Classifications

• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
  • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
  • D21C9/10—Bleaching ; Apparatus therefor
  • D21C9/16—Bleaching ; Apparatus therefor with per compounds
  • D21C9/163—Bleaching ; Apparatus therefor with per compounds with peroxides
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
  • D21C3/00—Pulping cellulose-containing materials
  • D21C3/04—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides
  • D21C3/06—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides sulfur dioxide; sulfurous acid; bisulfites sulfites
  • D21C3/10—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides sulfur dioxide; sulfurous acid; bisulfites sulfites magnesium bisulfite

Definitions

• the present invention relates to a completely bleached and strong sulfite chemical pulp, a process for the production thereof and products made of this pulp (nonwovens or paper, especially tissue paper).
• chemical pulp is a fibrous material obtained from plant raw materials from which most non-cellulose components have been removed by chemical pulping without substantial mechanical post-treatment.
• chemical pulping processes such as the sulfite or sulfate (Kraft) process, primarily the lignin components and the hemi-cellulose components are dissolved from the wood to varying degrees depending on the field of application of the chemical pulp.
• the result is a fibrous material consisting primarily of cellulose.
• Mechanical pulp is the general term for fibrous materials made of wood entirely or almost entirely by mechanical means, optionally at increased temperatures. Mechanical pulp is subdivided into the purely mechanical pulps (groundwood pulp and refiner mechanical pulp) as well as mechanical pulps subjected to chemical pretreatment: chemo-mechanical pulp (CMP), such as chemo-thermomechanical pulp (CTMP).
• CMP chemo-mechanical pulp
• CMP chemo-thermomechanical pulp
• the strength of papers made from chemical pulps is substantially determined by the pulping degree of the wood used as starting material.
• the binding ability of the fibers first increases as more and more lignin is removed and reaches a maximum at a lignin content of about 10%. At this residual lignin content, the fibrous material has good stiffness and resistance to tearing along with a high binding ability.
• the overall strength of the chemical pulp decreases due to the strong attack of most of the pulping chemicals on the carbohydrate portion (cellulose and hemicellulose) of the wood.
• Second pulp chemical pulp recovered by the sulfate process
• sulfate chemical pulp chemical pulp recovered by the sulfate process
• the lignin must be removed completely, since even small amounts of residual lignin are discolored due to chemical changes in the lignin structure (primary condensation). This is largely carried out in a pulping process. Any residual lignin still present is then removed in several bleaching steps.
• the native lignin is less discolored by the acidic sulfite process. For this reason, it was possible to use high-yield chemical pulps made by acidic or semi-acidic sulfite processes in unbleached form for special applications. If a higher degree of brightness was required, such chemical pulps were also bleached in a delignifying manner with chlorine and bleaching agents containing chlorine. However, these products were unable to satisfy the ever-increasing optical demands. In addition, environmental concerns about bleaching agents containing chlorine and chemical pulps containing chlorine led to a situation where industrial-level production of high-yield chemical pulps was not pursued. Furthermore, less expensive recycling paper has increasingly been used in paper production.
• G. Jayme, L. Broschinksi, W. Matzke (in Das Textil 18, 1964, pages 308 through 314) present a general survey of high-yield chemical pulps and give a detailed description of rapid pulping in the vapor phase with magnesium bisulfite at a maximum temperature of 180°C over a period of 8 to 20 minutes.
• DE-A-1- 517 219 relates to the preparation of a (high-yield) sulfite chemical pulp.
• Wood raw material is pulped with an aqueous solution containing sulfite and/or bisulfite ions as well as sodium, potassium, magnesium, or ammonium ions.
• the pH of the solutions at onset of pulping is 3.0 to 7.0, preferably 3.7 to 5.0.
• the maximum pulping temperature is 140° to 190° C, preferably 150° to 170° C.
• the entire pulping process takes more than 400 minutes.
• the residence time at the maximum temperature is 30 to 200 minutes.
• Pulping is carried out at a chlorine number of the finished chemical pulp in the range of 15 to 32, the pulped material then being subjected to controlled defibration and/or defibration/refinement. After that, fines are removed in an amount of 0.2 to 7 % of the amount of the chemical pulp.
• US 4,634,499 and US 4,734,162 each relate to processes for preparing a chemical pulp from hardwood which is especially suitable for the preparation of tissue papers. Pulping is carried out with ammonium sulfite, first at less than 110° C, then at a maximum temperature of 140° C to 155° C at a pH of about 2 to 3. The chemical pulp is not subjected to an additional bleaching step.
• EP 0 287 960 A relates to a process for preparing a hemicellulose hydrolysate and a special chemical pulp by a two-step process, wherein
• the resulting ligno-cellulosic material is mechanically defibrated and optionally bleached.
• Yields obtained in this manner range from 37.0 % to 45.7 % based on the wood used, the kappa number after cooling ranges from 17.2 to 48.1, and the degree of brightness (ISO value) after bleaching with chlorinated agents at 48.2 to 87.1.
• GB-1,546,877 B relates to a CTMP (chemo-thermomechanical pulp) which is suitable for absorbant products such as tissue paper, and, additionally, has a light color. Yields at 85 % to 95 % are well above the common values for high yield pulps.
