WO2008077450A1 - Procédé de production de papier tissu - Google Patents

Procédé de production de papier tissu Download PDF

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Publication number
WO2008077450A1
WO2008077450A1 PCT/EP2007/010165 EP2007010165W WO2008077450A1 WO 2008077450 A1 WO2008077450 A1 WO 2008077450A1 EP 2007010165 W EP2007010165 W EP 2007010165W WO 2008077450 A1 WO2008077450 A1 WO 2008077450A1
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WO
WIPO (PCT)
Prior art keywords
pulp
wood
digestion
annual plants
lignin
Prior art date
Application number
PCT/EP2007/010165
Other languages
German (de)
English (en)
Inventor
Hans-Ludwig Schubert
Frank Peter Meltzer
Esa-Matti Aalto
Original Assignee
Voith Patent Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE200610061480 external-priority patent/DE102006061480A1/de
Priority claimed from DE200710017061 external-priority patent/DE102007017061A1/de
Application filed by Voith Patent Gmbh filed Critical Voith Patent Gmbh
Priority to CA002673175A priority Critical patent/CA2673175A1/fr
Priority to BRPI0718883-8A2A priority patent/BRPI0718883A2/pt
Priority to EP07846766A priority patent/EP2126195A1/fr
Priority to JP2009541802A priority patent/JP2010514946A/ja
Publication of WO2008077450A1 publication Critical patent/WO2008077450A1/fr
Priority to US12/432,919 priority patent/US20090266500A1/en

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
    • D21H27/00—Special paper not otherwise provided for, e.g. made by multi-step processes
    • D21H27/002—Tissue paper; Absorbent paper
    • 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
    • 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
    • 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
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F11/00—Processes for making continuous lengths of paper, or of cardboard, or of wet web for fibre board production, on paper-making machines
    • D21F11/14—Making cellulose wadding, filter or blotting paper
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21F—PAPER-MAKING MACHINES; METHODS OF PRODUCING PAPER THEREON
    • D21F11/00—Processes for making continuous lengths of paper, or of cardboard, or of wet web for fibre board production, on paper-making machines
    • D21F11/14—Making cellulose wadding, filter or blotting paper
    • D21F11/145—Making cellulose wadding, filter or blotting paper including a through-drying process
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
    • D21H11/00—Pulp or paper, comprising cellulose or lignocellulose fibres of natural origin only
    • D21H11/02—Chemical or chemomechanical or chemothermomechanical pulp
    • D21H11/06—Sulfite or bisulfite pulp

