[go: up one dir, main page]

WO2012004459A1 - Procédé et système pour produire une matière première pour isolation thermique - Google Patents

Procédé et système pour produire une matière première pour isolation thermique Download PDF

Info

Publication number
WO2012004459A1
WO2012004459A1 PCT/FI2011/050642 FI2011050642W WO2012004459A1 WO 2012004459 A1 WO2012004459 A1 WO 2012004459A1 FI 2011050642 W FI2011050642 W FI 2011050642W WO 2012004459 A1 WO2012004459 A1 WO 2012004459A1
Authority
WO
WIPO (PCT)
Prior art keywords
refiner
chips
raw material
pulp
refined pulp
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/FI2011/050642
Other languages
English (en)
Inventor
Taisto Tienvieri
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
UPM Kymmene Oy
Original Assignee
UPM Kymmene Oy
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
Application filed by UPM Kymmene Oy filed Critical UPM Kymmene Oy
Publication of WO2012004459A1 publication Critical patent/WO2012004459A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • D21B1/023—Cleaning wood chips or other raw materials
    • 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
    • D21B1/06—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by dry methods
    • 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
    • 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
    • D21D1/30—Disc mills
    • 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
    • D21H11/08—Mechanical or thermomechanical pulp
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21J—FIBREBOARD; MANUFACTURE OF ARTICLES FROM CELLULOSIC FIBROUS SUSPENSIONS OR FROM PAPIER-MACHE
    • D21J1/00—Fibreboard
    • D21J1/16—Special fibreboard
    • D21J1/20—Insulating board