• the production process comprises the following steps:
• Suitable bleaching chemicals are alkali metal peroxides such as sodium peroxide or hydrogen peroxide, or reducing bleaching agents such as dithionite, hydroxyl amine, thiourea, or thioglycolic acid.
• An essential feature of the resulting chemical pulp is a content of at least 10 % by weight of sulfonated fiber bundles, each consisting of two to four individual fibers.
• EP 0 446 110 A describes a process for bleaching chemical pulps (yield ranges approx. 85 to 90 %), which are obtained mechanically (mechanical pulp), optionally combined with chemical methods (chemomechanical pulp) and/or thermal methods.
• This bleaching process comprises the following steps:
• this process produces degrees of brightness of 83.9% ISO.
• Bleached mechanical pulps and bleached chemomechanical pulps have the further disadvantage of an unstable degree of brightness. This is due to the fact that the bleaching chemicals convert chromophoric groups of the lignin into non-chromophoric groups, which however are unstable. This type of reduction in the degree of brightness (discoloration) may be induced either by light or heat.
• a disadvantage of known chemical pulps is their chlorine content and/or formation within the bleach of soluble reaction products containing chlorine, which is environmentally undesirable.
• a further aspect of the invention is to make available an economic process for producing such pulp.
• a further object of the present invention involves providing a process leading to a suitable balance between bleachability and the properties (of the bleached pulps), such as strength, optical quality and yield obtained.
• a further object of the present invention is to make available pulp-based paper or nonwovens and/or the corresponding products which are characterized by both resistance to mechanical stress and high quality of appearance.
• chips from ligno-cellulosic material are partially delignified in a sulfite pulping process, in particular in the presence of magnesium, until kappa values of below 50 (according to DIN 54357, August 1978) are reached.
• the partially delignified fibrous material obtained from the first step has a kappa value of maximally 49, maximally 48, maximally 47, or maximally 46 with increasing preference. Kappa ranges of 30 to 45, in particular 33 to 42 are even more preferred.
• kappa values are preferably achieved by conducting the delignification beyond the point of defibration of the material.
• the point of defibration is the point in time during the pulping at which the fibers subjected to chemical delignification may readily be separated into individual fibers without mechanical defibration.
• the individual fibers are collected generally by pumping off the pulped lignocellulosic material out of the digester.
• the residual lignin content of the pulp resulting from the sulfite process in particular the acidic sulfite process has not only relatively few chromophoric groups, but it is also less condensed and therefore more reactive.
• ligno-cellulosic material includes all materials containing cellulose and lignin as main components, typically wood. In (dry) wood, the lignin content is generally at least 20 wt.-% (hardwood about 22 wt.%, conifers 27 to 33 wt.-%).
• the cellulose content of wood is at least 40 wt.-%, generally 40 to 50 wt.-%.
• softwood from conifers and hardwood from deciduous trees may be used in the process of the invention.
• suitable kinds of wood comprise softwoods such as spruce or pine, and hardwoods such as aspen, beech, birch, maple, poplar and oak.
• eucalyptus is especially suitable as a hardwood source of fibers for soft tissue papers. The use of spruce and beech is especially preferred.
• the ligno-cellulosic material used Prior to pulping, the ligno-cellulosic material used is roughly chopped into chips.
• the size of the chips may vary and ranges for example from 1 to 5 cm in breadth and length, with a thickness of up to 1.5 cm.
• Pulping (first step) is carried out with an acidic sulfite solution in a known manner, e.g. with an aqueous solution containing sulfite and/or bisulfite ions as well as sodium, potassium, magnesium, or ammonium ions. Suitable methods are described in depth in G. A. Smook, M. J. Kocurek, Handbook for Pulp and Paper Technologists, Tappi, Atlanta, 1982, pages 58 through 65.
• the chemical pulping occurs in a single step, i.e. without sudden (as contrast to gradual) changes in conditions of the process such as pH. The entire pulping process does not require any additional mechanical means, even though this is not excluded by the invention.
• Chips of lignocellulosic material may be pulped in alkaline, neutral, or acidic conditions, however, preferably in an acidic environment with sulfite. Pulping at a pH of 1 to 5, especially 1.2 to 4.0 is particularly preferred.
• pulping is performed with an aqueous solution containing sulfite and/or bisulfite ions as well as magnesium ions.
• the pulping temperature preferably ranges from 130° to 165° C, in particular 135° to 150° C. Until a maximum temperature of 130° to 150° C is attained, heating should preferably be carried out over a period of 30 to 180 minutes, in particular 70 to 140 min, e.g. 90 to 120 min.
• the temperature is maintained at the maximum temperature preferably for a time period of 160 min to 15 hours (900 min), in particular 3 hours to 12 hours (e.g. 4, 6, 8 or 10 hours).
• a time period of 160 min to 15 hours (900 min) may suffice. This is for instance the case for hardwood chips such as beech chips, whereas softwood chips as obtained from spruce may require longer times, preferably in the order of from 480 to 720 min.
• a time period of 30 to 60 minutes is preferred for cooling from the maximum temperature (T max ) to room temperature.