Definitions

  • the invention relates to a method for producing a tissue web, which is produced from a fiber suspension comprising fibers.
  • the invention also relates to a process for the preparation of a stock suspension for the particular use for the production of tissue webs.
  • Tissue products today are mainly produced from whole pulps, preferably kraft pulps.
  • Typical mixing ratios between long fiber and short fiber pulps are in the 50:50 range.
  • the porosity and permeability of the tissue paper are critically determined by the degree of freeness of the fibers in the stock suspension from which the tissue paper is made.
  • a high freeness causes a high fines content in the suspension, resulting in a low porosity and permeability.
  • a high freeness causes a high water retention value for the fibers of the pulp suspension, whereby the tissue paper is poorly dewatered during its production.
  • tissue web must be tear-resistant.
  • Tear resistance is determined by both the manufacturing process and the degree of beating of the fibers. To increase the tear strength, the tissue paper must be compacted during its production. Furthermore, in order to obtain a high tear strength, the fines content must be high.
  • the object of the invention is therefore to enable the production of tissue paper with a high specific volume, the highest possible tear length with the lowest possible degree of grinding.
  • the pulp suspension contains lignocellulosic pulp of wood or annual plants having a tearing length of more than 6.0 km at 12 0 SR or a tearing length of more than 7.5 km at 15 ° SR and a lignin content of at least 15% in relation to otro pulp for unbleached softwood or a breaking length of more than 4,5 km at 20 0 SR and a lignin content of at least 12% related to the otro pulp for hardwood in the unbleached state or a breaking length of more than 3.5 km at 20 0 SR and a lignin content of at least 10% based on the otro pulp for annual plants in the unbleached state.
  • the fibers show high strength values even at a much lower degree of grinding compared with previously used fibers.
  • the fibrous material according to the invention is able to build up a good bond to adjacent fibers even at a low degree of grinding and thus also less expenditure of grinding energy.
  • the lignin content of the unbleached pulp may advantageously be at least 15%, preferably at least 18%, especially at least 21% of the otro pulp, in hardwood at least 12%, preferably at least 14%, especially at least 16% of the otro pulp and in annual plants at least 10% %, preferably at least 12% and in particular at least 19% of the otro pulp.
  • the breaking length for softwood fiber mass at 12 ° SR should be greater than 7 km, preferably greater than 7.5 km and in particular greater than 8 km.
  • the tenacity for softwood fiber mass at 15 ° SR should be greater than 9 km, preferably greater than 9.5 km and in particular greater than 10 km.
  • the tensile for Hardwood pulp should be at a lignin content of at least 12% and a freeness of 20 SR 0 greater than 6 km, preferably greater than 7 kilometers and in particular greater than 7.5 km away.
  • the tenacity for annual plant fiber mass should be greater than 3.5 km, preferably greater than 4 km and in particular greater than 4.5 km, at 20 ° SR.
  • the fibrous material according to the invention is not only characterized by high breaking lengths. Rather, the strength level is high overall.
  • the fiber properties improve considerably.
  • Bleaching treatment is required for some applications with higher whiteness requirements. It also aims to adjust and improve fiber properties.
  • the bleaching treatment increases the breaking lengths. - A -
  • the pulp suspension lignocellulosic pulp from wood or annual plants should contain, a tenacity of greater than 7.5 km at 15 0 SR and a lignin content of at least 13% based on the oven-dry pulp for softwood in the bleached state or a tenacity of greater than 5 , 0 km at 20 0 SR and a lignin content of at least 10% based on the otro pulp for hardwood in bleached condition or a breaking length of more than 5.5 km at 20 0 SR and a lignin content of at least 10% based on the otro pulp for annual plants in the bleached state.
  • the breaking length for softwood fiber mass at 15 ° SR should be greater than 9 km, preferably greater than 10 km.
  • the tenacity for hardwood pulp should be greater than 5.5 at 20 ° SR and the tenacity for annual plant fiber mass at 25 ° SR should be greater than 5 km, preferably greater than 5.5 km, and more preferably greater than 6 km.
  • the pulp suspension should contain exclusively lignocellulosic pulp as described above.
  • the stock suspension is only partially formed by such lignocellulosic pulp. It is advantageous if between 20 and 80%, preferably between 30 and 50% of the pulp of the pulp suspension of lignocellulosic pulp are formed as described above.
  • tissue web After the formation of a tissue web, it is preferably passed in a dewatering step between an upper, structured and permeable belt and between a lower permeable belt, along which Drainage section pressure is exerted on the upper band, the tissue web and the lower band.
  • the pressure exerted on the arrangement of upper band, tissue web and lower band pressure can be effected by a gas flow and / or by a mechanical pressing force.
  • a gas flows through first the upper band, then the tissue web and then the lower band.
  • the drainage takes place in the direction of the lower band.
  • the arrangement of upper belt, tissue web and lower belt is guided at least in sections between a tensioned press belt and a smooth surface, wherein the press belt acts on the upper belt and the lower band is supported on the smooth surface.
  • the arrangement of upper belt, tissue web and lower belt is at least partially flowed through in the region of the dewatering section of the gas stream, so that the dewatering takes place simultaneously by the pressing force of the press belt and the flow of the gas.
  • the gas flow through the tissue web should be about 150 m 3 per minute and meter length along the drainage path.
  • the press belt should be under a tension of at least 30 kN / m, preferably at least 60 kN / m and in particular 80 kN / m.
