensity obtains paddle board finished product by cutting plate, packing.Trimmed size is：
900~1270g/m of grammes per square metre2, single bag weight 250kg, 5 × 685 × 800mm of pulpboard finished size；Iron wire specification used in pack thread：Ф
2.18th, Ф 2.3mm, tensile strength are respectively 980-1200N/mm2、1000-1250N/mm2。
The yield of the low pure Eucalyptus pulpboard of whiteness sulfate of method production high intensity to being provided using the embodiment is counted
Calculate, be as a result 48.5~52%.The pure Eucalyptus pulpboard of the low whiteness sulfate of high intensity of production is detected, as a result for：Pulpboard
Whiteness is 75~87.5%ISO, tensile index >=60.0N.m/g, tear index >=6.6mN.m2/ g, burst index >=
4.0kPa.m2/ g, dichloromethane extract is below 0.6%, and dirt count is in 2.0mm2/m2Hereinafter, pulpboard grammes per square metre be 850~
1270g/m2, pulpboard moisture is 9~13wt%.
Embodiment 4
The preparation of the low whiteness sulfate hardwood pulpboard of high intensity
35~50wt% of moisture hardwood piece expects to be sieved in device in sieve, obtains accepted chips.The conjunction
Compaction degree 10~15%, the 160~190kg/m of stack density of erythrophloeum ferdii piece3.Bark and/or rotten material are total in the accepted chips
Accounting in wood chip is less than or equal to 1wt%；Accounting of wood chip of the thickness less than 3mm in total wood chip is less than or equal to 1wt%；Thickness
It is less than or equal to 6wt% for 3~7mm accounting of the wood chip in total wood chip；Thickness is 8~12mm wood chip accounting in total wood chip
Than less than or equal to 8wt%；Thickness is that accounting of the 13~45mm wood chip in total wood chip is more than or equal to 55wt%；Thickness is more than
Accounting of the 45mm wood chip in total wood chip is less than or equal to 2wt%.
Accepted chips enters chip impregnation tower decatize section after wood chip buffer and wood chip meter, impregnates tower impregnation stage
Upflowing vapor caused by the liquid of interior boiling carries out decatize and degasification to wood chip.Wood chip after decatize is in dipping tower impregnation stage leaching
Stain, dipping temperature are 80~110 DEG C.In dipping process, caused dipping black liquor is extracted by the extracting sieve plate inside dipping tower,
The dipping black liquor extracted is delivered to black liquor filter, and the filtrate being filtrated to get is delivered to vaporising device, and filtrate is in vaporising device
In be evaporated, obtain concentrated black liquor；The filter residue being filtrated to get is delivered to discharger, is finally delivered to boiling tower.
Dipping wood chip and maceration extract after dipping are delivered to the separation of boiling top of tower by discharger and high pressure feeder
Device.Wood chip and maceration extract separation, isolated maceration extract return to discharger in top separator；Isolated impreg
Piece enters steaming stage on boiling tower.Dipping wood chip mixes in upper steaming stage with white liquor, and NaOH concentration 125 in the white liquor~
145g/L, the sulphidity 30~35% of the white liquor.The white liquor adds upper steaming stage by the white liquor import of upper steaming stage.On
The liquid ratio of steaming stage is controlled in 3.5~7m3/bdt.Impregnate wood chip and carry out autoclaving, the temperature of autoclaving in upper steaming stage
Degree control is at 140~160 DEG C, and the Stress control of autoclaving is in 0.5~0.7MPa.One section of black digestion liquid caused by during boiling
Boiling tower is extracted by upper extracting sieve plate.White liquor addition is adjusted by residual alkali concentration in one section of black digestion liquid of detection.Take out
The one section of black liquor part proposed is delivered to discharger, and a part is delivered to chip impregnation tower, and a part is delivered to black liquor filtering
Machine.
Dipping wood chip is delivered to lower steaming stage in one section of boiling wood pulp that the progress boiling of upper steaming stage obtains.One section of boiling wood
Slurry mixes in lower steaming stage with white liquor.The white liquor adds lower steaming stage by the white liquor import of lower steaming stage, lower steaming stage
Liquid ratio is controlled in 1.5~3m3/bdt.One section of boiling wood pulp carries out two sections of autoclavings, the temperature of autoclaving in lower steaming stage
Degree control is at 140~160 DEG C, and the Stress control of autoclaving is in 0.5~0.7MPa.One section of boiling wood pulp is carried out in lower steaming stage
Two sections of boiling wood pulps that two sections of autoclavings obtain are delivered to washing section.Two sections of boiling wood pulps connect in washing section and cleaning solution adverse current
Touch.The dilution gfactor of washing is controlled in 1.2~2.5m3/adt.Wash obtained yellow slurry and be delivered to digestion blowing pot.Two sections of high pressures
Scrub raffinate caused by two sections of black digestion liquids caused by boiling and washing extracts boiling tower by lower extracting sieve plate, extracts
Two sections of black digestion liquids and scrub raffinate after being introduced into the white liquor heat exchange of boiling tower with being delivered to black liquor filter.
