WO2024133439A1 - Procédé de production de ht-ctmp à haute résistance à la traction - Google Patents

Procédé de production de ht-ctmp à haute résistance à la traction Download PDF

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Publication number
WO2024133439A1
WO2024133439A1 PCT/EP2023/086916 EP2023086916W WO2024133439A1 WO 2024133439 A1 WO2024133439 A1 WO 2024133439A1 EP 2023086916 W EP2023086916 W EP 2023086916W WO 2024133439 A1 WO2024133439 A1 WO 2024133439A1
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chips
pulp
bleached
ctmp
iso
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PCT/EP2023/086916
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English (en)
Inventor
Thomas Lindstedt
Thomas Granfeldt
Per Engstrand
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Billerud Aktiebolag (Publ)
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Publication of WO2024133439A1 publication Critical patent/WO2024133439A1/fr

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    • 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
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/02—Pretreatment of the raw materials by chemical or physical means
    • D21B1/021—Pretreatment of the raw materials by chemical or physical means by chemical means
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • 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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
    • 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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/06—Pretreatment of the finely-divided materials before digesting with alkaline reacting compounds
    • 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
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21D—TREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D1/00—Methods of beating or refining; Beaters of the Hollander type
    • D21D1/20—Methods of refining

Definitions

  • the present disclosure relates to the production of bleached high temperature chemithermomechanical pulp (HT-CTMP).
  • HT-CTMP bleached high temperature chemithermomechanical pulp
  • CTMP Chemithermomechancial pulp
  • HT-CTMP high temperature CTMP
  • the present inventors have realized that a bleached HT-CTMP having particularly good fiber bonding ability and thereby a high tensile strength can be produced if the process comprises low-consistency refining subsequent to the bleaching of the pulp.
  • a method for producing bleached HT-CTMP comprising the steps: a) providing wood chips comprising softwood, hardwood or a mixture thereof; b) impregnating the wood chips with an impregnation liquid comprising NaOH and/or Na 2 SO 3 to obtain impregnated chips; c) transferring the impregnated chips to a heating zone without compressing the impregnated chips; d) heating the impregnated chips in the heating zone with steam having a temperature of above 140 °C, such as at least 150 °C, such as at least 160 °C, to obtain pre-treated chips; e) defibrating the pre-treated chips to obtain a pulp; f) bleaching the pulp to obtain a bleached pulp; and g) refining the bleached pulp at a consistency of 3-8 wt. %.
  • a bleached HT-CTMP having high tensile strength may be obtained.
  • the bleaching in step f) may be a two-step process.
  • the first and the second bleaching step may be performed at different consistencies such as the first step occurring at a medium consistency of 10- 12 wt.% and the second step occurring at a high consistency of 30-35 wt. %.
  • the two- step bleaching processes facilitates the bleaching of the pulp to a high brightness.
  • all bleaching steps are performed prior to the refining in step g).
  • the defibration of the treated chips in step e) may occur at a solid content of 40-50 wt.%.
  • a more effective defibration can be obtained in step e).
  • the pressure during defibration in step e) may be 6-12 bar.
  • the pressure may be lower at the beginning of the defibration and then increase throughout the defibration step.
  • the high pressure during step e) may facilitate the defibration.
  • the low consistency (LC) refining in step g) may be performed using multiple parallel LC refiners.
  • the consistency in step g) is preferably 3-7 wt.%, such as 4-6 wt.%.
  • An advantage to using low consistencies during step g) is that the refining step may than be less expensive.
  • the method may further comprise dewatering of the pulp prior to bleaching of step f).
  • the dewatering may improve the bleaching procedure. Due to the energy-efficiency of the refining of step g), the freeness prior to bleaching may be kept relatively high (by a relatively low degree of defibration in step e) ), which means that the pulp is relatively easily dewatered.
  • the method of the first aspect enables energy efficient dewatering prior to the bleaching of step f).