Definitions

  • the invention relates to a method for producing fibrous raw material for thermal insulation.
  • the invention relates to a system for producing fibrous raw material for thermal insulation.
  • the invention also relates to fibrous raw material for thermal insulation.
  • Wool boards are used for thermal insulation in buildings. They are made by scattering or blowing a mixture containing dry fiber material, thermally acti- vated plastic material and additives onto a planar support (a wire or a plate) to form a layer of desired thickness, and treating it by compressing at an elevated temperature. In this way, an insulation wool board or mat is produced.
  • publications DE-10056829 and EP-1027505 discuss the manufacture of insulation material from pulp. The documents show how thermal insulation boards can be made of dry wood fibers and plastic or adhesive.
  • Document EP-1027505 presents that the fibers are made, for example, by a conventional cooking process which is also known as chemical pulping. The pulp prepared in this way is fed onto a wire to form a bandlike sheet which is dried and rolled up for storage. In the chemical process, lignin contained in the raw material is removed from the pulp. In a known way, pulp can also be prepared by mechanical refining, wherein the lignin contained in the wood raw material remains in the pulp.
  • thermomechanical pulping TMP
  • CMP chemithermomechanical pulping
  • thermomechanical pulping a lot of water is also used. Water is used to lubricate and cool the refiners and thereby to prevent the heating and burning of the wood raw material.
  • energy is used for refining wood chips in the refiners, and part of the energy is released with water evaporating in the refiners. Vapour produced in the process is utilized, among other things, in the drying and heating of the wood chips.
  • the energy consumption can be influenced, among other things, by means of the process temperatures and by heat recovery. Such energy saving solutions are described in publication US 7,540,938.
  • cellulose is organic material, it constitutes a substrate that is sus- ceptible to microbial growth when wet.
  • the pulp when pulp made by the above- described methods is applied in the manufacture of thermal insulation, the pulp must be dried before it is used.
  • the pulp is dried to a dry matter content of at least about 75%, for example by hot-air blowers, which requires a lot of energy.
  • the raw material for thermal insulation can also be made by the TMP process with a significantly smaller quantity of water, or the use of water can even be totally eliminated by selecting the raw materials and the process parameters according to the requirements of the final product on one hand and according to the properties of the raw material on the other hand.
  • the raw material for thermal insulation, obtained from the process is substantially dry, and no separate driers are needed. It is thus possible to significantly reduce the consumption of energy for unnecessary drying and to reduce the production costs.
  • an embodiment of the invention has the particular advantage that it can be implemented by existing production equipment, and that current thermomechanical processes and systems can be modified to correspond to the new process. In this way, systems can be modified at low cost, if neces- sary, for the production of raw material for thermal insulation. It is thus possible to reuse an old, redundant system in a new process, or to modify current systems for the new method and to meet the needs.
  • process parameter values are used which have not been experimented before and which fall outside the range of a normal pulping process.
  • Such parameters include, for example, the specific energy used in the refiner or refiners, and the rotational speed of the refiners.
  • the fibrous raw material used as insulation mate- rial does not need to be as finely ground as the pulp used for papermaking.
  • the application of these parameters reduces the amount of energy needed in the refiners and reduces the amount of water needed in the process, or even totally eliminates the need for water. Consequently, in the process, a reduction in the dry matter content of the raw material or pulp is avoided, and the aim is to avoid washing and the use of water in connection with the refining.
  • the advantage is also achieved that no additional energy needs to be consumed for removing added moisture.
  • the wood chips used as raw material are not washed with water, but impurities are separated by means of warm air.
  • the raw material is refined by applying relatively little energy, wherein the energy consumed is not sufficient to heat and ignite the raw material in the refiner, and it becomes unnecessary to add water into the refiner to prevent heating or a fire and thereby to remove added water from the finished pulp.
  • FIG. 1a shows a production process of prior art in a process flow chart
  • Fig. 1 b shows a production process of prior art, and the equipment
  • Fig. 2 shows the process according to a first embodiment for producing fibrous raw material, and the equipment used therein
  • Fig. 3 shows the process according to a second embodiment for producing fibrous raw material, and the equipment used therein
  • Fig. 4 shows the process according to a third embodiment for producing fibrous raw material, and the equipment used therein, and
  • Fig. 5 shows the process according to a fourth embodiment for
  • thermomechanical pulping process A conventional thermomechanical pulping process (TMP process) is shown in Figs. 1a and 1b.
  • Figure 1a shows a flow chart of the process
  • Fig. 1b also shows schematically some equipment applied at the initial end of the process.
  • Produced wood chips are stored, for example, in a silo or in an open depot.
  • the wood chips 1 are first fed into the pulping process, for example into a wood chip silo, where they are first preheated in the silo 10 at a temperature of 100°C, if this is necessary because of ambient conditions.
  • vapour produced in refining is utilized for the preheating.
  • the wood chips are washed in a washing unit 11.
  • the washing is performed with hot water, for example at 70 to 80°C, and it involves the separation of sand, metal bits and other impurities from the wood chips.
  • water 4 is supplied into the process and is heated, for example, by means of vapour produced in refining.