  • the press belt should have an open area of more than 50% and a contact area of at least 15%.
  • the smooth surface is preferably formed by the lateral surface of a roller.
  • the generation of the gas flow can advantageously take place via a suction zone in the roll and / or via an overpressure hood arranged above the upper strip.
  • the method according to the invention is based on the fact that higher quantities of chemicals are used for the production of high-yield fibers than has hitherto been customary. More than 5% of softwood chemicals are well above the hitherto common chemicals levels for engineering pulp production, also more than 3.5% for hardwood and 2.5% for annual plants. This high use of chemicals yields fibers with good yield and excellent strength properties. Thus, for softwood at grinding degrees of only 12 0 SR to 15 0 SR, breaking lengths of more than 8 km, but also breaking lengths of more than 9 km and more than 10 km are measured. For deciduous trees, values of more than 5 km, but also breaking lengths of more than 6 km and more than 7 km are measured at only 20 0 SR. This achieves the desired high level of strength.
  • Suitable annual plants are, in particular, bamboo, hemp, rice straw, bagasse, wheat, miscanthus or the like.
  • the fibrous materials produced by the process according to the invention have tear lengths of more than 8 km up to 11 km and tear strengths of more than 70 cN up to more than 110 cN, even at degrees in the range from 12 ° SR to 15 ° SR Leaf weight of 100 g / m 2 .
  • These low levels of grinding are moreover achieved with a low specific requirement of grinding energy, which is less than 500 kWh / t of pulp for softwood pulps, and in hardwood pulps the demand for grinding energy may even be less than 300 kWh / t Fibrous amount.
  • the realization that the high level of strength is already achieved at low grinding degrees of 12 0 SR to 15 0 SR for softwood and 20 0 SR for hardwood and below, is an essential part of the invention.
  • Hardwood fibers with a lignin content of more than 14%, preferably more than 16%, more preferably more than 18% and annual plants with a lignin content of more than 10%, preferably more than 12%, in particular more than 19% can also with the lignin are prepared according to the invention and show a high level of strength.
  • the composition of the chemical solution used for the digestion can be determined in accordance with the wood to be broken or the annual plants and the desired pulp properties. As a rule, only one sulfite component is used. Alternatively or in addition, a sulfide component may be added. Digestion with a sulfite component is not disturbed by the presence of sulfide components. Technically, sodium sulfite is usually used, but also the use of ammonium or potassium sulfite or magnesium bisulfite is possible. In particular, when high amounts of sulfite are used, can be dispensed with the use of an alkaline component, because even without the addition of alkaline components, a high pH value sets, which favors the digestion.
  • an acidic and / or an alkaline component can be added.
  • the alkaline component is usually sodium hydroxide (NaOH) is used. Is possible but also the use of carbonates, especially sodium carbonate. All information on chemical quantities of the digestion process in this document, eg. B. for the total use of chemicals or for the distribution of the sulfite component and the alkaline component, unless otherwise stated, each calculated and reported as sodium hydroxide (NaOH).
  • acids can be added to adjust the desired pH.
  • preference is given to the addition of SO 2 , if appropriate in aqueous solution. It is inexpensive and readily available, especially if the spent chemical solution z. B. based on sodium sulfite, after digestion is prepared for further use.
  • Optimal is a use of z.
  • anthraquinone which is between 0.005% and 0.5%.
  • Use of anthraquinone of up to 1% also provides the desired effect.
  • a use of more than 3% anthraquinone is usually uneconomical.
  • a chemical solution is prepared. Usually an aqueous solution is used.
  • Option can also be provided for the use or addition of organic solvents.
  • Alcohol especially methanol and ethanol, in combination with water, result in particularly effective chemical solutions for the production of high-quality high-yield fibers.
  • the mixing ratio of water and alcohol can be optimized for the respective raw material in a few experiments.
  • the amount of chemicals to be used according to the invention for producing a pulp with a yield of at least 70% is at least 5% for softwood, at least 3.5% for hardwood and at least 2.5% for annual plants, in each case based on the otro wood or annual plant mass to be broken up.
  • the quality of the produced pulp shows the best results with a chemical use of up to 15% for softwoods up to 10% for hardwood and up to 10% for annual plants. Preference is given to between 9% and 11% chemicals based on the used otro wood in softwood added. For hardwoods, the use of chemicals is rather lower, preferably between 4% and 10%, more preferably between 6% and 9% and in annual plants between 3 and 10%.
  • a ratio between an alkaline component and sulfur dioxide (SO 2 ) can be adjusted within a wide range.
  • SO 2 is mentioned here as representative of the above-mentioned acidic component. So it can be used instead of SO 2 and an acid. Since the possibly added quinone component is used only in minimal amounts, usually well below 1%, it is negligible for setting this ratio.
  • a ratio of alkaline component: SO 2 in a range of 5: 1 to 1, 6: 1 is well suited to carry out the inventive method and to achieve fibers with high strength properties.
  • a customary, particularly suitable range is between 2: 1 and 1, 6: 1.
  • the adjustment of the proportionate components takes place depending on the raw material to be digested and the respectively selected process control (digestion temperature, digestion time, impregnation).
  • the process of the invention can be carried out in a wide pH range.
  • the ratio of alkaline component to acidic component or the use of an acidic or an alkaline component can be adjusted so that at the beginning of the process, a pH between 6 and 11, preferably between 7 and 11, more preferably between 7.5 and 10 is set.