  • the pulp obtained in step e) may have a Canadian Standard Freeness (CSF) of 650-750 ml, such as 690-750 ml as measured according to ISO 5267-2:2001 after disintegration according to ISO 5263-3:2004.
  • CSF Canadian Standard Freeness
  • the impregnation liquid which is aqueous, comprises NaOH and/or Na2SO3.
  • the temperature of the impregnation liquid is preferably at least 7O°C, such as 7O°C-99°C, such as 8o°C-99°C. At such a relatively high temperature, the viscosity of the impregnation liquid is lower, which facilitates the absorption thereof.
  • the method may further comprise pre-steaming of the wood chips prior to the impregnation in step b).
  • the pre-steaming may remove air present within the chips and condition the chips, thereby improving the following impregnation.
  • the wood chips may further be feed to the impregnation liquid via a plug screw wherein the wood chips are compressed.
  • the compression may enable quick expansion once the wood chips come in contact with the impregnation liquid and hence improve the impregnation.
  • the residence time in step b) is preferably no more than two minutes.
  • a bleached HT-CTMP has a tensile index measured according to ISO 1924-3:2005 after sheet forming according to ISO 5269-1:2005 of at least 45 Nm/g, such as at least 50 Nm/g, such as at least 55 Nm/g.
  • An upper limit for the tensile index may be 70 Nm/g. For higher bulk values, the upper limit may be 60 Nm/g.
  • the bleached HT-CTMP may have a bulk of at least 1.25 cm3/g, such as at least 1.35 cm3/g, such as at least 1.60 cm3/g.
  • An upper limit for the bulk may be 2.00 cm3/g.
  • the upper limit may be 1.70 cm3/g.
  • Bulk is measured according to ISO 534:2011 after sheet forming according to ISO 5269-1:2005.
  • four different HT-CTMPs having a bulk in the range of 1.60-2.00 cm3/g and a tensile index in the range of 45-60 Nm/g have been prepared.
  • four different HT-CTMPs having a bulk in the range of 1.25-1.70 cm3/g and a tensile index in the range of 55-70 Nm/g have been prepared.
  • the CSF of the bleached HT-CTMP may be 200-460 ml as measured according to ISO 5267-2:2001 after disintegration according to ISO 5263-3:2004.
  • the bleached HT-CTMP may comprise at least 95 dry wt.%, such as at least 100 dry wt.%, hardwood fibres, such as birch fibres.
  • High temperature chemithermomechanical pulp is defined as CTMP produced according to a process in which impregnated chips are heated with steam having a temperature of above 140 °C, such as at least 150 °C, such as at least 160 °C.
  • An upper limit may be 190 °C.
  • FIG 1 schematically illustrates a system for producing bleached HT-CTMP.
  • FIG. 1 schematically illustrates a continuation of the system in Fig 1 designed for producing market HT-CTMP.
  • FIG. 3 schematically illustrates a continuation of the system in Fig 1 designed to produce market HT-CTMP and supply an adjacent board-making machine with HT-CTMP.
  • Fig 4a shows the bulk as a function of refining energy input for bleached pulp 4 and non-bleached pulp 4*.
  • the series starting with the filled triangle represents the unbleached pulp and the series starting with the unfilled triangle represents the bleached pulp.
  • Fig 4b shows the bulk as a function of refining energy input for bleached pulp 6 and non-bleached 6*.
  • the series starting with the filled diamond represents the unbleached pulp and the series starting with the unfilled diamond represents the bleached pulp.
  • Fig 5a shows the tensile index as a function of refining energy input for bleached pulp 4 and non-bleached pulp 4*.
  • the series starting with the filled triangle represents the unbleached pulp and the series starting with the unfilled triangle represents the bleached pulp.
  • Fig 5b shows the tensile index as a function of refining energy input for bleached pulp 6 and non-bleached 6*.
  • the series starting with the filled diamond represents the unbleached pulp and the series starting with the unfilled diamond represents the bleached pulp.
