CN103764904A

CN103764904A - Articles of manufacture made from pulp composition

Info

Publication number: CN103764904A
Application number: CN201280042556.6A
Authority: CN
Inventors: B·A·霍金斯; F·马丁
Original assignee: Cargill Inc
Current assignee: Cargill Inc
Priority date: 2011-08-30
Filing date: 2012-08-30
Publication date: 2014-04-30
Also published as: US20140205777A1; ZA201401309B; US20150041087A1; AR087707A1; EP2751332A1; WO2013033405A1; CA2846861A1; CO6900132A2; EP2751332A4; KR20140068093A; BR112014004226A2; MX2014002359A; AU2012301819A1

Abstract

One aspect of the invention relates to an article of manufacture made from a pulp composition comprising an ARF pulp. In one embodiment, the pulp composition made from agricultural renewable fibers (ARF) having low Kappa number with unexpected quality sufficient for papermaking (e.g., high strength parameters and high freeness). In another embodiment, the ARF pulp has ISO brightness of 60% or higher, and unexpected quality sufficient for papermaking (e.g. high strength parameters and high freeness). In another embodiment, the ARF pulp is made from a pulping process comprising using a high concentration of anthraquinone (AQ).

Description

The goods of being prepared by pulp composition

Technical field

The disclosure relates to the goods of being prepared by pulp composition.

Background technology

Paper pulp is the lignocellulosic fibre material making with chemistry or mechanical system defibre cellulose fiber by from timber or non-wood-fiber source.

" slurrying " is often referred to body fibre source material is reduced to its component fibre.Timber and other plant material for the preparation of paper pulp contain three kinds of key components (except water) conventionally: cellulose fibre (papermaking is required), lignin (three-dimensional polymer that cellulose fibre is bonded together) and hemicellulose (shorter branching carbohydrate polymer).The object of slurrying is that the body construction of fibre source (it is spile, cane or other plant part) is resolved into composition fiber.

Chemical pulping realizes this in the following way: lignin degradation is become to little water soluble molecules, and this little water soluble molecules can wash away and not make cellulose or hemicellulose fibers depolymerization from cellulose or hemicellulose fibers.Make cellulose depolymerization weaken fiber, and reduce the intensity of the paper pulp obtaining.Although the lignin in paper pulp can improve intensity, the paper pulp with high delignification's degree can make bleaching process easy.

Conventionally, in the situation that not using multiple delignifications process and/or without unacceptably destroying or weaken in the cellulosic situation in paper pulp, the paper pulp that existing paper pulp method does not provide κ (Kappa) enough to reduce.Therefore, need a kind of improved pulping process, it can obtain the paper pulp with desirable characteristics, and eliminates the many steps in step required in current technology simultaneously.

In addition, agriculture renewable fiber (ARF) is to use the one eco-friendly replacement scheme of timber as fibre source.ARF represents the promising source economically of non-wood-fiber.But due to the frangible character of agricultural residue, available ARF paper pulp for example, does not have enough intensity for many industrial uses (manufacture printing and write a grade paper) in the market.Therefore, need to be for the preparation of the consistent ARF paper pulp of the high-quality of goods, its alternative paper pulp being made by lumber fibre.

Summary of the invention

An aspect of the present disclosure relates to a kind of goods of being prepared by the pulp composition that comprises ARF paper pulp.

In one embodiment, described ARF paper pulp has approximately 15 or lower not bleaching κ number (Kappa number) and the intensive parameter that is enough to papermaking.

In another embodiment, ARF paper pulp is made by such pulping process, this pulping process comprises being enough to form the first mixture that boiling (cook) time of the first paper pulp and conditions of cooking boiling comprise fiber, water, alkali and delignification and selectively improve chemicals, and described the first paper pulp has approximately 15 or lower required κ number and the intensive parameter that is enough to papermaking.

Accompanying drawing explanation

Fig. 1: for the high H-factor and low H-factor treatment, the impact of the κ number of anthraquinone (AQ) concentration of processing for boiling on obtained paper pulp.

Fig. 2: according to the flow chart of the pulping process of an embodiment of the present disclosure.

The specific embodiment

An aspect of the present disclosure relates to the goods of being prepared by the pulp composition that comprises ARF paper pulp.

The example of the goods of being prepared by the pulp composition that comprises ARF paper pulp includes but not limited to thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper (as OGR, bleaching wrapping paper (bleached packaging grades), flexible package punch paper), more uncommon paper (as wet strength paper and release liner), regeneration liner board and molded packaging product.

ARF paper pulp can be paper pulp bleaching or unbleached.The example of the goods of being prepared by the pulp composition of the ARF paper pulp that comprises bleaching includes but not limited to thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper (as grease resistance paper (oil and grease resistant " OGR ") bleaching wrapping paper, flexible package punch paper) and more uncommon paper (as wet strength paper and release liner).The example of the goods of being prepared by the pulp composition that comprises unbleached ARF paper pulp include but not limited to regenerate liner board and molded packaging product.In certain embodiments, use bleaching or unbleached ARF paper pulp can improve the performance of goods.

ARF comprises the fiber available from agricultural production.The example of ARF includes but not limited to bagasse, wheat stalk, rice straw, maize straw (stem, leaf and shell), soybean residue, coconut tissue, cotton stalk, certain herbaceous plants with big flowers basket, mestha, industrial hemp, seed flax stalk, textiles flax stalk, sisal hemp, late aloe (hesperaloe), rye grass and their mixture.In one embodiment, ARF is bagasse or maize straw.

ARF paper pulp disclosed herein demonstrates excellent bonding characteristic.Although the fiber in ARF paper pulp is generally staple fibre, but due to excellent bonding characteristic, this fiber shows more as long fiber unexpectedly, demonstrate the physical size that is similar to hardwood fiber, and there is the intensity that makes their parts (if not completely) substitute northern bleached softwood kraft to starch (NBSK) etc.These bonding characteristics produce outstanding final paper sheets intensity to meet high request customer specification of today.This sheet strength realizes by a part for the required common refining energy of lumber fibre, and this is tissue applications and need to refines wood pulp and produce the remarkable cost savings of other application of intensity.In certain embodiments, the fibre count of every milligram is 19,000.

The premium grade toilet paper that meets North America high-quality specification is replaced minimum NBSK and and carries out anyly further making with ARF paper pulp by direct.

In one embodiment, described ARF paper pulp has approximately 15 or the lower intensive parameter of not bleaching κ number and being enough to papermaking.

κ number has reflected the degree of the delignification of hardness, bleaching property or paper pulp.Conventionally, κ number be approximately 5 or lower paper pulp can or bleach without chlorine compound (totally chlorine free (TCF) technology) in the situation that by chlorine dioxide (element-free chlorine (ECF) technology), to provide, there is required whiteness (be for example less than 50% ISO whiteness, approximately 60% or higher, approximately 70% or higher, approximately 80% or higher, approximately 84% or higher, approximately 88% or higher, approximately 80 to approximately 90% or approximately 90% or higher ISO whiteness).Conventionally, need cost to exceed that a slurrying step (being sometimes referred to as boiling or delignification) reduces κ number and the intensive parameter that simultaneously keeps paper pulp.The paper pulp with higher κ number will make ECF or TCF bleaching difficulty, thereby need xylon and/or ozone, and/or much more peroxide.Or the paper pulp with higher κ number can be by chlorine bleach.Therefore the ARF paper pulp that, has enough low κ number and a sufficiently high intensive parameter is that this area is required.

This area has been developed many methods of measuring delignification's degree, but great majority are the modification of permanganate test.Equivalent permanganate test can provide permanganate or " κ number ", its cubic centimetre number that is ten/monovalent (0.1N) liquor potassic permanganate of being consumed by the paper pulp of 1 gram of oven drying under specified requirements.For example, it can be measured by TAPPI standard testing T-236.The acceptable κ scope of counting will depend on the desired use of paper pulp and difference (for example, the κ number of brown wood board requires to can be approximately 50 to approximately 90, and the requirement of blank sheet of paper slurry can be less than 5).