  • the more alkaline pH's between 8 and 11, which are beneficial to the process of the invention, also favor the effect of the quinone moiety.
  • the method according to the invention is tolerant with regard to the pH; There are few chemicals required for pH adjustment. This has a favorable effect on the costs of chemicals.
  • acid or alkaline component arises, for.
  • a pH between 5 and 9 usually between 6.5 and 9 in the free-flowing chemical solution and the dissolved organic components that have been liquefied by the digestion, a.
  • the dissolved organic components are mainly lignosulfonates.
  • the liquor ratio ie the ratio of the amount of otro wood or annual plants to the chemical solution, is set between 1: 1, 5 and 1: 6.
  • a liquor ratio of 1: 2 to 1: 4 is preferred. In this range, a good and simple mixing and impregnation of the material to be digested is ensured.
  • a liquor ratio of 1: 3.5 is preferred.
  • the liquor ratio can also be significantly higher, to allow rapid wetting and impregnation.
  • the concentration of the chemical solution can be kept so high that the liquid volumes to be circulated are not too large.
  • the mixture or impregnation of the wood or Einjährauf Stamm preferably takes place at elevated temperatures.
  • Type of digestion liquid or vapor phase
  • the digestion of the mixed or impregnated with the chemical solution lignocellulosic material is preferably carried out at temperatures between 120 0 C and 190 0 C, preferably between 140 0 C and 180 0 C.
  • decomposition temperatures between 150 0 C and 170 0 C. set. Higher or lower temperatures can be adjusted, but in this temperature range, the energy required to heat and accelerate the digestion are in an economic relationship. Higher temperatures can also have a negative effect on the strength and whiteness of the fibers.
  • the pressure generated by the high temperatures can be easily absorbed by appropriate design of the digester.
  • the duration of the heating is only a few minutes, usually up to 30 minutes, advantageously up to 10 minutes, in particular when heated by means of steam.
  • the duration of the heating can take up to 120 minutes, preferably up to 60 minutes, z. B. when it is digested in the liquid phase and the chemical solution is to be heated together with the wood chips.
  • the duration of the digestion is chosen especially depending on the desired pulp properties.
  • the duration of the digestion can be shortened to up to 2 minutes, z. B. in the case of a vapor phase digestion of a Hardwood with low lignin content. But it can also be up to 180 minutes, if z. B. the digestion temperature low and the natural lignin content of the réellezhouden wood is high. Even if the initial pH of the digestion is in the neutral range, a long digestion time may be required.
  • the digestion time is up to 90 minutes, especially in coniferous wood.
  • the digestion time is up to 60 minutes, advantageously up to 30 minutes.
  • a digestion time of up to 60 minutes is mainly considered for hardwoods.
  • the digestion time is up to 90 minutes.
  • a quinone component in particular anthraquinone, allows a reduction of the digestion time to up to 25% of the time required without the addition of anthraquinone. If the use of quinone components is omitted, the digestion time is extended by more than one hour, for example from 45 minutes to 180 minutes, for comparable digestion results.
  • the duration of the digestion is set as a function of the selected liquor ratio.
  • the consumption of chemicals depends on the absolute amount of chemicals used for the digestion, based on the otro wood mass to be digested. The higher the use of digestion chemicals, the lower the direct sales of chemicals. When using 27.5% of chemicals based on otro wood pulp, for example, only about 30% of the chemicals used are consumed. However, when 15% of the chemicals are used in relation to otro wood, 60% of the chemicals used are consumed, as demonstrated in laboratory tests.
  • the consumption of chemicals for the process according to the invention is according to a preferred embodiment of the process during digestion up to 80%, preferably up to 60%, more preferably up to 40%, advantageously up to 20%, particularly advantageously up to 10% of the chemical use, the is used at the beginning of the digestion.
  • the chemical consumption for producing a ton of pulp is about 6%
  • the composition of the removed chemical solution is detected and then adjusted to a predetermined composition for re-use for the production of fibers.
  • the chemical solution that is removed before or after the decomposition of the wood or annual plants no longer has the original composition.
  • At least some of the chemicals used for digestion have - as described above - penetrated into the material to be digested and / or has been consumed in the digestion. The unused chemicals can easily be used again for the next digestion.
  • the process of the invention is specifically controlled so that only as little of the starting material used is degraded or dissolved.
  • the aim is to produce a pulp which has a lignin content of at least 15% based on the otro fiber mass for softwood, preferably a lignin content of at least 18%, more preferably 21%, advantageously at least 24%.
  • For hardwood is sought to achieve a lignin content of at least 12% based on the otro fiber mass, preferably of at least 14%, more preferably of at least 16%, advantageously of at least 18%.
  • the preferred lignin content is between 10 and 28%, in particular between 12 and 26%.
  • the yield of the process according to the invention is at least 70%, preferably more than 75%, advantageously more than 80%, in each case based on the wood used. This yield correlates with that given above
  • Lignin content of the pulp is specific to the species.
  • the yield loss is predominantly a loss of lignin.
  • the proportion of carbohydrates is markedly increased, eg. B. because digestion chemicals in an undesirable manner also bring cellulose or hemicelluloses in solution.
  • a further, advantageous measure is to remove after defibering and optionally grinding the lignocellulosic material, the remaining chemical solution and feed it to a further use.