  • Fig 6a shows the relationship between bulk and tensile index for bleached pulp 4 and non-bleached pulp 4*.
  • the series starting with the filled triangle represents the unbleached pulp and the series starting with the unfilled triangle represents the bleached pulp.
  • Fig 6b shows the relationship between bulk and tensile index for bleached pulp 6 and non-bleached 6*.
  • the series starting with the filled diamond represents the unbleached pulp and the series starting with the unfilled diamond represents the bleached pulp.
  • Fig 7 shows the relationship between bulk and tensile index of the tested bleached pulps.
  • Fig 8 shows the relationship between tensile index and CSF of the tested bleached pulps.
  • the present disclosure relates to a production method of a HT-CTMP having improved fiber bonding ability and thereby improved properties such as tensile strength.
  • the HT-CTMP of the present disclosure overcomes the shortcomings associated with HT-CTMP and opens up a variety of applications in which CTMP or HT-CTMP previously could not be used.
  • the properties of the obtained HT-CTMP may even be similar to Kraft pulp.
  • a HT-CTMP of similar properties as Kraft pulp is advantageous since HT-CTMP is produced in a much higher yield than Kraft pulp.
  • a HT-CTMP process typically gives rise to a high yield pulp having high bulk and relatively low tensile strength.
  • the low tensile strength is due to poor fiber bonding.
  • the fibers in HT-CTMP have a smooth surface as they are “coated” with lignin, which gives the poor fiber bonding ability.
  • the smooth fibers are difficult to refine and require a high amount of refining energy to develop a relatively low degree of tensile strength.
  • the present inventors have realized that by bleaching the pulp prior to a refining step at low consistency, a more efficient refining may be obtained and hence a higher tensile strength may be developed at a lower refining energy consumption.
  • the bleaching reacts with the lignin coated on the fibers and increases the surface roughness of the fibers enabling a better refining.
  • the energy requirement for refining the pulp to a certain freeness may be three times smaller for the bleached pulp compared to the non-bleached pulp.
  • Hardwood such as birch, maple and aspen as well as softwood such as spruce and pine may be used to produce the HT-CTMP of the present disclosure. It is further possible to modify the final properties of the HT-CTMP by using mixtures of hardwood and softwood e.g. to obtain an optimal relationship between long and short fibers.
  • Figures 1-3 illustrate exemplary embodiments of a system for producing bleached HT-CTMP.
  • a chipper 101 may be used to prepare chips from wood.
  • chips In case of hardwood, in particular maple, it is preferable to prepare chips that are relatively short, such as ⁇ 20 mm, to aid impregnation.
  • Softwood chips are generally easier to impregnate and can hence be longer, such as 22-24 mm.
  • the settings of a conventional wood chipper can be adjusted to achieve such lengths.
  • the thickness of the chips is proportional to its length, i.e. the shorter the chips are, the thinner they will be.
  • the chips from the chipper 101 are typically stored in at least one silo 102. When different types of wood are mixed in the system, there is typically one silo for each type of wood, such as one hardwood chips silo 102a and one softwood chips silo 102b. When there is more than one type of wood chips, a chips mixing system 103 is preferably arranged downstream of the silos 102a, 102b. [0042] The chips from the chips mixing system 103 are optionally stored in a maturation silo 104 for a period of at least 24 h (typically about 72 h). A typical temperature in the maturation silo 104 is 6o°C, which can be achieved by feeding low-pressure steam into the maturation silo 104. The treatment of the chips in the maturation silo 104 degrades triglycerides. The degradation products can then be more easily extracted in downstream process steps.
  • Another option is to design the chip silos 102a, 102b as maturation silos.
  • a benefit of this option is that the maturation time and temperature can be individually adapted to the respective wood types.
  • the chips Before being impregnated, the chips may be washed in a chip washing arrangement 106. Upstream the chip washing arrangement 106, a conditioning device 105 may be arranged.