Breaking length (tensile), tear index (tear index) and burst index (burst index) are the example that is ready to use in the intensive parameter of the paper pulp of manufacturing goods (for example paper stock or paper product).Conventionally, need higher pulp strength parameter that the higher-strength of the goods that made by it is provided.Than for example, paper pulp available from non-wood-fiber (ARF, as bagasse), available from the paper pulp of lumber fibre, conventionally show and there is better intensive parameter.For example, but some (breaking lengths) in the intensive parameter of pulp composition disclosed herein are similar to or those (referring to for example embodiment 9, tables 2) of the paper pulp that is better than being made by timber unexpectedly.

The example that is enough to the intensive parameter of the paper pulp of papermaking includes but not limited at least about the breaking length of 5.50km, at least about 6.00mN.m ²the tear index of/g, at least about 3.00kPa.m ²the burst index of/g and their combination.

In certain embodiments, pulp composition have approximately 15 or lower, approximately 10 or lower or approximately 5 or lower κ number.

In certain embodiments, pulp composition also has high freedom (freeness).

Term used herein " freedom " refers to " paper pulp freedom ", refer to the drainage rate of paper pulp, or paper pulp is discharged the degrees of freedom of its water.The importance of freedom in papermaking is, if freedom is too low, can not on paper machine, removes enough water and obtain good sheet structure and intensity.Conventionally, mechanical pulp is because the harshness effect that is applied to raw material has low freedom, and this harshness effect produces the fiber fines (fines) and the particle that stop up drainage paper washer.Use many chemical pulping processing of full stem stalk (bast and core) non-wood-fiber source material to there is the problem of the poor freedom causing due to the characteristic of core.

Some embodiments do not suffer the freedom problem of prior art processing.In fact, ARF paper pulp more disclosed herein have high freedom.This freedom is more much higher than conventional non-wood pulp, thus the problem of the platform capacity (table capacity) on paper machine while having eliminated about the alternative paper pulp based on timber.As used herein, term " high freedom " is intended to refer at least about 400mL CSF and above freedom.

In certain embodiments, ARF paper pulp disclosed herein has at least about 400,425,450,475,500,525 or the freedom of 550mL CSF.

In certain embodiments, ARF paper pulp has approximately 60% or higher ISO whiteness and the intensive parameter that is enough to papermaking.

There is the method for many measurement pulp brightness.This parameter is generally measuring of reflectivity, and its value is typically expressed as the percentage of certain scale.Herein, use International Standards Organization (International Standards Organization, ISO) whiteness test.In certain embodiments, ARF paper pulp of the present disclosure has the ISO whiteness that is less than 50%.In certain embodiments, ARF paper pulp of the present disclosure should have approximately 60% or higher ISO whiteness (be suitable for manufacturing printing and write a grade paper).

In certain embodiments, ARF paper pulp have approximately 60% or higher, approximately 70% or higher, approximately 80% or higher, approximately 84% or higher, approximately 88% or higher, approximately 80 to approximately 90% or approximately 90% or higher ISO whiteness.

In another embodiment, ARF paper pulp is made by such pulping process, this pulping process comprises being enough to forming the first mixture that the digestion time of the first paper pulp and conditions of cooking boiling comprise ARF fiber, water, alkali and delignification and selectively improve chemicals, and described the first paper pulp has approximately 15 or lower required κ number and the intensive parameter that is enough to papermaking.Boiling step can comprise that single boiling step is to obtain required paper pulp.

In one embodiment, in described pulping process, fiber used is ARF.In another embodiment, ARF is bagasse or maize straw.In another embodiment, in described pulping process, fiber used is lumber fibre, for example hardwood fiber or cork fibrous.

The example that is enough to the intensive parameter of papermaking includes but not limited at least about the breaking length of 5.50km, at least about 6.00mN.m ²the tear index of/g, at least about 3.00kPa.m ²the burst index of/g, wherein before boiling, raw material has approximately 60 or higher κ number, and their combination.

The concentration of the alkali in described the first mixture can be approximately 10 % by weight to 30 % by weight, extremely extremely extremely approximately 22.5 % by weight, approximately 20 % by weight, approximately 21 % by weight, approximately 22 % by weight, approximately 22.5 % by weight, approximately 24 % by weight or approximately 27 % by weight of approximately 22 % by weight, approximately 20 % by weight of approximately 25 % by weight, approximately 20 % by weight of approximately 15 % by weight of fiber feed (oven drying).The example of alkali is not limited to NaOH or potassium hydroxide, and it also can contain sulfur chemistry.As used herein, " OD " and " O.D. " is oven drying.Other examples of suitable alkali additive comprise ammonia and monoethanolamine or derivatives thereof.

The example that chemicals selectively improves in delignification includes but not limited to anthraquinone (AQ) or derivatives thereof.Approximately 0.2 % by weight that in the first mixture, the concentration of AQ or derivatives thereof can be OD fiber feed is to approximately 1.0 % by weight, at least about 0.1 % by weight, at least about 0.17 % by weight, at least about 0.2 % by weight, at least about 0.25 % by weight, at least about 0.27 % by weight, at least about 0.3 % by weight, at least about 0.35 % by weight, at least about 0.4 % by weight, at least about 0.45 % by weight, at least about 0.5 % by weight, at least about 0.55 % by weight, at least about 0.6 % by weight, at least about 0.65 % by weight, at least about 0.7 % by weight, at least about 0.75 % by weight, at least about 0.8 % by weight, or at least about 0.85 % by weight.

Liquid/the dried fibres of the first mixture is the total amount of liquid than the fiber of bone dry than (L/W), for example, be applied to the liquid weight of boiling vessel (digester) charging of the oven drying of Unit Weight.It comprises all liq that boiling relates to, and can be approximately 4,5,6,7,8 or 9 to approximately 10, approximately 7 or approximately 8.

The term " denseness " that is used in reference to " reaction denseness ", " mixture denseness " and " pulp thickness " herein represents percentage (%) solid content of reactant mixture, mixture or pulp, the % by weight of for example fiber in pulp/water slurry material (being generally paper pulp but not crude fibre).

Conditions of cooking can be under boiling temperature and cooking pressure.Boiling temperature can be approximately 120 ℃ to approximately 200 ℃, approximately 150 ℃ to approximately 190 ℃ or approximately 165 ℃ to approximately 185 ℃, approximately 175 ℃, lower than approximately 175 ℃, not higher than 175 ℃, approximately 165 ℃, lower than approximately 165 ℃ or not higher than 165 ℃.Cooking pressure can be about 60psi/g to about 150psi/g, 120psi/g to about 150psi/g or extremely about 140psig of about 130psig.

The digestion time that is enough to form the first paper pulp under conditions of cooking depends on condition, and under maximum temperature of cooking, can be approximately 15 minutes to approximately 180 minutes, approximately 15 minutes to approximately 120 minutes, approximately 15 minutes to approximately 90 minutes, approximately 30 to approximately 90 minutes, approximately 30 to approximately 60 minutes, approximately 53 minutes, approximately 50 minutes, approximately 40 minutes, approximately 35 minutes or approximately 34 minutes.

In certain embodiments, the first mixture is heated to temperature requiredly in the first digestion time process from lower temperature, and reaches the second digestion time in temperature required lower maintenance.For example, temperature requiredly can be approximately 90 ℃ to approximately 200 ℃, approximately 120 ℃ to approximately 200 ℃, approximately 150 ℃ to approximately 190 ℃ or approximately 165 ℃ to approximately 185 ℃, approximately 185 ℃, approximately 175 ℃ or approximately 165 ℃.Lower temperature can be about room temperature, approximately 90 ℃, approximately 120 ℃, approximately 150 ℃ or approximately 165 ℃.The first digestion time can be approximately 1 minute to approximately 120 minutes, approximately 1 minute to approximately 90 minutes, approximately 1 minute to approximately 60 minutes, approximately 5 minutes to approximately 120 minutes, approximately 5 minutes to approximately 90 minutes, approximately 5 minutes to approximately 60 minutes or approximately 60 minutes.The second digestion time can be approximately 15 minutes to approximately 180 minutes, approximately 15 minutes to approximately 120 minutes, approximately 15 minutes to approximately 90 minutes, approximately 30 to approximately 90 minutes, approximately 30 to approximately 60 minutes, approximately 53 minutes, approximately 50 minutes, approximately 40 minutes, approximately 35 minutes or approximately 34 minutes.In certain embodiments, conditions of cooking be at about 130psi/g under the cooking pressure of about 140psi/g, and temperature required be approximately 175 ℃.Lower temperature is approximately 90 ℃, and the first digestion time is 60 minutes, and the second digestion time is approximately 40 minutes.