• Total pulping time (heating + pulping at T max + cooling) ranges preferably from 220 to 1140 minutes.
• the SO 2 content of the pulping solution relative to the dry weight (see Examples for its determination) of the lignocellulosic material used preferably equals 5 to 30 % by weight, in particular 15 to 24 % by weight.
• the "active MgO" content can be measured by chloramine titration.
• the lignocellulosic material-to-liquor ratio preferably ranges from 1:1.5 to 1:5, relative to the dry weight of the lignocellulosic material.
• weight of the lignocellulosic material For some types of softwoods, such as spruce, lower ratios in the order of 1:1.5 to 1:3 may be most suitable, whereas particularly good results for hardwood such as beech were obtained with a ratio of from 1:3.5 to 1:4.5.
• the first step of the pulping process according to the invention results in an unbleached chemical pulp (hereinafter also referred to as "fibrous material”), which is then transferred to the bleaching sequence.
• fibrous material unbleached chemical pulp
• the yield of unbleached chemical pulp relative to the dry weight of the ligno-cellulosic material used is often less than 55 % by weight, can be (depending on the type of wood) less than 50 weight %, but preferably amounts to at least 40 % by weight, in particular at least 45 % by weight.
• the degree of brightness of the material thus obtained is preferably more than 45% ISO, more preferably 50 to 75% ISO, even more preferably at least 55 to 70% ISO, in particular more than 60% ISO (e.g. more than 65% ISO).
• the unbleached chemical pulp has the following strength parameters, each measured according to ISO 5269-2; August 1998, on test sheets having a basis weight of about 75 g/m 2 using a standard climate according to DIN EN 20187 (see description in the Examples). All of the following values are based on beaten chemical pulp which corresponds to a freeness value (°SR, measured according to DIN-ISO 5267/1; March 1999) of approx. 25:
• the above dry breaking length values are at least 9 km, more preferably at least 9.5 km, e.g. 10.5 km for softwood pulps such as spruce pulp; and at least 6 km, more preferably at least 7 km, e.g. 7.5 km for hardwood pulps, such as beech pulp.
• Preferred tear strength (dry) values for softwoods such as spruce are at least 65 cN, more preferably at least 70 cN, e.g. 75 cN; preferred values for hardwood such as beech are at least 50 cN, more preferably at least 53 cN, e.g. 57 cN
• the sulfite pulping process used as the first step of the process of the invention has the advantage over the sulfate process of producing a pulp having a relatively light color even at higher residual lignin contents.
• This intermediate which likewise is a part of the invention, as well as the process steps producing it, is then subjected to bleaching in one or more steps.
• the chemical pulp resulting from the first stage is separated from the cooking liquor in a known manner, e.g. it may be filtered and preferably washed (usually with water).
• each bleaching sequence used according to the invention is bleaching with a chlorine-free oxidant, in the presence of a base in a so-called “first bleaching step".
• the entire bleaching sequence is carried out with chlorine-free agents.
• chlorine-free bleaching sequence and chlorine-free bleaching chemicals mean that the bleaching chemicals contain no chlorine, neither elemental chlorine, nor chlorine-containing compounds such as, e.g. in chlorine dioxide.
• the entire bleaching sequence is preferably carried out without additional mechanical pulping means, i.e. defibration means.
• the entire bleaching sequence may comprise one, two, three or more bleaching steps.
• each step includes preferably only oxidative bleaching agents (rather than reducing conditions as obtained with formamidinosulfinic acid or dithionite).
• the base used in the first bleaching step is preferably the same base that is used in pulping. This makes it easier to close water cycles, since the filtrate from the washer after the first bleaching step may be used for washing in the washer after the pulping step. Furthermore, by using the same base, preferably one containing magnesium, the resulting bleach waste liquors may be disposed together with the cooking waste liquors or at least partially recycled. Further economic advantage could be taken from recycling the filtrates in the bleaching stage itself, therefore utilising the residual peroxide in the bleaching stage.
• Sodium hydroxide, magnesium oxide (MgO), and/or magnesium hydroxide (Mg(OH) 2 ) are preferred bases.
• Magnesium oxide (MgO) also includes the use of magnesium hydroxide (Mg(OH) 2 )).
• Hydrogen peroxide (H 2 O 2 ) is a preferred oxidant.
• the amount of oxidant is preferably 30 to 60 kg/t, in particular 35 to 55 kg/t, relative to the fibrous material used. (If not stated otherwise, kg/t always refers to the dry weight of the fibrous material treated).
• the amount of base used preferably ranges from 10 to 50, in particular 15 to 25 kg/t relative to the fibrous material used.
• the first bleaching step is preferably conducted at a temperature of 60° to 90° C, in particular 70 to 85°C.
• the preferred pH range is from 8.5 to 11.5. If magnesium hydroxide or oxide is used as base, the most preferred pH is from 8.5 to 9.5.
• a sodium hydroxide-based stage is preferably conducted at pH 10.5 to 11.5. The duration of this bleaching step is preferably 240 to 420 minutes.
• the effect of this first bleaching step may be intensified by using oxygen.
• oxygen may be used in an amount of 0.5 % to 3 % relative to the dry weight of the fibrous material used.