  • the conditioning device 105 is typically a chip steaming bin.
  • the purpose of the conditioning device 105 is to provide chips of fairly constant temperature.
  • the conditioning device 105 may also, to some extent, reduce variations in the moisture content of the chips.
  • the conditioning device 105 may be used to melt the ice on the chips, which facilitates the downstream washing and processing.
  • the conditioning device 105 maybe particularly advantageous when there is no upstream maturation silo.
  • the chips are typically soaked and agitated in water and then dewatered. Dirt and gravel are removed in the chip washing arrangement 106.
  • the washed and dewatered chips are then steamed in a pre-steaming bin 107.
  • the residence time of the chips in the pre-steaming bin 107 is typically at least 10 min such as 15-20 min.
  • the pre-steaming of the chips removes air from the chips and replaces it with steam leading to an improved impregnation downstream.
  • the steamed chips from the pre-steaming bin 107 are subjected to impregnation in one or two steps.
  • a plug screw 108 may feed the steamed chips into a reactor 109.
  • the steamed chips which were compressed in the plug screw 108, expand in a bath of aqueous impregnation liquid no in the reactor 109. During the expansion, the chips absorb impregnation liquid.
  • the temperature of the impregnation liquid is preferably 8o°C-99°C.
  • the expanded and impregnated chips are lifted from the bath of impregnation liquid 110 by means of a transport screw 111 and are then allowed to fall over an edge 112 and into a heating zone 113 of the reactor
  • the impregnation liquid comprises NaOH and/or Na 2 SO 3 .
  • a plug screw 115 may feed the steamed chips into a pre-impregnation chamber 116.
  • the steamed chips which were compressed in the plug screw 115, expands in a bath of pre-impregnation liquid 117 in the pre-impregnation chamber 116. During the expansion, the chips absorb preimpregnation liquid.
  • the temperature of the pre-impregnation liquid is preferably 8O°C-99°C.
  • the pre-impregnation liquid is water that may comprise NaOH and optionally Na 2 SO 3 .
  • the expanded and impregnated chips are lifted from the bath of pre-impregnation liquid 117 by means of a transport screw 118.
  • a plug screw 119 may then feed the pre-impregnated chips into a reactor 120.
  • the pre-impregnated chips which were compressed in the plug screw 119, expand in a bath of impregnation liquid 121 in the reactor 120.
  • the chips absorb impregnation liquid, which comprises NaOH and/or Na 2 SO 3 and preferably has a temperature of 8O°C-99°C.
  • the expanded and impregnated chips are lifted from the bath of impregnation liquid 121 by means of a transport screw 122 and are then allowed to fall over an edge 123 and into a heating zone 124 of the reactor 120, in which they are heated by steam having a temperature above 14O°C.
  • the transferring of the impregnated chips from the bath of impregnation liquid 121 to the heating zone 124 occurs without any compression of the chips.
  • the impregnation liquid is thereby not pressed out of the chips prior to reaching the heating zone 124.
  • the chips treated in the reactor 120 are transferred to the chips defibrator 114 without flashing off any steam on the way.
  • the impregnation liquid in both the one-step and the two-step impregnation, may comprise NaOH, Na 2 SO 3 or mixtures thereof.
  • the NaOH softens the wood chips by modification of the carbohydrates such as hemicellulose and is typically used more for hardwood.
  • the Na 2 SO 3 softens the wood by modifying the lignin by sulphonation making it more hydrophilic and is typically used more for softwood.
  • the impregnation liquid may be adjusted as to optimize the softening of the chips which may occur differently depending on the wood composition.
  • the dry matter content is 40-50 wt. % such as 45-50 wt.% (in case there is no plug screw between the heating zone 124 and the chips defibrator 114, the dry matter content may however be as low as 30%). It is advantageous for the solid content to be high in order to use as much of the defibration energy for defibrating rather than vaporizing the water in the impregnated chips. However, too high solid content, >50 wt.%, may lead to burnt fibers.