In certain embodiments, boiling temperature is approximately 120 ℃ to approximately 200 ℃, and digestion time is approximately 15,20 or 30 to approximately 45,50,60,70,80 or 90 minutes.In certain embodiments, boiling temperature is approximately 150 ℃ to approximately 190 ℃, and digestion time is approximately 30 to 60 minutes.In certain embodiments, boiling temperature is approximately 165 ℃ to approximately 185 ℃, and digestion time is approximately 35 to approximately 45 minutes.

In certain embodiments, the temperature of the first mixture is reduced to the boiling vessel simulation under temperature required.For example, second mixture with every kind of composition of the first mixture except ARF can make under temperature required, then ARF is added in the second mixture to form the first mixture.Digestion time under temperature required can be approximately 15 minutes to approximately 180 minutes, approximately 15 minutes to approximately 120 minutes, approximately 15 minutes to approximately 90 minutes, approximately 30 to approximately 90 minutes, approximately 30 to approximately 60 minutes, approximately 53 minutes, approximately 50 minutes, approximately 40 minutes, approximately 35 minutes or approximately 34 minutes.

In the prior art, the paper pulp being made by the first boiling step has higher κ number conventionally, or has damaged or destroyed cellulosic required character.For example, the paper pulp being made by bagasse known in the art has approximately 20 or higher κ number.This paper pulp further delignification for example, to reduce κ number (oxygen delignification and/or ozone treatment), and/or by chlorine bleach.This delignification and/or chlorine are processed intensity and other parameters of the paper pulp that likely infringement obtains and are increased process cost.

The κ number of the first paper pulp be approximately 5 or lower, approximately 7 or lower, approximately 10 or lower or approximately 15 or lower.κ number be 5 or the first lower paper pulp can be bleached by TCF or ECF, with obtain be suitable for preparation have required whiteness (be for example less than 50%, approximately 60% or higher, approximately 70% or higher, approximately 80% or higher, approximately 84% or higher, approximately 88% or higher, approximately 80 to approximately 90% or approximately 90% or higher ISO whiteness) the paper pulp of paper.

In certain embodiments, the κ number of the first paper pulp along be applied to boiling processing AQ amount increase and reduce (Fig. 1).

The relative velocity of H-factor representation lignin dissolution.It depends on digestion time and temperature.Due to the temperature dependency of delignification, the dependence of H-factor pair temperature is extremely strong.Even the difference in the several years of boiling temperature also can produce the significant difference of pulp quality.The H-factor is limited, make to be equal to for 1 hour in 100 ℃ the H-factor 1.Conventionally, boiling process in the higher H-factor the higher κ number of the first paper pulp is more likely provided.

The H-factor can be by

H = {&Integral;}_{0}^{t} e^{(43,2 - \frac{16115}{T})} dt

Calculate, wherein t is the time, and T is temperature (degree Kelvin).

In certain embodiments, slurrying process approximately 20 or higher, approximately 50 or higher, approximately 100 or higher, approximately 200 or higher, approximately 300 or higher, approximately 400 or higher, approximately 1000 or higher, approximately 200, approximately 300, approximately 400, approximately 1000, approximately 1100 or higher, approximately 1400 or higher, approximately 1700 or higher, approximately 2000 or higher, approximately 2500 or higher, approximately 3000 or higher, approximately 2000 to approximately 3000 the H-factor under carry out.

In another embodiment, conditions of cooking is pressure cooking condition.Pulping process before being also included in the first paper pulp being discharged from pressure cooking condition is cooled to the first paper pulp lower than its boiling point.Be released into atmospheric pressure and still higher than the cellulose fibre in the alkaline matrix of the boiling point of rare black liquor (weak black liquor), will suffer damage.Damage may be serious.For fear of this damage, before discharging the first paper pulp from pressure cooking condition, the first paper pulp can be cooled in the temperature range of approximately 70 to approximately 95 ℃.In certain embodiments, before discharging the first paper pulp from pressure cooking condition, will spurt pipeline (blowline) and be cooled to lower than its boiling point.In certain embodiments, before discharging the first paper pulp from pressure cooking condition, dilute the first paper pulp so that its temperature is reduced to lower than its boiling point with cooling washings.

In another embodiment, pulping process also comprises cleaning.In cleaning, for example, the paper pulp (the first paper pulp, the paper pulp through bleaching and/or for example, paper pulp available from each stage of bleaching (chelating, the bleaching of oxygen enrichment alkaline peroxide)) obtaining the fiber before fiber being added into the first mixture, from the first mixture or after one or more steps of slurrying processing, remove undesirable material (for example undesirable mineral material, undesirable cellulosic material and burning or partially combusted fiber).

The example of undesirable mineral material includes but not limited to rock, sandstone, rust, dirt, the metal being mingled with, refuse and superfine (silicate) particle.These particles can wear equipment, reduce whiteness, affect freedom and facilitate high content of ashes.Can be from being added into the fiber before the first mixture, from the first mixture and/or from paper pulp, remove undesirable mineral material.

The example of undesirable cellulosic material includes but not limited to pith (parenchyma cell and other non-fibrocytes).Undesirable cellulosic material has few structure paper manufacturing value, but their eshaustibility chemicals stop up sheet material.Undesirable cellulosic material may be difficult to remove from paper pulp.Therefore, need to from fiber and/or from the first mixture, remove as much as possible undesirable cellulosic material.

The example of burning or partially combusted bagasse particle includes but not limited to carbon and coke.If carbon, coke and partially combusted bagasse particle are of a size of microcosmic, they can reduce final pulp brightness.If these particles are larger, they will be shown as dust.Hope from being added into the fiber before the first mixture, from the first mixture and/or from paper pulp, remove these particles.

Coarse-fibred cleaning can comprise single or multiple cleaning stages.For example, in the first cleaning stage, soft stirring is applied to crude fibre, to provide, shears and discharge some in the pith being attached on fiber.

In the second cleaning stage, by centrifugal cleaner, from crude fibre, remove rock and grit.

In the 3rd cleaning stage, with the first clean denseness in water, mix crude fibre and continue the first cleaning time, to form the first cleaning mixt, then with the first clean sieve, filter.Optionally soft stirring is applied to blend step.The first clean denseness can be low to medium, and for example approximately 0.5 % by weight is to approximately 10 % by weight, approximately 1 % by weight or approximately 2 % by weight.Water can be at the temperature of approximately 20 ℃ to approximately 100 ℃, approximately 80 ℃ to approximately 100 ℃ or approximately 60 ℃.The first cleaning time can be 1 minute to approximately 1 hour or approximately 10 minutes.Optionally, can accelerate to soak with a small amount of washing agent.The first clean sieve can be scalping (about 0.5cm or larger).The first cleaning mixt can be toppled over by described sieve.Conventionally remove the fiber that is retained in sieve top, to prevent from forming thick-layer (thickness is as about 1cm or less).High a lot of denseness is with much thick that layer can stop separation.

For the fiber purification step of the first paper pulp, relate to and be called the chemicals of processing separation consumes and the non-paper pulp material of dissolving of washing.Washing is also for representing to use surfactant, and then water rinses, thereby removes macroscopic little undesirable particle and those particles that are of a size of microcosmic.Clean relate to Fen Li required fiber from unexpected fiber and other materials (system that is called sieve and cleaner as sandstone, coke or use slurrying step not completely the material of processing).The example of first kind treatment facility is rotary-drum vacuum washer, wash press and diffusion washing unit.The example of Equations of The Second Kind treatment facility is pressure-sensitive paper pulp screen and centrifugal cleaner.