  • this reuse can include two aspects. On the one hand, the decomposed during the partial digestion or dissolved in organic material, predominantly lignin, further used. It is burned, for example, to gain process energy. Or it is prepared to be used elsewhere. On the other hand, the used and unused chemicals are reprocessed so that they can be used for a renewed, partial digestion of lignocellulosic material. This includes the treatment of used chemicals.
  • the chemical solution used is used extremely efficiently. After defibering and optionally grinding, the pulp is washed to displace the chemical solution as much as possible through water.
  • the filtrate produced in this washing or displacement process contains considerable amounts of chemical solution and organic material.
  • this filtrate is supplied to the removed or separated chemical solution before the chemical solution is fortified and fed to the next digestion.
  • the chemicals and organic components contained in the filtrate do not disturb the digestion. To the extent that they still contribute to delignification during the next digestion, their content is recorded in the chemical solution and taken into account in determining the amount of chemicals required for this digestion.
  • the further contained in the filtrate chemicals behave inert during the pending digestion. They do not bother.
  • the organic constituents contained in the filtrate are also inert. They will continue to be used in the processing of the chemical solution after the next digestion, either to generate process energy or otherwise.
  • Figure 1 an apparatus for performing the method according to the invention
  • Figure 2 a second device.
  • the yield was calculated by weighing the raw material used and the pulp obtained after the pulping, in each case dried at 105 ° C. to constant weight (atro).
  • the lignin content was determined as Klason lignin according to TAPPT T 222 om-98.
  • the acid-soluble lignin was determined according to TAPPI UM 250
  • the breaking length was determined according to Zellcheming regulation V / 12/57.
  • the whiteness was determined by preparing the test sheets according to Zellcheming leaflet V / 19/63, measured according to SCAN C 11: 75 with a Datacolor elrepho 450 x photometer; the whiteness is given in percent according to ISO standard 2470.
  • the viscosity was determined according to the leaflet IV / 36/61 of the Association of Pulp and Paper Chemists and Engineers (Zellcheming). - All% figures in this document are to be read as weight percent unless otherwise specified.
  • otro in this document refers to "oven-dry” material which has been dried at 105 ° C. to constant weight. - The chemicals for the digestion are given in percent by weight as sodium hydroxide, unless otherwise stated.
  • Example 1 Softwood pulping in the liquid phase
  • a mixture of spruce wood and Douglas fir wood chips was after a damping (30 minutes in saturated steam at 105 0 C) with a sodium sulfite pulping solution at a liquor ratio of wood: digestion solution 1: 3 added.
  • the total use of chemicals was less than 15% based on otro woodchips.
  • the pH at the beginning of the digestion was adjusted to pH 8.5-9 by addition of SO 2 .
  • the impregnated with chemical solution spruce wood chips were heated over a period of 90 minutes at 170 ° C and digested for 60 minutes at this maximum temperature.
  • the open-ended wood chips were shredded. Aliquots of the pulp so produced were ground for different lengths to determine the strength at different degrees of grinding. The energy required to shred the partially digested chips was less than 300 kWh / t of pulp.
  • the yield in this experiment was 77% based on the wood pulp used. This corresponds to a pulp with a lignin content of well over 20%.
  • the average lignin content for spruce wood is given as 28% in relation to the otro wood mass (Wagensuppl, Anatomie des Holzes, VEB frabuchverlag für, 1980).
  • the actual lignin content of the pulp is higher than 20%, because during digestion mainly but not exclusively lignin is broken down.
  • Carbohydrates cellulose and hemicelluloses
  • the values given show that the digestion has a good selectivity with regard to lignin and carbohydrate degradation.
  • the whiteness is unexpectedly high with values of over 55% ISO and thus provides a good starting point for a possible subsequent bleaching, in the whiteness of 75% ISO can be achieved.
  • a grinding time of 20 to 30 minutes is required. Up to a grinding time of 20 minutes (freeness SR 12 0 - 15 0 SR), the freeness independent of pH (pH 6 to pH 9.4) developed at the beginning of the pulping process in a narrow range.
  • the pulp was made from spruce wood chips with the pH at the beginning of the digestion being 9.4.
  • the chemical solution 0.1 anthraquinone was added based on the amount of wood used. The duration of the digestion was 60 minutes.
  • the duration of digestion can be reduced from approx. 180 minutes to 60 minutes under otherwise unchanged digestion conditions. This time saving is valuable, above all because the plants for producing pulp can be made smaller. Further savings potential lies in the fact that the temperature required for digestion only needs to be maintained for a much shorter period of time.
  • Eucalyptus chips were added after attenuation with a sodium sulfite digestion solution at a liquor ratio of wood digestion solution 1: 3.
  • the use of chemicals here was 10.5% (as NaOH) on otro woodchips.
  • the pulp was impregnated and the food was heated to the maximum digestion temperature of 170 0 C.
  • the cooking time was 50 minutes.
  • Digestions with eucalyptus wood show that these substances can be produced with a specific energy input for defibration of less than 250 kWh / t.
  • the fibers produced in the vapor phase have excellent strengths.
  • the tenacity was measured, for example, 10 km and 11 km at 15 0 SR.
  • the tear resistance was measured, for example, at 82.8 cN and 91.0 cN.
  • the fibrous materials according to the invention require only a small amount of energy during grinding in order to build up high breaking lengths without reducing the tear propagation resistance.
  • Grinding 12 0 SR was achieved in 0-10 minutes; Grinding degree 13 0 SR 5-30 minutes, usually 10-20 minutes.