  • the pressure at the beginning of the defibration step is typically 6-7 bar and may increase to 10-12 bar during the duration of the defibration step.
  • the defibrated chips from the chips defibrator 114 may be subjected to flashing in a steam separator 125 and then pulped in a first pulper 126.
  • the pulp from the first pulper 126 may then be treated in a first dewatering press 127.
  • the pressate from the first dewatering press 127 contains extractives (and dissolved wood substances and residual chemicals) that are unwanted in the final HT-CTMP product. Separation of extractives by pressing in this position is advantageous since the pulp still has very high freeness (typically >650 ml or even >700 ml) and is thus easily dewatered.
  • Limiting the residence time in the first pulper 126 to below 10 min (typically about 3 min) is advantageous since it limits the time available for the extractives to be re-adsorbed onto the fibers before the first dewatering press 127.
  • the pulp from the first dewatering press 127 is subjected to middle consistency (MC) bleaching in a MC bleach tower 128 using unreacted peroxide from a downstream high consistency (HC) bleaching.
  • Fresh alkali such as NaOH may be added to the MC bleaching if necessary.
  • MC means 10-12 wt.%.
  • the MC-bleached pulp may be dewatered in a second dewatering press 129 also producing a pressate.
  • the pulp from the second dewatering press is subjected to high consistency (HC) bleaching in a HC bleach tower 130 using fresh peroxide and alkali. It is advantageous that the hydrogen peroxide is present in excess compared to the alkali during the entire bleaching process in order to obtain a high brightness.
  • the HC-bleached fibers from the HC bleach tower 130 may be pulped in a second pulper 131 (residence time is preferably ⁇ 10 min, such as about 3 min) to produce a pulp having a consistency of about 3-8 wt.%.
  • This pulp is then subjected to low consistency (LC) refining in LC refiners 132.
  • the LC refining may be performed in multiple stages, typically three LC refiners are used.
  • a third dewatering press 133 may then separate a third pressate from the LC-refined pulp.
  • the fibers from the third dewatering press 133 may be pulped in a third pulper 134 (residence time is preferably ⁇ 10 min, such as about 3 min) to produce a pulp having a consistency of 2- 4 wt.%.
  • Screens 135 may then be used to separate a reject from the pulp from the third pulper 134.
  • the separated reject is collected in a reject tank 136.
  • the pulp from the screens 135 are cleaned in cyclones 137 to provide cleaned pulp and acsecond reject that is collected in a second reject tank 138.
  • the cleaned pulp is then filtered in a disc filter 139 and collected in a MC tower 140.
  • a fourth dewatering press 141 produces dewatered fibers and a fourth pressate.
  • the dewatered fibers are led to an arrangement for fiber treatment and shredding 142 and then to a flash drying arrangement 143.
  • bales of the dried fibers from the flash drying arrangement 143 are formed in a baling arrangement 144.
  • the pulp from the screens 135 is filtered in a disc filter 145 and treated in a fourth dewatering press 146 such that a fourth pressate and an MC pulp are obtained.
  • the MC pulp is collected in a MC tower 147.
  • a fifth dewatering press 148 produces dewatered fibers and a fifth pressate from the MC pulp from the MC tower 147.
  • the dewatered fibers are led to an arrangement for fiber treatment and shredding 149 and then to a flash drying arrangement 150.
  • bales of the dried fibers from the flash drying arrangement 150 are formed in a baling arrangement 151.
  • MC pulp from the MC tower 147 is led to a board-making machine.
  • a bleached HT-CTMP having a tensile index of at least 45 Nm/g, such as at least 50 Nm/g, such as at least 55 Nm/g can be obtained according to the present disclosure.
  • An upper limit for the tensile index may be 70 Nm/g. For higher bulk values, the upper limit may be 60 Nm/g.
  • the tensile index is measured according to ISO 1924-3:2005 after sheet forming according to ISO 5269-1:2005.