The normal pressure diffuser at the top of spraying pot is delivered to from the yellow slurry of boiling tower discharge, Huang slurry expands by normal pressure
Dissipate and the blow bin of spraying pot bottom is fallen into after washer washing, after the yellow slurry concentration in blow bin is diluted to 3.0~4.3wt%
It is delivered to 3 parallel connections, one section of knotter.
Huang slurry is except section in one section of knotter, and the pressure of entering to starch for setting knotter is 190~200kPa, operation pressure 10
~30kPa, ash-retention efficiency are that 5~21%, preferably one section ash-retention efficiencies are 21%.The good slurry of one section of knotter is delivered to after dilution
3 in parallel one section pressurized screens, the tailings of one section of knotter are diluted to concentration to enter two after 3.0~4.3wt% tailings liquid
Section knotter.The tailings of one section of knotter continues, except section, to set entering for knotter after being diluted to tailings liquid in two sections of knotters
Slurry pressure is 190~200kPa, and operation is 10~30kPa except section pressure difference；Ash-retention efficiency is that 5~24%, preferably two sections ash-retention efficiencies are
24%.The good slurry of two sections of knotters is delivered to 3 in parallel one section pressurized screens, enters weight after the tailings dilution in two sections of knotters
Impurity scummer.The good slurry of heavy seeds scummer enters scalping, and the tailings of heavy seeds scummer is delivered to bits collecting bin.Weight is miscellaneous
The good slurry of matter scummer is washed and is dehydrated in scalping, obtains more dry knot, and knot returns to chip impregnation tower or conveying
To knot collecting bin.
Enter 3 in parallel one section pressurized screens after good slurry dilution in one section of knotter.One section of pressurized screen enters to starch concentration
For 2.0~2.5wt%, it is 200~300kPa to enter to starch pressure, and operation pressure is 10~60kPa.The good slurry concentration of one section of pressurized screen
It is diluted to 1.0~1.2wt% and is delivered to 3 in parallel one section double roller wash engines afterwards, the tailings of one section of pressurized screen is by dilution
After be delivered to two sections of pressurized screens.The concentration of entering to starch of two sections of pressurized screens is 1.6~1.8wt%, and it is 100~200kPa to enter to starch pressure,
Operation pressure is 10~60kPa.The good slurry of two sections of pressurized screens returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens passes through
Enter desander after dilution.Arranged outside the impurity that desander is isolated, desander enters three sections of pressurized screens after obtaining good slurry dilution.Three
The concentration of entering to starch of section pressurized screen is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.Three
The good slurry of section pressurized screen returns to two sections of pressurized screen charging apertures, and the tailings of three sections of pressurized screens enters four sections of pressurized screens after dilution.
The concentration of entering to starch of four sections of pressurized screens is 0.8~1.0wt%, and it is 100~200kPa to enter to starch pressure, and operation pressure is 10~60kPa.
The good slurry of four sections of pressurized screens enters three sections of pressurized screen charging apertures, and the tailings of four sections of pressurized screens enters pressafiner.Four sections of pressure
The tailings of sieve is squeezed in pressafiner, and the dry slag for squeezing to obtain is delivered to bits storehouse, squeezes obtained filtrate conveying
To filtrate storage tank.
The good slurry concentration dilution of one section of pressurized screen is delivered to 3 in parallel one section double roller pulp washings afterwards to 1.0~1.2wt%
Machine, slurries are washed in one section of double roller wash engine.The pulp concentration of one section of double roller wash engine is 12~14wt%, and one section double
The vacuum of roller wash engine operation is not less than -30kPa, and running speed is 1.0~2.0rpm.Caused washing is useless in washing process
Liquid returns to boiling tower as the cleaning solution of boiling tower washing section, good slurry concentration dilution after washing to 1.0~1.2wt% it is laggard
Enter 2 in parallel two section double roller wash engines.The pulp concentration of two sections of double roller wash engines is 12~14wt%, two sections of double roller wash engines
The vacuum of motion is not less than -30kPa, and running speed is 1.0~2.0rpm.Scrub raffinate caused by two sections of double roller wash engines is made
One section of double roller wash engine is returned to for the cleaning solution of one section of double roller wash engine, the good slurry that two sections of double roller wash engines wash to obtain is delivered to
One section of oxygen delignification tower.