• This first bleaching step may be combined with at least one other (so-called “second") bleaching step which is also conducted with an oxidant, in the presence of a base.
• oxidant hydrogen peroxide
• PAA peracetic acid
• the amount of oxidant is preferably smaller than in the first bleaching step, in particular less than 35, for instance 25 to 35 kg/t, relative to the dry weight of the fibrous material used.
• the amount of base used in the second bleaching step preferably ranges from 10 to 30, in particular from 12 to 20 kg/t relative to the dry weight of the fibrous material used.
• the second bleaching step is preferably conducted at the same temperature and the same pH range as the first bleaching step.
• the duration of this bleaching step is preferably shorter than that of the first bleaching step, and ranges in particular from 60 to 240 minutes.
• bleaching abilities may be improved by first treating the fibrous material with a complexing agent.
• This is even more preferred for the "first" bleaching step, in particular if this first bleaching step uses hydrogen peroxide. It is believed that this complexing step lowers the transition metal content of the pulp to be bleached and therefore contributes to the stability of hydrogen peroxide which is liable to decompose in the presence of some transition metals.
• suitable complexing agents are nitrogen-containing organic compounds, in particular nitrogen-containing polycarboxylic acids, nitrogen-containing polyphosphonic acids, and nitrogen-containing polyalcohols.
• nitrogen-containing polycarboxylic acids are diethylenetriamine pentaacetic acid (DTPA), ethylenediamine tetraacetic acid (EDTA), and nitrilotriacetic acid (NTA).
• DTPA diethylenetriamine pentamethylenephosphonic acid
• DTPMPA diethylenetriamine pentaphosphonic acid
• diethylenetriamine pentaphosphonic acid are examples of nitrogen-containing poylphosphonic acids.
• Preferred complexing agents are: DTPA, DTPMPA, and EDTA.
• complexing agent may be added in the amount of 0.5 to 3 kg/t relative to the fibrous material used.
• the complexing treatment is performed at higher temperature, preferably at 50 to 70° C. Its duration depends on the temperature used. Most suitably it ranges from 10 min to 60 min.
• the "Q" type complexing technique is most preferred.
• An alternative technique of stabilizing bleaching oxidants, in particular hydrogen peroxide in the presence of a base, such as NaOH or in particular MgO involves the use of water-soluble silicates during the bleaching step. It is preferred to use water-soluble sodium and potassium silicate solutions which are known as "water-glass". Preferably the water-glass has a molar ratio of 2 to 4 mol SiO 2 per mol alkali oxide. It is further possible and preferred to combine the two stabilizing techniques explained, i.e. to conduct a complexing treatment followed by an oxidative bleaching step in the presence of water-soluble silicates (this applies in particular to the use of hydrogen peroxide as oxidant).
• the amounts of stabilizing silicate range from 0.5 to 10 kg/t fibrous material, in particular from 1 to 7 kg/t.
• oxidants e.g. lower amounts of hydrogen peroxide
• stabilizing silicate also require lower amounts of stabilizing silicate.
• an acid treatment prior to an oxidative bleaching step, in particular between two oxidative bleaching steps.
• this acid treatment contributes to a lower profile of transition metal traces in the pulp and therefore increases the efficiency of subsequent oxidative steps, in particular if these are performed with hydrogen peroxide.
• a non-oxidizing, chlorine-free acid such as sulphuric acid is taken. It is preferred to add from 10 to 50 kg/t, in particular from 20 to 40 kg/t acid to the fibrous material. It has proven beneficial to conduct the acid treatment above room temperature (20°C), preferably at temperatures ranging from 30 to 80°C, in particular 40 to 70°C. The duration of this acid treatment is typically from 30 minutes to 180 minutes, preferably from 30 to 90 minutes.
• the acid treatment is preferably conducted at pH values ranging from 2.5 to 3.5.
• the second (optional) bleaching step may be followed by additional oxidizing bleaching steps with chlorine-free oxidants in the presence of base.
• This third oxidizing bleaching can be performed under the same conditions as those described in the second bleaching step, but preferably with even lower amounts of oxidant and shorter durations.
• oxidizing bleaching steps can be combined with a so-called "reducing bleaching step" using a reducing bleaching agent, even though this is not preferred.
• Bleaching agents that are suitable for the reducing bleaching step include water-soluble dithionite salts, hydroxylamine, thiourea, thioglycolic acid, borohydride (e.g. sodium borohydride), or formamidinosulfinic acid. Especially preferred is the use of formamidinosulfinic acid or dithionite, particularly sodium dithionite.
• the amount of reducing agent used in the reducing bleaching step may range from 5 to 15 % by weight relative to the amount of fibrous material used. This reaction can be performed at a pH ranging from 9 to 11.
• Sodium hydroxide or magnesium oxide can be used to set the pH.
• Magnesium oxide has the advantage that the spent filtrate of this step may be utilized together with pulping spent liquor.
• Usable temperatures for the reaction are in the range of 80° to 95° C. The reaction preferably takes from 60 to 90 minutes.
• the total residence time of the pulp in all bleaching steps ranges preferably from 200 to less than 700 minutes, e.g. maximally 650 min, more preferably from 250 to 600 minutes, in particular from 300 to 500 minutes.