In addition, for example, can be by initiatively rinsing paper pulp and remove undesirable cellulose and/or mineral material from paper pulp by clean water.Before rinsing optionally diluted pulp for example, to form lower denseness (approximately 1.0%).Rinsing step can carry out in the case with sieve screen apertures base plate, does not wherein allow the pulp mat forming on mesh to gather.Once you begin on mesh, form the paper pulp of one deck through washing, just shifted out and preserve.

Diffuser is that the multistage diffusion unit that operates under conditions of cooking is to improve detersive efficiency.In certain embodiments, diffusion unit has 5 or more washing stage.Optionally, working pressure diffuser after each washing step, to allow energy to reduce by never cooling this processing.

In order to obtain good separation in cleaning course, preferably remain on the upper thinner pulp mat forming of sieve.In certain embodiments, before sieve shifts out pulp mat, pulp mat has the thickness that is less than 1 inch or is less than 0.5 inch.The size in the hole on sieve can be approximately 1/8 inch or approximately 3/8 inch.

Optionally, in separation process, can vibrating screen.For example (but being not restricted to), vibration can be approximately 0.1 to approximately 2 inch, approximately 0.1 to approximately 1 inch, approximately 0.1 to approximately 0.5 inch, approximately 0.25 to approximately 0.5 inch.

In certain embodiments, before digestion crude fibre, by dropping to, on the sieve for separating of undesirable material, clean the first mixture or paper pulp.Crude fibre, the first mixture or paper pulp are with the angle drippage except 90 °, to prevent obstruction.Described angle can be approximately 45 ° or larger.Wish to have and consistent topple over speed with to sieve feed, thereby on whole sieve surface, keep more smooth with consistent distribution of material.

In certain embodiments, by vertical type hammer grinder or by drum sieve, from crude fibre, the first mixture or paper pulp, separate undesirable material.This is that thick bagasse is prepared for being loaded into the first procedure of processing of paper pulp grinding machine, and is called semidry method except marrow.

In another embodiment, pulping process also comprises that bleaching the first paper pulp is to provide the paper pulp of bleaching.In certain embodiments, pulp composition have approximately 60% or higher, approximately 70% or higher, approximately 80% or higher, approximately 84% or higher, approximately 88% or higher, approximately 80 to approximately 90%, or approximately 90% or higher ISO whiteness.

Blanching step can relate to chlorine, chlorine dioxide (ECF technology) or without chlorine compound (TCF technology).Blanching step comprises one or more stages.Each stage can comprise or not comprise bleaching agent.Each stage can be carried out independently or be carried out with another stage combination simultaneously.Optionally, after each stage, carry out cleaning (for example, via wash press, diffuser or diffusion sheet washer).For example, in the C stage, apply chlorine.In PO, Ep, P, P1 or P2 stage, apply hydrogen peroxide.In the E stage, the extraction of NaOH is used in application.In D, D1 or D100 stage, apply chlorine dioxide.In the Eop stage, apply NaOH, and add hydrogen peroxide and a small amount of oxygen.In the O stage, apply oxygen.In the Q stage, apply chelating agent to remove metal.In the PO stage, apply alkaline peroxide and oxygen to improve peroxide efficiency simultaneously.

Optionally, after completing, each stage of reaction washs.

Chelating is for the protection of the step of peroxide that is used as bleaching chemical in next stage.The example of chelating agent includes but not limited to ethylenediamine tetra-acetic acid (EDTA), DTPA (DTPA) and diethylenetriamine pentamethylenophosphonic acid (DTPMPA).In certain embodiments, the pH of pending paper pulp is adjusted to 4.0 to remove calcium and other metals.At 80 ℃ or higher chelating temperature for example, for example, with chelating agent (EDTA, DTPA) and sour (H ₂sO ₄) pulp treatment reaches 10 minutes to 30 minutes or the longer chelating time.When using DTPMPA, do not need pH to regulate.The target of all chelating agents is mainly Mn, and it causes the catalysis loss of hydrogen peroxide.Chemicals adds via high shear chemical mixer or any other suitable apparatus/method known in the art.In certain embodiments, before chelation treatment, by paper pulp be adjusted to approximately 5 to approximately 30%, approximately 10 to approximately 30%, approximately 15 to approximately 20%, approximately 10%, approximately 15% or approximately 20% denseness.In certain embodiments, before carrying out next stage, washing is available from the paper pulp of chelation stage.Washing can be carried out in wash press, and this wash press compacting then dilution is also suppressed paper pulp again for washing.Washing can be undertaken by additive method known in the art and equipment.

In certain embodiments, if for example the first paper pulp has the κ number higher than approximately 5～15, can first chlorine bleach method be applied to the first paper pulp k value is reduced to lower than about 5～15(C stage), then (if needs) alternative hypochlorite of hydrogen peroxide that harmfulness is lower.For example, C/Eop/PO or C/Ep/PO bleaching order can be applicable to replace the blanching step of prior art order C/E/H or C/EOP/H or C/EP/H.

In certain embodiments, the first paper pulp has approximately 5 – 15 or lower κ number, and ECF or TCF method are suitable for.

ECF method comprises the one or more stages that are selected from D, D100, D1, Ep, D, PO and Eop.ECF means to use at least some chlorine dioxide." E " expression " element " in ECF, means and does not use chlorine itself.These have replaced the older order that is generally C/E/H or its variant.

TCF method generally includes the one or more stages that are selected from Q, P, PO and O." T " in TCF represents altogether.TCF order also can comprise multiple other chemistry, as ozone " Z ", peracetic acid, Caro's acid, sodium hydrogensulfite etc.

In certain embodiments, TCF method comprises the Q stage, is multiple peroxides in atmosphere stages or single atmosphere P stage and PO stage afterwards afterwards.In the Q stage, the chelating agent of chelating use 0.5% and 0.4% H ₂sO ₄at 80 ℃, carry out as mentioned above 30 minutes, if use DTPMPA, do not use H ₂sO ₄but apply identical condition.In the PO stage, bleaching completes in single utmost point alkaline peroxide bleaching stage, and this stage is rich in oxygen to improve peroxide efficiency.Great majority or even all whiteness gains can realize in the P/PO stage.In certain embodiments, at the temperature of approximately 120 ℃, paper pulp (for example approximately 5 to approximately 30%, approximately 10 to approximately 30%, approximately 15 to approximately 20%, approximately 10%, approximately 15% or approximately 20%) and steam, caustic alkali (NaOH, approximately 2.6 % by weight of dry pulp), oxygen (pressure of 60psi/g), hydrogen peroxide (approximately 6.0 % by weight of dry pulp are to approximately 9.0 % by weight, approximately 6.0 % by weight or approximately 7.0 % by weight), sodium metasilicate (approximately 4.0 % by weight of dry pulp), magnesium sulfate (magsulfate) (approximately 0.3 % by weight of dry pulp) are mixed approximately 120 minutes.This stage can be in high shear paper pulp/steam/chemical mixture, or carries out in any other suitable apparatus/method known in the art.The ISO whiteness of paper pulp of bleaching be approximately 60% or higher, approximately 70% or higher, approximately 80% or higher, approximately 84% or higher, approximately 88% or higher, approximately 80 to approximately 90% or approximately 90% or higher.Productive rate can be approximately 90% or higher, feed fiber of feed fiber approximately 94% or higher, feed fiber approximately 95% or higher.

In certain embodiments, TCF method has Q/P1/Q/P2 and Q/P1/PO and Q/P1/Q/PO, and the order of Q/PO, and wherein Q stage and P and PO stage are same as described above.At P with in the PO stage, at the temperature of approximately 80 ℃, use caustic alkali (NaOH, approximately 0.7 % by weight of dry pulp), hydrogen peroxide (approximately 1.0 % by weight of dry pulp), sodium metasilicate (approximately 4.0 % by weight of dry pulp), magnesium sulfate (approximately 0.3 % by weight of dry pulp) process paper pulp available from a Q stage (optionally through washing, denseness is approximately 5 to approximately 30%, approximately 10 to approximately 30%, approximately 15 to approximately 20%, approximately 10%, approximately 15%, or approximately 20%) approximately 30 minutes, final pH was approximately 10.6.The ISO whiteness of the paper pulp of bleaching is approximately 60% or higher.Then the paper pulp obtaining by another Q stage and foregoing P2/PO phase process.