The good slurry that two sections of double roller wash engines wash to obtain carries out one section of oxygen delignification in one section of oxygen delignification tower.One section of oxygen
Flow of oxygen is 10~20kg/adt during delignification, and NaOH dosages are 15~26kg/adt, and the pH value of reaction system maintains
10.8~11.5, pressure maintains 600~800kPa, and temperature maintains 90~95 DEG C, and pulp concentration is arranged to 10~
12wt%, residence time of the wood pulp in one section of oxygen delignification tower are arranged to 20~25min.One section is obtained after one section of oxygen delignification
Oxygen delignification wood pulp.One section of oxygen delignification wood pulp is delivered to two sections of oxygen delignification towers and carries out two sections of oxygen delignifications.The de- wood of two sections of oxygen
Flow of oxygen is 5~10kg/adt during element, and NaOH dosages are 0~5kg/adt, the pH value of reaction system maintains 10~
11, pressure maintains 300~600kPa, and temperature maintains 98~110 DEG C, and pulp concentration is arranged to 10~12wt%, and wood pulp exists
Residence time in two sections of oxygen delignification towers is arranged to 40~45min.Two sections of oxygen delignification wood pulps are obtained after two sections of oxygen delignifications.
Two sections of oxygen delignification wood pulps are delivered to DD wash engines, are washed in DD wash engines.DD wash engines enter to starch concentration for 10~
11wt%, pulp concentration are 11~12wt%, and dilution gfactor is 2~2.5m3/ adt, it is 30~50kPa to enter to starch pressure, and operation turns
Speed is 1.0~2.0rpm.Obtained primary colors wood pulp is delivered to one section of bleaching tower after the washing of DD wash engines, caused by washing process
Scrub raffinate returns to two sections of double roller wash engines as the cleaning solution of two sections of double roller wash engines.
Primary colors wood pulp is bleached in one section of bleaching tower, and the bleaching agent used is chlorine dioxide, the dosage of bleaching agent for 9~
13kg/adt.One section of bleached wood pulp is obtained after one section of bleaching, the whiteness of one section of bleached wood pulp is 68%ISO.
One section of bleached wood pulp is delivered to delignification tower and carries out delignification, using NaOH and oxygen to the de- wood of one section of bleached wood pulp
Element, NaOH dosages are 12~13kg/adt, and flow of oxygen is less than 5kg/adt.Delignification wood pulp, delignification are obtained after delignification
The kappa value of wood pulp is 1.8~2.0, and whiteness is 75~80%ISO.
Is bleached in delignification wood pulp conveying second stage bleaching tower, the bleaching agent used is chlorine dioxide, the use of bleaching agent
Measure as 1.2kg/adt.Sulfate hardwood pulp is obtained after second stage bleaching, the whiteness of sulfate hardwood pulp is 80~87.5%
ISO。
Obtained sulfate hardwood pulp is delivered into paddle board to manufacture paper with pulp machine.Paddle board manufactures paper with pulp machine by one section of pressurized screen, two sections of pressures
Power sieve, one section of scummer, two sections of scummers, head box, wet end, twin wire press, heavy squeezer and drying baker composition.Sulfuric acid
Salt yearning between lovers wood pulp enters one section of pressurized screen after diluting first.The slurry ability of entering of one section of pressurized screen is 512adt/d, enters to starch concentration and is
2.8~3.2wt%, operating pressure 0.6MPa.The good slurry that one section of pressurized screen obtains enters head box, one section of pressure after dilution
The tailings of power sieve carries out two sections of pressurized screens after dilution.The slurry ability of entering of two sections of pressurized screens is 192adt/d, enters to starch concentration and is
2.0~2.3wt%, pulp concentration are 1.1~1.3wt%, and operating pressure is 0.15~0.35MPa, go out good slurry ability and are
152adt/d.The good slurry that two sections of pressurized screens obtain returns to one section of pressurized screen charging aperture, and the tailings of two sections of pressurized screens is after dilution
Into 8 parallel connections, one section of scummer.The slurry ability of always entering of one section of scummer is 48adt/d, and it is 1.1~1.3wt% to enter to starch concentration,
It is 37adt/d always to go out good slurry ability, and pulp concentration is 1~1.2wt%.The good slurry that one section of scummer obtains returns to two sections of pressurized screens
Charging aperture, the tailings of one section of slagging-off carry out 2 and the slagging-off of di- section after dilution.Two sections of scummers always to enter slurry ability preferred
For 12adt/d, it is 0.5wt% to enter to starch concentration.The good slurry that two sections of scummers obtain returns to one section of scummer charging aperture, two sections of slagging-off
Tailings outside arrange.