  • the bleached HT-CTMP may further have a bulk of at least 1.25 cm3/g, such as 1.35 cm3/g, such as at least 1.60 cm3/g.
  • An upper limit for the bulk may be 2.00 cm3/g. For higher tensile index values, the upper limit may be 1.70 cm3/g.
  • the bulk is measured according to ISO 534:2011 after sheet forming according to ISO 5269-1:2005.
  • HT-CTMPs having a bulk in the range of 1.60-2.00 g/cm3 and a tensile index in the range of 45-60 Nm/g can be obtained.
  • Another example of the present disclosure is HT-CTMPs having a bulk in the range of 1.25-1.70 g/cm3 and a tensile index in the range of 55-70 Nm/g.
  • the bleached HT-CTMP may have a CSF in the range of 200-460 ml as measured according to ISO 5267-2:2001 after disintegration according to ISO 5263-3:2004.
  • Pilot tests were performed using birch and spruce as raw materials in dry weight ratios of 100/0, 70/30 and 55/45.
  • the raw materials were treated in a chipper to obtain chips which were thereafter screened using a vibrating screen equipped with hole-plates having a diameter of 35 mm and 8 mm.
  • the screening was mainly performed in order to remove oversized chips and sawdust.
  • the birch and spruce chips were then mixed together in different ratios.
  • the mixed chips were heated for about 15 min in an atmospheric presteaming bin to a temperature of at least 90 °C using steam. After the pre-steaming, the chips were transferred to a reactor via a plug screw. The chips were compressed in the plug screw which had a compression rate of 1:3.
  • the reactor comprised an impregnator (bath of impregnation liquid) and a heating zone, wherein a vertical twin-screw impregnator was used.
  • the pre-steamed chips and the impregnation liquid were continuously feed to the impregnator at separate inlets.
  • the impregnation liquid was feed into the impregnator at a flow rate corresponding to 0.5 m3/tonne fiber.
  • NaOH and Na 2 SO 3 were used as the impregnation chemicals at different concentrations, see table 1.
  • dietylenetriamine penta acetic acid (DTPA) was added as a complexing agent in an amount of 2 kg/tonne fiber.
  • the impregnation occurred instantaneously as the compressed chips expanded in the impregnation liquid.
  • the impregnation liquid had a temperature of ⁇ 4O°C and the liquid uptake was 2.2 m3/tonne fiber.
  • the impregnated chips were transferred to the heating zone of the reactor via the twin-screw.
  • the impregnated chips were heating at a saturated steam pressure corresponding to a temperature of 140 °C or 165 °C for 1-2 min.
  • the pre-treated chips were then transferred to defibration.
  • the chips were defibrated using a 20-inch OVP 20 flat disk defibrator supplied with standard 5811 Valmet pilot refiner plates. The defibrator was run at 1500 rpm.
  • the defibrated pulp was dewatered and then bleached in a laboratory procedure. NaOH and hydrogen peroxide (H2O2) were used as bleaching chemicals at different ratios, see Table 1. After the bleaching, the bleached pulp was refined at a consistency of 4-6 wt.% in a laboratory LC refiner at different refining energies.
  • H2O2 hydrogen peroxide
  • Table 1 The recipes for the different HT-CTMP produced in the pilot test.
  • the tensile index was determined according to ISO 1924-3:2005 after sheet formation according to ISO 5269-1:2005.
  • the bulk was determined according to ISO 534:2011 after sheet formatting according to ISO 5269-1:2005 and the CSF was determined according to ISO 5267-2:2001 after disintegration according to ISO 5263-3:2004.
  • figures 5a-5b also show a steeper increase in tensile index with increasing refining energy input for the bleached pulps (pulp 4 and 6) compared to the unbleached pulps (pulps 4* and 6*) (as can be observed by the steeper incline of the plotted values for the bleached pulps 4 and 6).
  • the LC refining is much more efficient on bleached pulp compared to unbleached pulp.