  • the Jokro mill had to work for 30-40 minutes and for grind level 15 0 SR it took between 35 and 40 minutes. It is obvious that a grinding up to Mahlgrade by 40 0 SR would require an enormous amount of grinding energy.
  • a particular advantage of the method according to the invention is therefore to be seen in the fact that with low energy consumption to be milled fibers are produced with high strengths.
  • the device for providing a pulp suspension which is used in the process according to the invention for the production of a tissue web, comprises a pulper in which the dry raw materials and pulp and waste paper are dissolved in water and converted into a pumpable state. Subsequently, the substance thus formed is fed to a mixing vessel
  • the stock suspension is ground to a freeness of 12 ° SR or more.
  • the stock suspension is very strongly diluted with white water and fed to a headbox 13.
  • the material emerging from the headbox 13 Pulp has a freeness of less than 20 0 SR and has a tearing length of more than 4.5 km.
  • a stock suspension 1 with the above-mentioned properties emerges from the headbox 13 in such a way that it is injected into the incoming gap between a forming fabric 14 and a structured, in particular 3-dimensionally structured, band 3, whereby a tissue web 1 is formed.
  • the Formiersieb 14 has a directed to the tissue web 1 side, which is smooth relative to that of the structured band 3.
  • the side of the structured band 3 facing the tissue web 1 has recessed areas and elevated areas relative to the recessed areas, so that the tissue web 1 is formed in the recessed areas and the raised areas of the structured band 3.
  • Areas and raised areas is preferably 0.07mm and 0.6mm.
  • the area formed by the raised areas is preferably 10% or more, more preferably 20% or more, and most preferably 25% to 30%.
  • the assembly of upper belt 3, tissue web 1 and forming fabric 14 is directed around a forming roll 15 and the tissue web 1 is substantially dewatered through the forming fabric 14 before the forming fabric 14 is removed from the tissue web 1 and the tissue web 1 on the Volume 3 is transported on.
  • the voluminous sections of the tissue web 1 formed in the recessed areas of the band 3 have a higher volume and a higher basis weight than the sections of the tissue web 1 formed in the raised areas of the band 3.
  • the tissue web 1 therefore already has a 3-dimensional structure due to its formation on the structured band 3.
  • the sheet formation can, however, also take place between two smooth forming fabrics 14, so that a substantially smooth tissue web 1 is formed without a 3-dimensional structure.
  • Tissuebahn 1 is drained in the direction of the belt 2, as indicated by the arrows in both figures.
  • the tissue web 1 wraps around the rolls 2, 3 a roll 5.
  • the voluminous sections are compressed less than the other sections, so that As a result, the voluminous structure of these sections is retained.
  • the pressure for dewatering the tissue web 1 is generated at least in sections at the same time by a gas flow and by a mechanical pressing force in the dewatering step according to FIG.
  • the gas stream flows through first the structured band 3, then the tissue web 1 and then the formed as a felt lower band 2.
  • the gas flow through the tissue web 1 is about 150 m 3 per minute and meter web length.
  • the gas flow is generated by a suction zone 10 in the roller 5, wherein the suction zone 10 has a length in the range between 200 mm and 2500 mm, preferably between 800 mm and 1800 mm, more preferably between 1200 mm and 1600 mm.
  • the negative pressure in the suction zone 10 is between -0.2bar and -0.8bar, preferably between -0.4bar and -0.6bar.
  • the mechanical pressing force is produced by guiding the arrangement of structured band 3, tissue web 1 and band 2 of a dewatering section 11 between a press belt 4 under tension and a smooth surface during the dewatering step, the press belt 4 being structured Band 3 acts and the band 2 is supported on the smooth surface.
  • the smooth surface is formed by the lateral surface of the roller 5.
  • the dewatering section 11 is essentially defined by the wrap area of the press belt 4 around the lateral surface of the roller 5, wherein the wrap area is determined by the distance between the two guide rollers 12.
  • the press belt 4 is under a tension of at least 30 kN / m, preferably at least 60 kN / m or 80 kN / m and has an open area of at least 25% and a contact surface of at least 10% of its entire surface facing the upper band 3.
  • the press belt 4 designed as a spiral link fabric, has an open area of between 51% and 62% and a contact area of between 38% and 49% of its total area facing the upper belt 3.
  • PCT / EP2005 / 050198 should be included in full in the disclosure of the present application.
  • the tissue web 1 leaves the dewatering section 11 with a dry content of between 25% and 55%.
  • the tissue web 1 is guided in a subsequent dewatering step further dewatering step together with the structured band 3 through a press nip, wherein the tissue web 1 is arranged in the press nip between the structured band 3 and a smooth roll surface of a Yankee drying cylinder 7.
  • the press nip here is an extended press nip formed by the Yankee dryer cylinder 7 and a shoe press roll 8.
  • the tissue web 1 rests on one side with a relatively large area on the lateral surface of the Yankee drying cylinder 7, the tissue web 1 resting on the other side on the structured band 3.
  • the recessed areas and the relatively elevated areas of the structured band 3 are in this case designed and arranged relative to one another such that the voluminous sections in the press nip are essentially not pressed. On the other hand, the other sections are pressed, whereby the strength of the tissue web 1 is further increased.
  • a further dewatering step can be provided, which can be carried out by means of a device 9.
  • the tissue web 1, before it passes through the press nip, is guided together with the structured band 3 around an evacuated deflection roller, the structured band 3 being arranged between the tissue web 1 and the evacuated deflection roller (not shown).