In another embodiment, pulping process carries out as shown in the flow chart of Fig. 2.In bagasse washing step, plain boiled water for Bagasse Material is (available from the fresh water (FW) of paper manufacturing systems, as the fresh water (FW) of the difference washing available from as shown in the figure) washing, so that bagasse (it is for the boiling of boiling vessel step) and the bagasse washings effluent (it is directed to drainpipe) through washing to be provided, as mentioned above.After digestion, gained slurrying mixture is sent to the washing by different washing methodss as above.Obtained washings effluent is sent to further processing.By carrying out as mentioned above chelating through the bagasse of washing, wash as mentioned above, then in blanching step, bleach.Although only show a bleaching frame in figure, can introduce single or multiple bleaching stages, as mentioned above.In certain embodiments, the washing between step can be optional.After bleached pulp, wash, clean and be dried and pull out paper pulp.

embodiment

embodiment 1. is coarse-fibred clean

Bagasse is as coarse-fibred example.First under 0.5% to 2.0% denseness, under appropriateness stirs, with the clean water of heat (water temperature more than room temperature, approximately 40 ℃ or 60 ℃) hydration bagasse 10 minutes.In Trammel sieve, separate pith and sandstone from fiber, Trammel sieve is rotary drum, its lifting and drippage material, and " hole receives water and pith until 1/2 to pass through the hole of the 1/8th inch.Collect the material intercepting and remove to prevent from gathering from sieve, and disposing, dry before being added in slurrying processing.Depend on the quality of Bagasse Material, washing productive rate is approximately 80% or higher or approximately 85.9%.

the soda AQ slurrying of embodiment 2. bagasses

Under the maximum temperature of approximately 175 ℃, take liquid/dried fibres than 7(denseness as approximately 12.5%), by 0.3 % by weight of the dry weight of NaOH (20 % by weight of OD bagasse) and AQ(OD bagasse) process OD bagasse (clean as described in Example 1, κ number is 89) 35 or 40 minutes.The time that reaches maximum temperature is 60 minutes.

The target H-factor is 1060, is low to moderate 20, high to 3000, and the temperature of pulping reaction is 120 ℃ to 185 ℃.The κ number of the paper pulp obtaining is 4.5.

the washing of embodiment 3. paper pulp

Paper pulp available from embodiment 2 is washed in pressure diffusion sheet washer, and described pressure diffusion sheet washer is specifically designed to and uses individual unit to complete all washings and in paper pulp, do not introduce undesirable change.Select the temperature of washings paper pulp temperature is cooled to approximately 100 ℃, 95 ℃, 90 ℃, 85 ℃, 80 ℃ or lower.Output forwards blanching step to, and is cooled to 100 ℃ or lower to prevent flash distillation.

the chelation stage (Q stage) of embodiment 4. paper pulp

Pass through H ₂sO ₄(approximately 0.4 % by weight of the dry weight of paper pulp), by the denseness and the pH4 that are adjusted to 15% available from the paper pulp of embodiment 3, then uses 0.5 % by weight of the dry weight of DTPA(paper pulp at 80 ℃) process 10 minutes.Continuing in wash press, to wash obtained paper pulp before next stage.

the alkaline peroxide bleaching (P2/PO stage) of embodiment 5. paper pulp

The paper pulp through washing available from embodiment 4 is adjusted to 15% denseness, and proceeds to the P2/PO stage.In high shear paper pulp/steam/chemical mixture, at the temperature of approximately 120 ℃, paper pulp (15% denseness) and steam, caustic alkali (NaOH, 2.6 % by weight of dry pulp), oxygen (pressure of 60psig), hydrogen peroxide (7.0 % by weight of dry pulp), sodium metasilicate (approximately 4.0 % by weight of dry pulp), magnesium sulfate (approximately 0.3 % by weight of dry pulp) are mixed approximately 120 minutes.The ISO whiteness of the paper pulp of bleaching is 86% or higher, and is at most 89.2.Productive rate be feed fiber approximately 94% or higher.Final pH is 10.2.

the paper pulp that embodiment 6. bleaches clean and dry

The paper pulp of the bleaching available from embodiment 5 is diluted to <2% denseness, and processes to remove sandstone, dirt particle and other dusts and undesirable material by centrifugal cleaner.These cleaners have 20psig difference at cleaner place.In this stage, there is 1% loss of yield.

After the paper pulp of cleaning and bleaching, before being dried in air ejector dryer, be shaped to sheet material and be pressed into 50% drying solid.Minimum aridity is 92%.Sheet material is cut into required size, and be stacked into the bundle with required size and weight.By these bale packagings, hitch and store for transporting.

embodiment 7. is available from the ECF bleaching of the paper pulp of embodiment 3

To κ number be 5 or lower paper pulp carry out the ECF bleaching that order is D100/E/D.

The D100 stage (low pH, approximately 2.4, the ECF stage is in order to by delignified pulp lignifying): process denseness and be 10% paper pulp under 0.25 the k factor at 50 ℃ 60 minutes.Final pH is 2.5, and residual chlorine extremely can not detect for few.

The Ep stage: process available from the paper pulp in D100 stage 60 minutes with hydrogen peroxide (0.50 % by weight to 0.8 % by weight of dry pulp weight) at 80 ℃.Final pH is 10.5-11.0, and the final ISO whiteness of the paper pulp obtaining is about 80-82%.The viscosity of the paper pulp of bleaching is high.

The D stage: process available from the paper pulp in Ep stage 150 minutes with chlorine dioxide (1.2 % by weight of dry pulp weight) at 80 ℃.Final pH is 3.5-4.0, and residual chlorine dioxide is 0.05%, and the final ISO whiteness of the paper pulp of bleaching is approximately 89%.The viscosity of the paper pulp of bleaching is high.

embodiment 8. is available from the TCF bleaching of the paper pulp of embodiment 3

To κ number be 5 or lower paper pulp there is the TCF bleaching that the order of following reaction condition is Q/P/PO.

The Q stage: at 80 ℃ by the 0.5-0.7 % by weight of DTPMPA(dry pulp weight) process the paper pulp 30 minutes that denseness is 10%.Final pH is 7.

The P stage: at 85 ℃ by 0.25 % by weight of hydrogen peroxide (2.0 % by weight of dry pulp weight), NaOH (the 1.0-1.1 % by weight of dry pulp weight), DTPMPA(dry pulp weight), MgSO ₄(0.60 % by weight of dry pulp weight), NaSiO ₃(0.50 % by weight of dry pulp weight) processed available from the paper pulp in Q stage 60 minutes.Final pH is 10.5-11.0, and the final ISO whiteness of the paper pulp obtaining is approximately 80%.Residue is approximately 0.05%.The viscosity of the paper pulp of bleaching is high.

The PO stage: at 120 ℃ by 0.25 % by weight of hydrogen peroxide (5 % by weight of dry pulp weight), DTPMPA(dry pulp weight), MgSO ₄(0.60 % by weight of dry pulp weight), NaSiO ₃(0.50 % by weight of dry pulp weight) processed available from the paper pulp in P stage 120 minutes.The final ISO whiteness of the paper pulp of bleaching can be 88.00%.The viscosity of the paper pulp of bleaching is high.

the benchmark intensity of the pulp product that embodiment 9. is made by bagasse

i) Bagasse Material is clean

By the clean bagasse #11 of same processes as described in Example 1, different is uses 3/8 " sieve but not 1/8 " sieve.

iI) boiling

Under the maximum temperature of approximately 165 ℃, at liquid/dried fibres, than 8.0(denseness, be approximately 12%) under, by 0.2 % by weight of NaOH (22 % by weight of OD bagasse) and the dry weight of AQ(OD bagasse) processing is through clean bagasse 35 minutes.From 90 ℃ of times that reach maximum temperature be 60 minutes.