  • the steeper increase further indicates that higher tensile indexes can be obtained by bleaching prior to LC refining.
  • Figure 7 shows the relationship between bulk and tensile index, bulk/tensile index curve, at different refining energy inputs for the tested bleached pulps (the pulps were refined after bleaching), see table 1. All the tested pulps showed the same trend, a decrease in bulk and an increase in tensile index with increased refining energy input. The bulk/tensile curve was affected by the wood composition, impregnation and bleaching chemistry as can be observed in figure 7. [0075] Figure 7, hence, shows that a HT-CTMP with a wide variety of ratios between tensile index and bulk can be obtained by varying the raw materials, impregnation chemistry and bleaching chemistry.
  • pulp 1 comprising 100 % birch had a tensile index of 66.4 Nm/g and a bulk of 1.26 cm3/g at a specific refining energy input.
  • pulp 6 which had a tensile index of 45.2 Nm/g and a bulk of 1.92 cm3/g at a specific refining energy input.
  • Figure 8 shows the relationship between tensile index and CSF at different refining energy inputs for the tested bleached pulps.
  • the tensile index of the tested pulps increases with decreased CSF (increased refining energy input).
  • pulp 6 may, at a certain refining energy input, have a tensile index of 58.5 Nm/g and a CSF or 277 ml.
  • pulp 6 may have a tensile index of 45.2 Nm/g and a CSF of 460 ml.

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Abstract

L'invention concerne une pâte chimicothermomécanique haute température blanchie et un procédé de production de ladite HT-CTMP comprenant les étapes consistant à : a) fournir des copeaux de bois comprenant du bois tendre, du bois dur ou des mélanges de ceux-ci ; b) imprégner les copeaux de bois avec un liquide d'imprégnation comprenant du NaOH et/ou du Na2SO3 pour obtenir des copeaux imprégnés ; c) transférer les copeaux imprégnés vers une zone de chauffage sans comprimer les copeaux imprégnés ; d) chauffer les copeaux imprégnés dans la zone de chauffage avec de la vapeur ayant une température supérieure à 140°C, par exemple au moins 150°C, par exemple au moins 160°C, pour obtenir des copeaux pré-traités ; e) défibrer les copeaux pré-traités pour obtenir une pâte ; f) blanchir la pâte pour obtenir une pâte blanchie ; et g) raffiner la pâte blanchie à une consistance de 3 à 8% en poids pour obtenir la HT-CTMP blanchie.
PCT/EP2023/086916 2022-12-21 2023-12-20 Procédé de production de ht-ctmp à haute résistance à la traction WO2024133439A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP22215619.2 2022-12-21
EP22215619.2A EP4389964A1 (fr) 2022-12-21 2022-12-21 Procédé de production de ht-ctmp ayant une résistance à la traction élevée

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WO2024133439A1 true WO2024133439A1 (fr) 2024-06-27

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4486267A (en) * 1983-11-14 1984-12-04 Mead Corporation Chemithermomechanical pulping process employing separate alkali and sulfite treatments
US4798651A (en) * 1987-03-24 1989-01-17 Stake Technology Ltd. Process for preparing pulp for paper making
WO2003000982A1 (fr) * 2001-06-21 2003-01-03 Holmen Aktiebolag Procede de production de pate thermomecanique (ptm) blanchie ou de pate chimico-thermomecanique (pctm) blanchie

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4486267A (en) * 1983-11-14 1984-12-04 Mead Corporation Chemithermomechanical pulping process employing separate alkali and sulfite treatments
US4798651A (en) * 1987-03-24 1989-01-17 Stake Technology Ltd. Process for preparing pulp for paper making
WO2003000982A1 (fr) * 2001-06-21 2003-01-03 Holmen Aktiebolag Procede de production de pate thermomecanique (ptm) blanchie ou de pate chimico-thermomecanique (pctm) blanchie

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EP4389964A1 (fr) 2024-06-26

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