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Paper (AREA)

Abstract

L'invention concerne un procédé de production d'une bande de tissu (1) qui est fabriquée à partir d'une suspension de tissu comportant des fibres. Le volume et la longueur à la rupture sont ainsi améliorés grâce à un grain le plus petit possible, la suspension de tissu contenant des fibres lignocellulosiques issues du bois ou de plantes annuelles, qui présentent une longueur à la rupture de plus de 6,5 km à 12 °SR ou une longueur à la rupture de plus de 8,0 km à 15 °SR et une teneur en lignine d'au moins 15 % par rapport à la fibre séchée à l'étuve pour le bois de résineux dans un état non blanchi ou une longueur à la rupture de plus de 4,5 km à 20 °SR et une teneur en lignine d'au moins 12 % par rapport à la fibre séchée à l'étuve pour le bois de feuillus dans un état non blanchi ou une longueur à la rupture de plus de 3,5 km à 20 °SR et une teneur en lignine d'au moins 10 % par rapport à la fibre pour plantes annuelles dans un état non blanchi.
PCT/EP2007/010165 2006-12-23 2007-11-23 Procédé de production de papier tissu WO2008077450A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CA002673175A CA2673175A1 (fr) 2006-12-23 2007-11-23 Procede de production de papier tissu
BRPI0718883-8A2A BRPI0718883A2 (pt) 2006-12-23 2007-11-23 Processo para produção de papel de seda
EP07846766A EP2126195A1 (fr) 2006-12-23 2007-11-23 Procédé de production de papier tissu
JP2009541802A JP2010514946A (ja) 2006-12-23 2007-11-23 ティッシュペーパーの製法
US12/432,919 US20090266500A1 (en) 2006-12-23 2009-04-30 Process for producing tissue paper