• All steps of the bleaching sequence are preferably carried out in an aqueous slurry at fibre consistencies of from 1 to 15 weight%, based on the dry weight of the fibres. Consistencies of from 1 to 5 weight % are preferred for the complexing treatment. The other treatments are more preferably carried out at consistencies ranging from 5 to 15 weight%.
• the fibrous material is preferably separated from the bleaching solution, e.g. by filtration, and washed. In this manner, the consumption of chemicals in bleaching may often be reduced.
• the purity of the pulp according to the invention may be increased.
• the wash water from the washing following the first bleaching step is preferably used for washing the pulp following the pulping process. It is possible in the cases described above to use fresh water in addition to the wash water that is led in countercurrent.
• Selection and sequence of the bleaching steps may be varied, where with multi-step bleaching sequences it is preferred to begin the bleaching sequence with an oxidative bleaching of the type P MgO (bleaching step with hydrogen peroxide in the presence of MgO as base).
• the bleaching may also be conducted in one oxidative bleaching step, preferably hydrogen-peroxide-based bleaching step.
• one oxidative bleaching step preferably hydrogen-peroxide-based bleaching step.
• one oxidative bleaching step is sufficient to efficiently bleach hardwoods, such as beech, if this bleaching steps follows the delignification procedure explained above.
• bleaching sequences as follows:
• bleaching sequences 3, 4 and 6 represent the best mode for practicing the invention.
• the pulp according to the invention has a brightness of at least 83% ISO.
• the invention preferably pertains to pulp having a degree of brightness of more than 86% ISO, for instance at least 86.2% ISO, more preferably at least 86.5% ISO, in particular at least 86.8% ISO, e.g. 88%, 89% or 90% ISO.
• the pulp according to the invention is further characterized by a breaking length (dry) of at least 4 km, and with increasing preference at least 5 km, at least 6 km, at least 7 km, at least 8 km, at least 9 km, and at least 9.5 km, e.g. 10 km [measured (according to Zellcheming V/12/57) on a test sheet made from beaten pulp (freeness of 25° SR measured according to DIN-ISO 5267/1; March 1999) basis weight of approx. 75 g/m 2 , produced according to ISO 5269-2; August 1998, in a standard climate according to DIN EN 20187; November 1993)].
• a breaking length (dry) of at least 4 km, and with increasing preference at least 5 km, at least 6 km, at least 7 km, at least 8 km, at least 9 km, and at least 9.5 km, e.g. 10 km [measured (according to Zellcheming V/12/57) on a test sheet made from beaten pulp (freeness of 25° SR measured according to DIN-ISO 5267/1
• preferred breaking length (dry) values are at least 7 km, preferably at least 8 km, more preferred at least 9 km, in particular at least 10 km, e.g. 10.5 km.
• the breaking length (dry) is at least 4 km, preferably at least 5 km, , more preferred at least 5.5 km, even more preferred at least 6 km, e.g. 6.5 km.
• One advantage of the pulp according to the invention is that in contrast to mechanical pulp or chemomechanical pulp, its degree of brightness does not significantly decline during further processing and usage.
• the pulp according to the invention is substantially free of chlorine and/or chloride.
• the pulp has an OX content of less than 30 mg/kg, or in particular, is free of OX.
• the OX content relates to the residual halogen organic compounds in the pulp, which may essentially be formed during bleaching and are measured in accordance with DIN 38414/18 and PTS-RH012/90.
• Pulp that is low in OX or is OX-free, and/or products derived from such pulp are more environmentally compatible than pulp and pulp-derived products containing OX. This also applies to the production process. In order to close water cycles as much as possible, it is likewise preferred that only chlorine-free chemicals be used in pulp production, because that way a build-up of chlorine, chloride, and/or chlorine-containing substances may be avoided.
• the bleached, unbeaten pulps according to the invention have the same bleached, unbeaten pulps according to the invention.
• test sheets which were produced as described above under breaking length, except for using unbeaten bleached pulp having a degree of freeness of about 12 to 14°SR.
• the (bleached) pulp according to the invention preferably has a very low fiber bundle content of bundles having at least two fibers, i.e. preferably less than 1 % by weight relative to the dry weight. It is more preferred for it to be free of such bundles.
• the residual lignin content of the bleached pulp according to the invention ranges preferably from 10 to 29, more preferred from 12 to 25, in particular from 12 to 20.
• For softwood, such as spruce preferred kappa values range from 12 to 25, in particular from 15 to 20.
• Preferred values for hardwood, such as beech are from 10 to 20, more preferably from 12 to 18, in particular from 13 to 17.
• the process according to the invention thus makes it possible to a large extent to delignify lignocellulosic material in very short bleaching sequences. This is possible without the aid of mechanical pulping means.
• the average fiber length of the inventive bleached pulp ranges preferably from 1.8 to 2.2 mm (measured according to Kajaani using a Kajaani machine FS-200).
• the water retention capacity of the pulp according to the invention ranges preferably from 130 to 150 %, in particular from 140 to 145 % (measured according to Zellcheming IV/33/57, as described in the Examples).