The target H-factor is 452.Through screening and the κ number of quick-drying paper pulp, be 5.0, boiling productive rate is 56.8%, through the productive rate of the paper pulp of screening, is 55.8%, and always barrier is that 1.0% (+0.010 "), the viscosity of paper pulp is 44.0mPa.s.

By first paper pulp being diluted to 1.0% denseness, then in the case with sieve screen apertures base plate, rinse paper pulp and the paper pulp that obtains is the paper pulp through case washing (box-washed), wherein do not allow the pulp mat accumulation forming on mesh to exceed 1 inch.Once the layer of the paper pulp through washing starts to form on mesh, is just shifted out and preserve the next step for processing.

iII) bleaching

ECF order by D100/Ep/D1 is bleached the paper pulp through washing, so that the paper pulp A4420-1-D1 through case washing to be provided.The pulp sample through washing copying by the TCF order bleaching of Q/P1/PO, to provide the paper pulp A4420-2-PO through case washing.

Use following condition to carry out the ECF order of D100/Ep/D1:

The D100 stage: use 0.25 the k factor, use ClO at 50 ℃ ₂(with Cl ₂count 1.15%) to process denseness be 10% paper pulp 60 minutes.Final pH is 2.0, and residual chlorine is that 0.02g/L(is with available Cl ₂meter).

The Ep stage: 0.7 % by weight of using hydrogen peroxide (0.5 % by weight of dry pulp weight), NaOH(dry pulp weight at 80 ℃) and MgSO ₄(0.1 % by weight of dry pulp weight) processed available from the paper pulp in D100 stage 60 minutes.Final pH is 11.2, and the final ISO whiteness of the paper pulp obtaining is approximately 75.6%.The viscosity of bleaching is 21.4mPa.s just

The D stage: at 80 ℃ by chlorine dioxide (1.5 to 1.7 % by weight of dry pulp weight) and 0.70 % by weight of NaOH(dry pulp weight) processing is available from the paper pulp in Ep stage 150 minutes.Final pH is 4, and residual chlorine dioxide is 0.09%, and the final ISO whiteness of the paper pulp of bleaching is approximately 88.4%.

Use following condition to carry out the TCF order of Q/PO.

The Q stage: at 80 ℃ by 0.5 % by weight of DTPMPA(dry pulp weight) process the paper pulp 30 minutes that denseness is 10%.Final pH is 6.6.

The P1 stage.At 85 ℃ by 0.5 % by weight of hydrogen peroxide (2.0 % by weight of dry pulp), NaOH (1.1 % by weight of dry pulp), DTPMPA(dry pulp), magnesium sulfate (0.6 % by weight of dry pulp), sodium metasilicate (1.0 % by weight of dry pulp) processes available from the paper pulp in Q stage 60 minutes.Final pH is 11.2, and the ISO whiteness of paper pulp is approximately 67.7%.Residual peroxide is 1.25%.

The PO stage: at 120 ℃ by 0.5 % by weight of hydrogen peroxide (6.0 % by weight of dry pulp weight), NaOH (2.8 % by weight of dry pulp weight), DTPMPA(dry pulp weight), MgSO ₄(0.60 % by weight of dry pulp weight), NaSiO ₃(3.0 % by weight of dry pulp weight) are processed and are reached 120 minutes available from the paper pulp in P1 stage.Final pH is 11.2, and the final ISO whiteness of the paper pulp obtaining is approximately 86%.Residual hydrogen peroxide is approximately 0.39%.

Table 1 shows the paper pulp A4420-1-D1(paper pulp 9-1 through case washing) and through the paper pulp A4420-2-Po(paper pulp 9-2 of case washing) κ number and ISO whiteness.

table 1: the κ number of paper pulp 9-1 and paper pulp 9-2 and ISO whiteness

Analyze	Unit	Paper pulp 9-1	Paper pulp 9-2
				The κ number of the paper pulp before bleaching	?	4.57	4.57
ISO whiteness	%	89	86.5
				Gross production rate	%	>50	>50

Table 2 shows than the bagasse pulp available from Thailand's grinding machine (paper pulp 9-3), with standard paper pulp (the paper pulp 9-4 from bagasse under 0 revolution in TAPPI standard P FI analyzes, the bagasse pulp of bleaching, paper pulp Atlas (atlas) paper pulp #60), with TAPPI standard P FI analyze in 0, standard paper pulp (the paper pulp 9-5 from timber under 1000 and 2000 revolution, eucalyptus bleached kraft pulp cenrtl.coastl. Brazil paper pulp, paper pulp Atlas paper pulp #35), through the paper pulp A4420-1-D1(paper pulp 9-1 of case washing) and through the paper pulp A4420-2-Po(paper pulp 9-1 of case washing) benchmark intensity.

table 2: available from the paper pulp of this embodiment, available from the paper pulp of the bagasse from another grinding machine, from sugarcane the standard paper pulp of slag and from the benchmark intensity of the standard paper pulp of timber

* be most possibly abnormal.

Use standard P FI Ginding process (tappi test method T-248) to evaluate the pulp quality for papermaking.For some revolution, paper pulp arranges middle quilt " whipping " or " refining " in laboratory, to reflect the further processing of paper pulp in grinding machine.Zero revolution means paper pulp not to be further processed.The data of standard timber paper pulp (paper pulp 9-5) show that the further processing of paper pulp has reduced freedom, but have improved intensive parameter, as break, tear and tension parameters.Than those freedoms, tension force and the rupture parameters of standard bardwood pulp (paper pulp 9-5) or do not have with revolution, the bagasse pulp available from this embodiment (paper pulp 9-1 and paper pulp 9-2) without revolution has higher freedom, tension force and rupture parameters.Than those of standard timber paper pulp (paper pulp 9-5) without revolution, tear and extensograph parameter, the bagasse pulp available from this embodiment (paper pulp 9-1 and paper pulp 9-2) without revolution has higher tearing and extensograph parameter.This has shown available from the bagasse pulp of this embodiment to have fabulous papermaking quality and without the required further processing of wood pulp.

Available from the characteristic of the bagasse pulp (paper pulp 9-1 and paper pulp 9-2) of this embodiment also from known bagasse pulp under different revolutions (the standard bagasse pulp available from the paper pulp 9-3 of Thailand's grinding machine and paper pulp 9-4(from paper pulp Atlas)) those characteristics compare (table 3).

table 3: available from the selected parameter of the bagasse pulp of soda AQ slurrying processing

Table 3 has shown the selected parameter of using the bagasse pulp that different revolutions make by separate sources.

When revolution is 0, available from the freedom of the paper pulp (paper pulp 9-1 and paper pulp 9-2) of this embodiment than those freedoms of the bagasse pulp (paper pulp 9-3 and paper pulp 9-4) available from other sources high approximately 10% to approximately 18%.

When revolution is 0, the burst index of paper pulp 9-1 and paper pulp 9-2 is than those burst index of paper pulp 9-3 and paper pulp 9-4 high approximately 60% to 150%.Although under higher revolution, the burst index of paper pulp 9-3 and paper pulp 9-4 increases, burst index and paper pulp 9-4 burst index under 750 revolutions still lower than paper pulp 9-1 or the paper pulp 9-2 burst index under zero revolution of paper pulp 9-3 under 1000 revolutions.

When revolution is 0, the tension parameters of paper pulp 9-1 and paper pulp 9-2 is than those tension parameterses of paper pulp 9-3 and paper pulp 9-4 high approximately 54% to approximately 100%.Although under higher revolution, the tension parameters of paper pulp 9-3 and paper pulp 9-4 increases, tension parameters and paper pulp 9-4 tension parameters under 750 revolutions still lower than paper pulp 9-1 or the paper pulp 9-2 tension parameters under zero revolution of paper pulp 9-3 under 1000 revolutions.