The good slurry that one section of pressurized screen obtains enters head box after dilution, the range of flow of head box for 9500~
24500L/min；Pulp concentration is 1.6~2.2wt%.Wood pulp is delivered to wet end by head box, wood pulp after net part forming successively
Into twin wire press and heavy squeezer, obtain mass dryness fraction and be more than 45% wet wood-pulp board.Wet wood-pulp board is delivered in drying baker
Dry, obtain the low whiteness sulfate hardwood pulpboard of high intensity.The operation speed of machine of drying baker is arranged to 60~140m/min.
The low whiteness sulfate hardwood pulpboard of above-mentioned high intensity obtains paddle board finished product by cutting plate, packing.Trimmed size is：
900~1270g/m of grammes per square metre2, single bag weight 250kg, 5 × 685 × 800mm of pulpboard finished size；Iron wire specification used in pack thread：Ф
2.18th, Ф 2.3mm, tensile strength are respectively 980-1200N/mm2、1000-1250N/mm2。
The yield of the low whiteness sulfate hardwood pulpboard of method production high intensity to being provided using the embodiment is counted
Calculate, be as a result 48.5~52%.The low whiteness hardwood pulpboard of high intensity of production is detected, as a result for：Pulpboard whiteness is
75~87.5%ISO, tensile index >=60.0N.m/g, tear index >=6.6mN.m2/ g, burst index >=in 4.0kPa.m2/
G, dichloromethane extract is below 0.6%, and dirt count is in 2.0mm2/m2Hereinafter, pulpboard grammes per square metre is 850~1270g/m2, pulpboard
Moisture is 9~13wt%.
Described above is only the preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (12)
1. a kind of preparation method of the low whiteness sulfate leaf wood pulpboard of high intensity, comprises the following steps：
A), broad-leaved wood chip is stocked up；
The broad-leaved wood chip be yearning between lovers wood chip, Eucalyptus piece and hardwood piece in one or more, the broad-leaved wood chip it is aqueous
Measure as 35~50wt%；
The compaction degree of wood chip after stock is 10~15%, and stack density is 160~230kg/m3；Bark in wood chip after stock
And/or accounting of the rotten material in total wood chip is less than or equal to 1wt%, accounting of wood chip of the thickness less than 3mm in total wood chip is less than
Equal to 1wt%, thickness is that accounting of the 3~7mm wood chip in total wood chip is less than or equal to 6wt%, and thickness is 8~12mm wood chip
Accounting in total wood chip is less than or equal to 8wt%, and thickness is that accounting of the 13~45mm wood chip in total wood chip is more than or equal to
55wt%, accounting of wood chip of the thickness more than 45mm in total wood chip are less than or equal to 2wt%；
B) wood chip after, stocking up carries out decatize in the decatize section of dipping tower first, and the dipping tower includes upper and lower double-layer structure,
Upper strata is decatize section, and lower floor is impregnation stage, and decatizing steam comes from upflowing vapor caused by impregnation stage maceration extract；Wood after decatize
Piece falls into impregnation stage, and wood chip is impregnated in impregnation stage, obtains impregnating wood chip；The temperature of the dipping is 80~110 DEG C；
Impregnate obtained dipping wood chip and enter the device for discharging full of current-carrying liquid, then enter high pressure feeder with current-carrying liquid, it is high
Pressure feeder will impregnate wood chip and current-carrying liquid is delivered to the separator of boiling tower；The boiling tower include separator, upper steaming stage,
Lower steaming stage and washing section, the separator, upper steaming stage, lower steaming stage and washing section along boiling tower vertical direction from top to bottom
Distribution；The separator is arranged at boiling top of tower；The upper steaming stage and lower steaming stage extract sieve plate by top and separated；Institute
State lower steaming stage and washing section and sieve plate separation is extracted by bottom；
After dipping wood chip and current-carrying liquid are delivered to separator, separator separates to dipping wood chip and current-carrying liquid, isolated
Current-carrying liquid return device for discharging, high pressure feeder or dipping tower impregnation stage；Isolated dipping wood chip enters upper steaming stage；
Impregnate wood chip and white liquor and mix one section of autoclaving of progress in upper steaming stage；The white liquor is NaOH and Na2S mixed solution；