• the present invention also relates to paper or nonwoven comprising the bleached pulp according to the invention, preferably in the amount of at least 50 % by weight, in particular at least 80 % by weight, relative to the dry weight of the finished product.
• the paper can be a packaging paper, a graphic paper or tissue paper.
• the paper is a tissue paper.
• the tissue paper or nonwoven may be one-ply or multiple-ply.
• Nonwovens may also be called textile-like composite materials, which represent flexible porous fabrics that are not produced by the classic methods of weaving warp and weft or by looping, but by intertwining and/or by cohesive and/or adhesive bonding of fibers which may for example be present in the form of endless fibers or prefabricated fibers of a finite length, as synthetic fibers produced in situ or in the form of staple fibers.
• the nonwovens according to the invention may thus consist of mixtures of synthetic fibers in the form of staple fibers and the pulp according to the invention.
• Paper are also planar materials, albeit essentially composed of fibers of a plant origin and formed by drainage of a fibrous-material suspension on a wire or between two continuously revolving wires and by subsequent compression and drainage or drying of the thus produced fibrous mat (cf. DIN 6730, May 1996).
• the standard restricts the range of mass per unit area (basis weight) for paper to a maximum of 225 g/m 2 .
• the production process comprise also a sizing and/or smoothing step, along with the typical process steps of sheet formation, pressing, and drying described above.
• tissue production is counted among the paper making techniques.
• the production of tissue is distinguished from paper production by its extremely low basis weight of normally less than 50 g/m 2 and its much higher tensile energy absorption index. (In processing inventive pulp to tissue paper, one generally selects a basis weight of 8 to 30 g/m 2 , especially 10 to 25 g/m 2 per ply.
• the total basis weight of multiple-ply tissue products is preferably equal to a maximum of 65 g/m 2 , more preferably to a maximum of 50 g/m 2 .
• the tensile energy absorption index is arrived at from the tensile energy absorption in which the tensile energy absorption is related to the test sample volume before inspection (length, width, thickness of sample between the clamps before tensile load). Paper and tissue paper also differ in general with regard to the modulus of elasticity that characterizes the stress-strain properties of these planar products as a material parameter.
• a tissue's high tensile energy absorption index results from the outer or inner creping.
• the former is produced by compression of the paper web adhering to a dry cylinder as a result of the action of a crepe doctor or in the latter instance as a result of a difference in speed between two wires ("fabrics"). This causes the still moist, plastically deformable paper web to be internally broken up by compression and shearing, thereby rendering it more stretchable under load than an uncreped paper.
• Most of the functional properties typical of tissue and tissue products result from the high tensile energy absorption index (see DIN EN 12625-4 and DIN EN 12625-5).
• tissue papers and hygiene products are represented by hygiene papers, particularly tissue papers and hygiene products (tissue products) made therefrom and which are e.g. used in personal grooming and hygiene, the household sector, industry, the institutional field in a wide variety of cleaning processes. They are used to absorb fluids, for decorative purposes, for packaging or even as supporting material, as is common for example in medical practices or in hospitals.
• Hygiene paper primarily includes all kinds of dry-creped tissue paper, as well as wet-creped paper and cellulose or pulp wadding.
• tissue paper or more accurately raw tissue paper.
• the one-ply raw tissue may be built up of one or a plurality of layers respectively.
• tissue products All one-ply or multi-ply final products made of raw tissue and tailored to the end user's needs, i.e. fabricated with a wide variety of requirements in mind, are known as "tissue products".
• tissue products All one-ply or multi-ply final products made of raw tissue and tailored to the end user's needs, i.e. fabricated with a wide variety of requirements in mind, are known as "tissue products".
• tissue products as used in the description and the claims thus also covers the term “tissue products”.
• tissue paper Typical properties include the ready ability to absorb tensile stress energy, their drapability, good textile-like flexibility, properties which are frequently referred to as bulk softness, a high surface softness, a high specific volume with a perceptible thickness, as high a liquid absorbency as possible and, depending on the application, a suitable wet and dry strength as well as an interesting visual appearance of the outer product surface.
• tissue paper to be used for example as cleaning cloths, sanitary products (e.g. toilet paper), paper handkerchiefs, cosmetic wipes (facials) or as serviettes/napkins.
• tissue paper is to be made out of the pulp according to the invention, the process essentially comprises
• the pulp is refined prior to formation.
• the resulting pulp has a freeness value of more than 15, in particular more than 16 and simultaneously not more than 26 °SR. With an increased freeness value there is an increase in breaking length. It is further preferred to refine only long fibres as occurring in softwood. According to a further preferred embodiment, a mixture of unrefined hardwood short fibres and refined softwood long fibres is used to prepare the aqueous slurry which is then supplied to the formation part of the paper machine.
• This additional surface treatment (beating), which has a favorable effect on the strength properties of the resulting paper/tissue paper, may preferably be brought about within the pulp refinement system of a paper/tissue paper machine.
• such surface treatment (beating) occurs as part of pulp production, i.e. while it is still at the pulp plant.
• a refiner is particularly suitable for this purpose. Fibrillation of the surface occurs during mechanical treatment of the pulp/water suspension. This treatment influences the static and dynamic strength properties.