Paper pulp 9-1 and paper pulp 9-2 tear and extensograph parameter also tearing and extensograph parameter higher than paper pulp 9-3 and paper pulp 9-4.

Available from the paper pulp of this embodiment, have than with reference to the significantly higher rupture index of bagasse pulp (approximately 60% to approximately 150% or higher in height).

Paper pulp 9-1 and paper pulp 9-2 are significant and unexpected than the intensive parameter of the improvement with reference to bagasse pulp, and the intensive parameter of described improvement is for example also found in, from other paper pulp that bagasse or other fibre sources (maize straw of following disclosed embodiment 11) make by the disclosed pulping process of the disclosure.

the clean benchmark to the final pulp product of processing available from soda AQ in embodiment 10. slurrying processing the impact of intensity

i) bagasse is clean

According to the clean bagasse #6 of the operation of describing as embodiment 1.

iI) boiling

At approximately 175 ℃, the liquid/dried fibres that is 7.0 than (denseness is approximately 12.5%) under, by 0.3 % by weight of NaOH (20 % by weight of OD bagasse) and the dry weight of AQ(OD bagasse) processing is through clean bagasse 34 minutes.The time that reaches maximum temperature is 60 minutes.

The target H-factor is 1056, and pulping reaction temperature is 175 ℃.The κ number of paper pulp through screening is 4.1, and boiling productive rate is 57.9%, through the productive rate of the paper pulp of screening, is 56.6%, and total barrier is that 1.3% (+0.010 "), the viscosity of paper pulp is 38.3mPa.s.

iII) bleaching

By thering is the TCF that the order of following reaction condition is Q/P, bleach the paper pulp available from boiling step, thereby obtain paper pulp A4354-1-P.

The Q stage: at 80 ℃ by the 0.5-0.7 % by weight of DPTA(dry pulp weight) process the paper pulp 30 minutes that denseness is 10%.PH is 4.

The P stage: at 85 ℃ by 0.25 % by weight of hydrogen peroxide (2.0 % by weight of dry pulp weight), NaOH (the 1.0-1.1 % by weight of dry pulp weight), DTPMPA(dry pulp weight), MgSO ₄(0.60 % by weight of dry pulp weight), NaSiO ₃(0.50 % by weight of dry pulp weight) processed available from the paper pulp in Q stage 60 minutes.Final pH is 10.5-11.0, and the final ISO whiteness of the paper pulp obtaining is approximately 84.75%.Residue is approximately 0.05%.

Paper pulp A4354-2-P, available from the process identical with paper pulp A4354-1-P, is also included in TCF bleaching and by case, washs the clean paper pulp available from boiling step before.

By first paper pulp being diluted to 1.0% denseness, then in the case with sieve screen apertures base plate, rinse paper pulp and obtain the paper pulp through case washing, wherein do not allow the pulp mat accumulation forming on mesh to exceed 1 inch.Once the layer of the paper pulp through washing starts to form on mesh, is just shifted out and preserve the next step for processing.

Paper pulp A4354-1-P(paper pulp 10-1) and paper pulp A4354-2-P(paper pulp 10-2) benchmark intensity be shown in following table 4.

table 4: paper pulp A4354-1-P(paper pulp 10-1) and paper pulp A4354-2-P(paper pulp 10-2) base accurate intensity

Analyze	Unit	Paper pulp 10-1	Paper pulp 10-2
				24 grams, 0.2mm gap	?	?	?
PFI,TAPPI	Revolution	0	0
				C.S. freedom	mL	465	506
Basic weight, Condition Weights	g/m ²	66.50	66.43
				Bulk	cc/g	1.45	1.41
Burst factor	?	33	33
				Burst index	kPa.m ²/g	3.22	3.23
Tear factor	?	59	59
				Tear index	mN.m ²/g	5.74	5.76
Breaking length	km	5.88	6.00
				Tensile index	N.m/g	57.7	58.8
Stretch	%	2.31	2.40
				Anti-tensile can absorb	J/m ²	63.0	66.3
Porosity, Ge Li	sec/100ml	27	24
				Zero span, Pulmac (being dried)	km	10.3	10.0
Optical property:	?	?	?
				Whiteness, ISO	%	84.75	85.6
Opacity	%	68.4	68.1
				CIE color	?	?	?

L*	?	95.29	95.53
				a*	?	-0.67	-0.67
b*	?	2.77	2.53
				Hunter color	?	?	?
L	?	93.98	94.27
				a	?	-0.69	-0.69
b	?	2.81	2.57

Result shows, under 0 revolution, paper pulp A4354-1-P and paper pulp A4354-2-P all have desirable strength (for example tear, tension force and break), and are applicable to the required C.S. freedom of papermaking.Case washing step has increased the C.S. freedom of final bleached pulp, and the product of more wishing is provided.

the soda AQ slurrying of embodiment 11. maize straws

Paper pulp 11(paper pulp L1503-2-Po) by following operation, by maize straw, made:

i) maize straw is clean

To through aging moist maize straw, immerse in cold water 1 hour, " refining under gap, washing on 4.75mm sieve is then washed on 1.4m sieve to use on-gauge plate 0.080.

iI) boiling

Under the maximum temperature of approximately 165 ℃, at liquid/dried fibres, than 7.0(denseness, be approximately 12.5%) under, by 0.2 % by weight of NaOH (20 % by weight of OD maize straw) and the dry weight of AQ(OD maize straw) processing is through clean maize straw 8 minutes.The time that reaches maximum temperature is 48 minutes.

The target H-factor is 200, and pulping reaction temperature is 165 ℃.The κ number of paper pulp through screening is 5.0, and boiling productive rate is 56.8%, through the productive rate of the paper pulp of screening, is 56.5%, and total barrier is 0.2% (+0.010 " sieve), and the viscosity of paper pulp is 101.2mPa.s.

iII) paper pulp cleaning

With lightning type blender, use 1.0% denseness, the flow velocity of 30gpm and the pressure of 34psi, with the clean paper pulp available from boiling step of cyclean.With lightning type blender, in 0.05% denseness, further clean through clean paper pulp by water under the flow velocity of 30gpm and the pressure of 34psi.

iV) bleaching

By thering is the TCF that the order of following reaction condition is QP1QPO, bleach through clean paper pulp, thereby obtain paper pulp L1503-2-Po.

The Q stage: 0.5 % by weight of using DTPMPA(dry pulp weight at 80 ℃) and H ₂sO ₄(0.35%) paper pulp that processing denseness is 10% 30 minutes.Initial pH is 4.0.

The P1 stage: use hydrogen peroxide (1.0 % by weight of dry pulp weight), NaOH (0.8 % by weight of dry pulp weight), MgSO at 85 ℃ ₄(0.3 % by weight of dry pulp weight), NaSiO ₃(4.0 % by weight of dry pulp weight) are processed available from the paper pulp in Q stage 60 minutes.The ISO whiteness of the paper pulp obtaining is that the productive rate in 73.5%, P1 stage is 98.2%.

The Q-stage.At 80 ℃, use 0.5 % by weight of DTPMPA(dry pulp weight) and H ₂sO ₄(0.35%) to process denseness be 10% available from the paper pulp in P1 stage 30 minutes.Initial pH is 4.0.

The PO stage: use hydrogen peroxide (6.0 % by weight of dry pulp weight), NaOH (2.8 % by weight of dry pulp weight), NaSiO at 120 ℃ ₃(4.0 % by weight of dry pulp weight), O ₂(pressure measxurement is 60psi) processes available from the paper pulp in Q stage 120 minutes.Final pH is 10.5, remaining H ₂o ₂be that 0.37%, ISO whiteness is 90.8%, stage productive rate is 95.9%.