The temperature of one section of autoclaving is 140~160 DEG C, and pressure is 0.5~0.7MPa, and liquid ratio is 3.5~7m3/bdt；Leaching
Stain wood chip obtains one section of boiling wood pulp after one section of autoclaving；One section of black digestion liquid is as leaching caused by one section of autoclaving
Stain liquid returns to dipping tower；
One section of boiling wood pulp enters lower steaming stage；One section of boiling wood pulp and white liquor mix in lower steaming stage carries out two sections of high pressures
Boiling；The temperature of two sections of autoclavings is 140~160 DEG C, and pressure is 0.5~0.7MPa, and liquid ratio is 3.5~7m3/
bdt；Steaming stage is slightly starched after carrying out two sections of autoclavings under one section of boiling wood pulp；
The thick slurry enters washing section, and enter boiling tower washing section from cleaning solution import after cleaning solution supercharging carries out adverse current to thick slurry
Washing, wood pulp obtain yellow slurry after washing；
The dilution gfactor of the washing is 1.5~2.5m3/adt；The kappa value of the yellow slurry is 16.0~20.0；
C1), the yellow slurry carries out one section of oxygen delignification after except section, screening and washing, obtains one section of oxygen delignification wood pulp；
The concentration of entering to starch of one section of oxygen delignification is 10~12wt%, and pulp concentration is 10~12wt%, the time is 20~
25min；Pressure is 600~800kPa, and temperature is 90~95 DEG C, and pH value is 10.8~11.5, and flow of oxygen is 10~20kg/
Adt, oxygen delignification agent dosage are 15~26kg/adt；
C2), one section of oxygen delignification wood pulp passes through two sections of oxygen delignifications, obtains two sections of oxygen delignification wood pulps；
The concentration of entering to starch of two sections of oxygen delignifications is 10~12wt%, and pulp concentration is 10~12wt%, the time is 40~
45min；Pressure is 300~600kPa, and temperature is 98~110 DEG C, and pH value is 10~11, and flow of oxygen is 5~10kg/adt, oxygen
Delignification agent dosage is 0~5kg/adt；
C3), two sections of oxygen delignification wood pulps obtain primary colors wood pulp by washing；
D1), the primary colors wood pulp obtains one section of bleached wood pulp by one section of bleaching；
The bleaching agent used in one section of bleaching process is chlorine dioxide, and the dosage of the bleaching agent is 9~13kg/adt；
D2 delignification wood pulp), is obtained to one section of bleached wood pulp delignification using oxygen and alkali；
The dosage of the oxygen is less than 5kg/adt, and the dosage of the alkali is 12~13kg/adt；
D3), the delignification wood pulp passes through second stage bleaching, obtains sulfate hardwood pulp；
The bleaching agent used during the second stage bleaching is chlorine dioxide, and the dosage of the bleaching agent is 1~2kg/adt；
E), the sulfate hardwood pulp obtains sulfate leaf wood pulpboard by manufacturing paper with pulp.
2. preparation method according to claim 1, it is characterised in that in step b), NaOH concentration is in the white liquor
125~145g/L, the sulphidity of the white liquor is 30~35%.
3. preparation method according to claim 1, it is characterised in that the delignification wood pulp is carried out after second stage bleaching
Tri-stage bleaching；
The bleaching agent used during the tri-stage bleaching is chlorine dioxide or hydrogen peroxide, and the dosage of the bleaching agent is less than
0.5kg/adt。
4. preparation method according to claim 1, it is characterised in that described except section specifically includes following steps：
The yellow slurry carries out one section except section, one section enter screening process except the good slurry that section obtains, and one section except the tailings of section is by dilute
Two sections are carried out after releasing except section, two sections enter screening process except the good slurry of section, two sections except the tailings of section is by dilution, cleaning and dehydration
After return to cooking process.
5. preparation method according to claim 4, it is characterised in that described one section except section enter to starch concentration for 3.0~
4.3wt%, it is 190~220kPa to enter to starch pressure, and ash-retention efficiency is 5~21%, except section pressure difference is 10~40kPa；Described two sections are removed
The concentration of entering to starch of section is 3.0~4.3wt%, and it is 190~220kPa to enter to starch pressure, and ash-retention efficiency is 5~24%, except section pressure difference is 10
~40kPa.