• the fibers are shortened (cut) or are fibrillated, which includes the separation of the outer layers of the fiber wall, this latter process substantially increasing the surface and bonding capacity of the fibers.
• the refiner operating mode associated with fibrillation is therefore preferred.
• Paper can be formed by placing the fibers, in an oriented or random manner, on one or between two continuously revolving wires of a paper making machine while simultaneously removing the main quantity of water of dilution until dry-solids contents of usually between 12 and 35 % are obtained.
• Drying the formed primary fibrous web occurs in one or more steps by mechanical and thermal means until a final dry-solids content of usually about 93 to 97 %.
• tissue making this stage is followed by the crepe process which crucially influences the properties of the finished tissue product in conventional processes.
• the conventional dry crepe process involves creping on a usually 4.5 to 6 m diameter drying cylinder, the so-called yankee cylinder, by means of a crepe doctor with the aforementioned final dry-solids content of the raw tissue paper (wet creping can be used if lower demands are made of the tissue quality).
• the creped, finally dry raw tissue paper (raw tissue) is then available for further processing into the paper product or tissue paper product according to the invention.
• the invention gives preference to the use of a modified technique in which an improvement in specific volume is achieved by a special kind of drying within process section b and in this way an improvement in the bulk softness of the thus made tissue paper is achieved.
• This process which exists in a variety of subtypes, is termed the TAD (through air drying) technique. It is characterized by the fact that the "primary" fibrous web (like a nonwoven) that leaves the sheet making stage is pre-dried to a dry-solids content of about 80% before final contact drying on the yankee cylinder by blowing hot air through the fibrous web.
• the fibrous web is supported by an air-permeable wire or belt and during its transport is guided over the surface of an air-permeable rotating cylinder drum. Structuring the supporting wire or belt makes it possible to produce any pattern of compressed zones broken up by deformation in the moist state, resulting in increased mean specific volumes and consequently leading to an increase in bulk softness without decisively decreasing the strength of the fibrous web .
• Another possible influence on the softness and strength of the raw tissue lies in the production of a layering in which the primary fibrous web to be formed is built up by a specially constructed headbox in the form of physically different layers of fibrous material, these layers being jointly supplied as a pulp strand to the sheet making stage.
• the following procedural steps are normally used individually or in combination: cutting to size (longitudinally and/or cross cutting), producing a plurality of plies, producing mechanical ply adhesion, volumetric and structural embossing, ply adhesion, folding, imprinting, perforating, application of lotions, smoothing, stacking, rolling up.
• an intermediate step preferably occurs with so-called doubling in which the raw tissue in the finished product's desired number of plies is usually gathered on a common multiply master roll.
• the processing step from the raw tissue that has already been optionally wound up in several plies to the finished tissue product occurs in processing machines which include operations such as repeated smoothing of the tissue, edge embossing, to an extent combined with full area and/or local application of adhesive to produce ply adhesion of the individual plies (raw tissue) to be combined together, as well as longitudinal cut, folding, cross cut, placement and bringing together a plurality of individual tissues and their packaging as well as bringing them together to form larger surrounding packaging or bundles.
• the individual paper ply webs can also be pre-embossed and then combined in a roll gap according to the foot-to-foot or nested methods.
• Spruce chips of a length of 13 to 35 mm and with a thickness of 1 to 10 mm were pulped in a magnesium bisulfite solution (SO 2 as hydrogen sulfite or sulfite-bound SO 2 ) having a total SO 2 content of 16% by weight/wood (dry weight) and a magnesium content (measured as active MgO) of 5,0 % by weight/wood (dry weight) at an initial pH of 4,0 and temperature of 146° C.
• the wood-to-liquor ratio was 1:2. Heating to the maximum temperature of 146°C took 120 minutes. The temperature was maintained at the maximum level for a total of 10 hours (600 minutes).
• the resulting pulp was separated from spent liquor, washed with water, and dried, yielding approximately 54 % (dry weight) relative to the wood used, at a kappa number of 37,0 and a degree of brightness of 67,5 % ISO.
• the washed pulp was not subjected to a complexing treatment. Instead the pulp was immediately bleached in aqueous solution containing 50 kg of hydrogen peroxide and 18 kg MgO/ oven-dried pulp (at a consistency of 11 %) for a reaction time of 210 minutes and at a reaction temperature of 80° C. Additionally 3 kg/t of sodium silicate/oven-dried pulp was added to stabilise the hydrogen peroxide against degradation.
• the brightness after the first bleaching stage (PMgO) was approximately 83 % ISO.
• the washed pulp was subsequently subjected to an acidic treatment, being conducted at a temperature of 50° C for a period of 60 minutes with 30 kg/t of sulfuric acid at a consistency of 9 %.
• the pulp was then bleached in aqueous solution containing 30 kg/t of hydrogen peroxide and 15 kg/t NaOH (at a consistency of 13 %) for a reaction time of 120 minutes and at a reaction temperature of 78° C.
• the aqueous solution contained 1,5 kg sodium silicate/oven-dried pulp, added to stabilise the peroxide against degradation.
• Brightness of the resulting pulp was determined to be 87,0 % ISO.