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE200610061480 DE102006061480A1 (de) 2006-12-23 2006-12-23 Verfahren zum Herstellen von Faserstoff
DE102006061480.1 2006-12-23
DE102007017061.2 2007-04-11
DE200710017061 DE102007017061A1 (de) 2007-04-11 2007-04-11 Verfahren zur Herstellung von Tissuepapier

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US12/432,919 Continuation US20090266500A1 (en) 2006-12-23 2009-04-30 Process for producing tissue paper

Publications (1)

Publication Number Publication Date
WO2008077450A1 true WO2008077450A1 (fr) 2008-07-03

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US (1) US20090266500A1 (fr)
EP (1) EP2126195A1 (fr)
JP (1) JP2010514946A (fr)
BR (1) BRPI0718883A2 (fr)
CA (1) CA2673175A1 (fr)
RU (1) RU2009128370A (fr)
WO (1) WO2008077450A1 (fr)

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WO2009015699A1 (fr) * 2007-07-31 2009-02-05 Voith Patent Gmbh Matière fibreuse lignocellulosique issue de plantes annuelles
CN102154899A (zh) * 2011-04-28 2011-08-17 永州湘江纸业有限责任公司 一种砂纸原纸及其生产方法
CN105297526A (zh) * 2015-11-03 2016-02-03 山东鲁南新材料股份有限公司 一种耐水砂纸原纸及其生产方法
WO2020229737A1 (fr) * 2019-05-15 2020-11-19 Kemira Oyj Formulation de fibres, son utilisation et son procédé de fabrication

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US8524374B2 (en) * 2011-09-21 2013-09-03 Kimberly-Clark Worldwide, Inc. Tissue Product comprising bamboo
US10577748B2 (en) 2015-04-29 2020-03-03 Essity Hygiene And Health Aktiebolag Tissue paper comprising pulp fibers originating from miscanthus and method for manufacturing the same
US11473245B2 (en) 2016-08-01 2022-10-18 Domtar Paper Company Llc Surface enhanced pulp fibers at a substrate surface
US11499269B2 (en) 2016-10-18 2022-11-15 Domtar Paper Company Llc Method for production of filler loaded surface enhanced pulp fibers
MX2019008742A (es) 2017-02-22 2019-10-02 Kimberly Clark Co Papel tisu estratificado que comprende fibras no leñosas.
WO2019152969A1 (fr) * 2018-02-05 2019-08-08 Pande Harshad Produits de papier et pâtes ayant des fibres de pâte à surface améliorée et une capacité d'absorption accrue, et leurs procédés de fabrication
CA3134990A1 (fr) 2019-03-26 2020-10-01 Domtar Paper Company, Llc Produits en papier soumis a un traitement de surface comprenant des fibres de pulpe a surface traitee par des enzymes et leurs procedes de fabrication

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Publication number Priority date Publication date Assignee Title
WO2009015699A1 (fr) * 2007-07-31 2009-02-05 Voith Patent Gmbh Matière fibreuse lignocellulosique issue de plantes annuelles
CN102154899A (zh) * 2011-04-28 2011-08-17 永州湘江纸业有限责任公司 一种砂纸原纸及其生产方法
CN105297526A (zh) * 2015-11-03 2016-02-03 山东鲁南新材料股份有限公司 一种耐水砂纸原纸及其生产方法
WO2020229737A1 (fr) * 2019-05-15 2020-11-19 Kemira Oyj Formulation de fibres, son utilisation et son procédé de fabrication

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EP2126195A1 (fr) 2009-12-02
BRPI0718883A2 (pt) 2014-02-18
RU2009128370A (ru) 2011-01-27
CA2673175A1 (fr) 2008-07-03
US20090266500A1 (en) 2009-10-29

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