The benchmark of paper pulp 11 is shown in Table 5 as follows.

table 5: the benchmark of paper pulp 11

Result shows that the paper pulp with the high ISO whiteness of having of desirable strength parameter is available from maize straw.

the impact of AQ concentration in embodiment 12. boilings processing on ARF slurrying

Thick bagasse washs as described in Example 1, and boiling as described in Example 2, parameter is summarized in the H-factor as high in following table 6(, boiling L1483-1, L1483-2, L1483-3, L1484-3, A4385) and the low H-factor of table 7(, boiling L1486-2, L1488-2, L1488-3, A4397, A4400) in.The impact of the κ number of the %AQ applying in boiling is processed shown in table 6 and 7 on obtained paper pulp is reflected in Fig. 1.

table 6: the impact of the AQ concentration in the soda AQ of bagasse boiling is processed (the high H-factor (～1000))

Paper pulp number	12-1	12-2	12-3	12-4	12-5
						Boiling number	L1483-1	L1483-2	L1483-3	L1484-3	A4385
Boiling：	?	?	?	?	?
						NaOH, in the % of OD fibre weight	20	20	20	20	20
AQ,%	0	0.05	0.1	0.1	0.3
						L/W	7.0	7.0	7.0	7.0	7.0
Maximum temperature, ℃	175	175	175	175	175
						From 90 ℃ of times that reach maximum temperature, min	60	60	60	47	60
Time under maximum temperature, min.	34	34	34	37	34
						?	?	?	?	?	?
Boiling finishes：	?	?	?	?	?
						Remaining EA, g/L, with Na ₂O meter	3.7	2.47	2.93	4.47	2.78
Remaining AA, g/L, with Na ₂O meter	4.63	3.24	3.55	5.24	3.55
						The H-factor	1055	1067	1078	965	1080
?	?	?	?	?	?
						Unbleached paper pulp：	?	?	?	?	?
Boiling productive rate, %	54.9	62*	56.6	52.7	57.3
						Total barrier ,+0.010 ", %	0.66	0.50	1.07	0.5	1.00
Screening productive rate, %	54.2	?	55.5	52.1	56.3
						K, through screening, rapid draing	8.4	6.0	5.5	5.3	5.2
Viscosity, mPa.s	32.1	30.5	26.8	28.7	30.6

table 7: the impact (the low H-factor (～300)) of the AQ concentration in boiling is processed

the goods that embodiment 13. is prepared by the renewable fibre pulp of agricultural

The ARF paper pulp making is as mentioned above prepared as every gram of fibre count with 19,000.The premium grade toilet paper that meets North America high-quality specification is by directly substituting the NBSK of minimum with ARF paper pulp and without any further refining, use ARF paper pulp and making.

Can by with ARF paper pulp or as described herein other pulp composition partially or completely substitute the wood pulp of prior art, the example of other goods that made by paper pulp as herein described comprises thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper (as OGR, bleaching wrapping paper, flexible package punch paper), more uncommon paper (as wet strength paper and release liner), regeneration liner board and molded packaging product.

Although the present invention is described with reference to preferred embodiment and specific embodiments, those skilled in the art are easy to understand without departing from the spirit and scope of the present invention in the situation that, and many modifications of the present invention and remodeling are possible.Therefore, should know that understanding only by way of example but not the mode limiting the scope of the invention carry out this description.All lists of references are herein incorporated herein by reference.

Claims

1. goods of being prepared by pulp composition, described pulp composition comprises the fiber from the renewable fibre source of agricultural, wherein said pulp composition is unbleached, and have approximately 15 or lower κ number, high freedom, at least about the breaking length of 5.50km, at least about 6.00mN.m ²the tear index of/g and at least about 3.00kPa.m ²the burst index of/g.

2. goods according to claim 1, described goods are selected from thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper, OGR, bleaching wrapping paper, flexible package punch paper, wet strength paper, release liner, regeneration liner board and molded packaging product.

3. goods according to claim 1, wherein said κ number is approximately 10 or lower.

4. goods according to claim 1, wherein said κ number is approximately 5 or lower.

5. goods according to claim 1, the renewable fibre source of wherein said agricultural is bagasse or maize straw.

6. goods according to claim 2, the renewable fibre source of wherein said agricultural is bagasse or maize straw.

7. goods according to claim 3, the renewable fibre source of wherein said agricultural is bagasse or maize straw.

8. goods of being prepared by pulp composition, described pulp composition comprises the fiber from the renewable fibre source of agricultural, and wherein said pulp composition has approximately 15 or the lower intensive parameter of not bleaching κ number, high freedom and being enough to papermaking.

9. goods according to claim 8, wherein said pulp composition has at least about the breaking length of 5.50km, at least about 6.00mN.m ²the tear index of/g and at least about 3.00kPa.m ²the burst index of/g.

10. goods according to claim 8, wherein said ISO whiteness is to be less than 50% ISO.

11. goods according to claim 8, wherein said ISO whiteness is approximately 70% or higher.

12. goods according to claim 8, wherein said ISO whiteness is approximately 80% or higher.

13. goods according to claim 9, wherein said ISO whiteness is approximately 80% or higher.

14. goods according to claim 8, wherein said ISO whiteness is approximately 88% or higher.

15. goods according to claim 9, wherein said ISO whiteness is approximately 88% or higher.

16. goods according to claim 8, wherein said ISO whiteness is approximately 90% or higher.

17. goods according to claim 9, wherein said ISO whiteness is approximately 90% or higher.

18. goods according to claim 8, the renewable fiber of wherein said agricultural is bagasse or maize straw.

19. goods according to claim 9, the renewable fiber of wherein said agricultural is bagasse or maize straw.

20. goods according to claim 13, the renewable fiber of wherein said agricultural is bagasse or maize straw.

21. goods according to claim 15, the renewable fiber of wherein said agricultural is bagasse or maize straw.

22. goods according to claim 18, the renewable fiber of wherein said agricultural is bagasse or maize straw.

23. goods according to claim 8, described goods are selected from thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper, OGR, bleaching wrapping paper, flexible package punch paper, wet strength paper, release liner, regeneration liner board and molded packaging product.

24. goods according to claim 9, described goods are selected from thin paper, writing and printing paper, communication paper, bleached paperboard, food contact packing paper, OGR, bleaching wrapping paper, flexible package punch paper, wet strength paper, release liner, regeneration liner board and molded packaging product.

25. 1 kinds of goods of being prepared by pulp composition, described pulp composition comprises agriculture renewable fibre pulp, and the renewable fibre pulp of described agricultural is by comprising prepared by following pulping process:

The first mixture of the product that comprises following material is provided:

The renewable fiber of agricultural,

Water,

Concentration is approximately 0.1 % by weight of dried fibres or higher anthraquinone or derivatives thereof, and

Alkali,

Wherein said mixture has liquid/dried fibres ratio of approximately 4 to approximately 10, and approximately 60 or higher initial κ number; And

Be enough to form have approximately 15 or lower κ number, high freedom and be enough to the digestion time of the second mixture of the intensive parameter of papermaking and conditions of cooking under make described mixture reaction.

26. goods according to claim 25, the wherein said intensive parameter that is enough to papermaking is selected from least about the breaking length of 5.50km, at least about 6.00mN.m ²the tear index of/g, at least about 3.00kPa.m ²the burst index of/g or their combination.

27. goods according to claim 26, wherein said conditions of cooking and digestion time provide approximately 200 or the higher H-factor.

28. goods according to claim 27, the wherein said H factor is approximately 1000 or higher.

29. goods according to claim 26, wherein said the second mixture has approximately 10 or lower κ number.

30. goods according to claim 26, wherein said the second mixture has approximately 5 or lower κ number.

31. goods according to claim 25, the renewable fiber of wherein said agricultural comprises bagasse or maize straw.

32. goods according to claim 26, wherein said pulping process also comprises described the second mixture of bleaching.

33. goods according to claim 25, the renewable fibre pulp of wherein said agricultural has approximately 60% or higher ISO whiteness.

34. goods according to claim 25, the renewable fibre pulp of wherein said agricultural has approximately 70% or higher ISO whiteness.

35. goods according to claim 25, the renewable fibre pulp of wherein said agricultural has approximately 80% or higher ISO whiteness.

36. goods according to claim 25, the renewable fibre pulp of wherein said agricultural has approximately 85% or higher ISO whiteness.

37. goods according to claim 25, the renewable fibre pulp of wherein said agricultural has approximately 90% or higher ISO whiteness.