6. preparation method according to claim 1, it is characterised in that the screening specifically includes following steps：
Except the yellow slurry after section carries out one section of screening, one section is screened obtained good slurry and enters washing procedure, the tailings warp of one section of screening
Two sections of screenings are carried out after crossing dilution, the good slurry of two sections of screenings returns to one section of screening process, and the tailings of two sections of screenings is after dilution
Three sections of screenings are carried out, the good slurry of three sections of screenings returns to two sections of screening process, and the tailings of three sections of screenings carries out four sections after dilution
Screening, the good slurry of four sections of screenings return to three sections of screening process.
7. preparation method according to claim 6, it is characterised in that one section of screening enter to starch concentration for 2.0~
2.5wt%, it is 200~300kPa to enter to starch pressure, and screening pressure difference is 10~60kPa；Two sections of screenings enter to starch concentration for 1.6
~1.8wt%, it is 100~200kPa to enter to starch pressure, and screening pressure difference is 10~60kPa；Three sections of screenings are entered to starch concentration and are
0.8~1.0wt%, it is 100~200kPa to enter to starch pressure, and screening pressure difference is 10~60kPa；Four sections of screenings enter to starch concentration
For 0.8~1.0wt%, it is 100~200kPa to enter to starch pressure, and screening pressure difference is 10~60kPa.
8. preparation method according to claim 1, it is characterised in that the step e) specifically includes following steps：
The sulfate hardwood pulp by fine screen choosing, wood pulp streaming, shaping, squeezing and is dried successively, obtains sulfate broad-leaved
Wood-pulp board.
9. preparation method according to claim 8, it is characterised in that the fine screen choosing specifically includes following steps：
The sulfate hardwood pulp carries out one section of screening, and one section is screened obtained good slurry and send work into wood pulp stream after dilution
Sequence, one section is screened obtained tailings and two sections of screenings is carried out after dilution, and two sections are screened obtained good slurry and return to one section of screening work
Sequence, the tailings of two sections of screenings carry out one section after dilution and removed the gred, one section of obtained good slurry two sections of screening process of return that remove the gred, and one
The tailings that section slagging-off obtains carries out two sections of slagging-off after dilution, and two sections of obtained good slurries that remove the gred return to one section of slagging-off process.
10. preparation method according to claim 9, it is characterised in that one section of screening enter to starch concentration for 2.8~
3.2wt%, it is 0.4~0.8MPa to enter to starch pressure；The concentration of entering to starch of two sections of screenings are 2.0~2.3wt%, enter to starch pressure and are
0.15~0.35MPa；The concentration of entering to starch of one section of slagging-off is 1.1~1.3wt%；Two sections of slagging-off are entered to starch concentration and are
0.5wt%.
11. preparation method according to claim 8, it is characterised in that during the wood pulp stream is sent, the flow of wood pulp is
9500~24500L/min；Wood pulp concentration is 1.6~2.2wt%.
12. preparation method according to claim 8, it is characterised in that the squeezing specifically includes following steps：
Wood pulp after shaping obtains wet wood-pulp board successively by double net squeezings and heavy squeezing；
Press felt tension force is 4~8N/mm in double net expressing process；The tension force of press felt in the heavy expressing process
For 3~3.5N/mm.
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| CN201410542998.8A CN105568740B (en) | 2014-10-15 | 2014-10-15 | Low whiteness sulfate leaf wood pulpboard of a kind of high intensity and preparation method thereof |
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| CN109957981A (en) * | 2017-12-25 | 2019-07-02 | 福建省青山纸业股份有限公司 | A kind of high-strength high stretched paper bag process thoroughly of production |
| CN108978307A (en) * | 2018-08-28 | 2018-12-11 | 海南金海浆纸业有限公司 | A kind of high intensity leaf wood wood pulp and preparation method thereof |
| CN113089373B (en) * | 2021-02-08 | 2022-06-17 | 华邦古楼新材料有限公司 | Medical high-strength dialysis paper and preparation method thereof |
| CN115748290B (en) * | 2022-11-21 | 2023-08-22 | 亚太森博（山东）浆纸有限公司 | Low-whiteness and low-DCM extract bleached sulfate hardwood pulp and preparation method thereof, wood pulp board and preparation method thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101054777A (en) * | 2006-04-13 | 2007-10-17 | 安德里兹有限公司 | Hardwood alkaline pulping processes and systems |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101054777A (en) * | 2006-04-13 | 2007-10-17 | 安德里兹有限公司 | Hardwood alkaline pulping processes and systems |
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