• Beech chips of a length of 15 to 30 mm and with a thickness of 3 to 8 mm were pulped in a magnesium bisulfite solution (free SO 2 as hydrogen sulfite or sulfite-bound SO 2 ) having a total SO 2 content of 18% by weight/wood (dry weight) and a magnesium content (measured as active MgO) of 5,7 % by weight/wood (dry weight) at an initial pH of 4,2 and temperature of 150° C.
• the wood-to-liquor ratio was 1:4. Heating to the maximum temperature of 150°C took 90 minutes. This temperature was maintained at the maximum level for a total of 3.5 hours (210 minutes).
• the resulting pulp was separated from spent liquor, washed with water, and dried, yielding 48,8 % (dry weight) relative to the wood used, at a kappa number of 39,6 and a degree of brightness of 59,6 % ISO.
• the washed pulp subsequently was subjected to complexing treatment by bringing the same into contact with 2 kg/t of complexing agent DTPA at a consistency of 3 % at a temperature of 60° C for a period of 30 minutes.
• the pH value was set at 5.2 for the complexing treatment with H 2 SO 4 .
• the pulp was washed and bleached in aqueous solution containing 40 kg/t of hydrogen peroxide and 20 kg/t MgO (at a consistency of 10 %) for a reaction time of 360 minutes and at a reaction temperature of 80° C.
• To this aqueous solution 2 kg/t of sodium silicate was added to stabilise the hydrogen peroxide against degradation.
• the peroxide consumption was 80,7 % of charge.
• the degree of brightness of the resulting pulp was determined to be 84.1 % ISO.
• the yield (dry weight) of the pulp obtained after the bleaching sequence was 95.5 % by weight relative to the dry weight of the pulp subjected to the bleaching sequence.
• Beech chips of a length of 15 to 30 mm and with a thickness of 3 to 8 mm were pulped in a magnesium bisulfite solution (free SO 2 as hydrogen sulfite or sulfite-bound SO 2 ) having a total SO 2 content of 18% by weight/wood (dry weight) and a magnesium content measured as active MgO of 5,7 % by weight/wood (dry weight) at an initial pH of 4,2 and temperature of 150° C.
• the wood-to-liquor ratio was 1:4. Heating to the maximum temperature of 150°C took 90 minutes. This temperature was maintained at the maximum level for a total of 3.75 hours (225 minutes).
• the resulting pulp was separated from spent liquor, washed with water, and dried, yielding 49,1 % (dry weight) relative to the wood used, at a kappa number of 35,6 and a degree of brightness of 62,1 % ISO.
• the washed pulp subsequently was subjected to complexing treatment by bringing the same into contact with 2 kg/t of complexing agent DTPA at a consistency of 3 % at a temperature of 60° C for a period of 30 minutes.
• the pH value was set at 5.2 for the complexing treatment with H 2 SO 4 .
• the degree of brightness of the resulting pulp was determined to be 86,0 % ISO.
• the yield (dry weight) of the pulp obtained after the bleaching sequence was 95.9 % by weight relative to the dry weight of the pulp subjected to the bleaching sequence.
• Beech chips of a length of 15 to 30 mm and with a thickness of 3 to 8 mm were pulped in an acid magnesium sulfite solution (free SO 2 as hydrogen sulfite or sulfite-bound SO 2 ) having a total SO 2 content of 20% by weight/wood (dry weight) and a magnesium content measured as active MgO of 4,4 % by weight/wood (dry weight) at an initial pH of 1,7 and temperature of 138° C.
• the wood-to-liquor ratio was 1:4. Heating to the maximum temperature of 138°C took 90 minutes. This temperature was maintained at the maximum level for a total of 3.0 hours (180 minutes).
• the resulting pulp was separated from spent liquor, washed with water, and dried, yielding 49,9 % (dry weight) relative to the wood used, at a kappa number of 39.0 and a degree of brightness of 46,8 % ISO.
• the washed pulp subsequently was subjected to complexing treatment by bringing the same into contact with 2 kg/t of complexing agent DTPA at a consistency of 3 % at a temperature of 60° C for a period of 30 minutes.
• the pH value was set at 5.2 for the complexing treatment with H 2 SO 4 .
• the pulp was washed and bleached in aqueous solution containing 40 kg/t of hydrogen peroxide and 40 kg/t NaOH (at a consistency of 10 %) for a reaction time of 360 minutes and at a reaction temperature of 70° C.
• This aqueous solution contained 5 kg/t of sodium silicate to stabilise the hydrogen peroxide against degradation.
• the peroxide consumption was 69,8 % of charge.
• the degree of brightness of the resulting pulp was determined to be 86,0 % ISO.
• the yield (dry weight) of the pulp obtained after the bleaching sequence was 92,2 % by weight relative to the dry weight of the pulp subjected to the bleaching sequence.
• the pulp which is pulped and bleached according to the invention, and/or any paper produced from such are characterized by an excellent combination of degree of brightness and strength properties.
• the pulp according to the invention has a high stability in degree of brightness.

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• 2002
  • 2002-06-17 EP EP02013497A patent/EP1375734A1/de not_active Withdrawn

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