  • the dry matter content in the mixture of wood chips and water is typically about 3 to 4%.
  • the warm water increases and evens out the moisture of the chips.
  • Recirculated water is typically used for the washing.
  • the mixture of wood chips and water is led to dewatering, after which the chips are typically conveyed by a screw conveyor to a preheater, and the chips are preheated by vapour in a preheater 12.
  • a difference to the condi- tions prevailing in the silo 10 is that this preheating typically takes place under slight overpressure and at a temperature slightly above 100°C (for example, under an overpressure of 100 kPa and at a temperature of 120°C or lower).
  • pressure refers to an effective overpressure higher than the prevailing pressure. Because of the pressure, water vapour 2a can be released or discharged from the preheating. In other parts of the process, vapour produced in the refiners is utilized for heating and drying. By means of the heating, the moisture of the wood chips evens out and the detachment of fibers is facilitated. After sufficient preheating, the chips are typically fed by a screw conveyor to a feed screw for a refiner and further to a first refiner 13. At this stage, the dry matter content of the wood chips is typically about 20 to 27%.
  • the refiner is a single disc refiner (SD), which is a disc refiner or a conical refiner, and in which one disc rotates, another one being stationary.
  • SD single disc refiner
  • a refin- ing process for forming coarsely refined pulp is performed in the first refiner 13.
  • the chips are crushed into pin-like pieces and further into fiber bundles and single fibers.
  • vapour 2b can be separated from the coarse pulp obtained from the refiner, by means of a vapour separating device, typically a cyclone.
  • the dry matter content of the once-refined pulp is typically 24 to 40%.
  • the dry matter content is preferably low at this stage.
  • the energy consumption is monitored, for example, by monitoring the loading of the motors of the refiner.
  • the blade gap of the refiner and the method of refining influence the energy consumption of the refiner.
  • the so-called specific energy consumption and the refining conditions thus have a significant effect on the refined pulp. It is also typical to add dilution water into the refiner to influence the refining conditions and the consistency of the refined pulp.
  • Once-refined pulp is further fed into a second refiner 14, for example by blowing with vapour or by means of a screw conveyor.
  • a pressure of about 300 to 500 kPa is typically prevailing, and the temperature in the refiners is about 143 to 159°C.
  • Vapour 2c can also be separated from the refined pulp downstream of the second refiner 14, typically by means of a cyclone.
  • the fibers are normally not rectilinear, and because of this, they are subjected to removal of latency in a latency removal container 15, to which the refined pulp is typically led from the vapour separation cyclone by means of a screw conveyor.
  • the refined pulp is normally diluted to a consistency of 2 to 4% at a temperature of 70 to 80°C.
  • the pulp is led to a screening device 16, which is typically a pressure screen, whose operation is based on a pressure plate, and to a drier 17 and finally to a storage 18.
  • a screening device 16 which is typically a pressure screen, whose operation is based on a pressure plate
  • coarse and long fibers are typically removed, and the reject can be refined again and admixed to the pulp.
  • refined pulp made by the TMP process is dried separately either in a flash drier or in a drying machine.
  • a pulp mat is formed of the refined pulp, and these mats are rolled up for the time of storage.
  • the finished raw material typically has a dry matter content higher than 75%.
  • the finished refined pulp 3 is transported to an insulation material factory according to the use. Before the refined pulp stored in this way can be used as raw material for wool boards, the pulp mats must be shredded to fibers again.
  • Dilution water is used in refiners for various reasons.
  • the dilution water lubricates and cools the refiner and has an effect on the consistency of the refined pulp. It has been surprisingly found that raw material for thermal insulation can also be made with a significantly smaller amount of water, or the use of water can even be totally eliminated by selecting the raw materials and the process parameters, for example the refining conditions, on one hand according to the requirements of the final product and on the other hand according to the properties of the raw material. It is thus possible to significantly reduce the energy consumption and the production costs.
  • the method can be implemented with existing production equipment even if the use of water was totally abandoned. This is possible, for example, by selecting suitable process parameters so that one refiner used in the process is only applied for drying and for increasing the dry matter content of the raw material. It is significant that the fibrous raw material for thermal insulation does not need to be quite as fine as the raw material for paper, or even the raw material for wool boards of prior art.
  • the refiners can be used to make more coarsely refined pulp, and a larger blade gap can be applied, wherein the energy consumption of the refiners is reduced, and the use of dilution water, for example for reducing the consistency or for preventing the burning of the refined pulp, can be reduced or totally abandoned.
  • the fibrous raw material for thermal insulation can be coarser than before, and it can have a greater fiber length. Furthermore, such raw material has a substantially lower water retention capacity than pulp used as raw material for paper.
  • a low specific energy can be used with the refiners, wherein the need for cooling and lubrication is reduced or eliminated by selecting the refining conditions in a suitable way. Consequently, the fibrous raw material made of refined pulp obtained already after the refining is sufficiently dry with respect to its dry matter content, typically at least 75%, and separate driers will no longer be needed.
  • the finished raw material is obtained from the vapour separation cyclone, for example from its screw conveyor.
  • curled fibers can also be accepted as raw material, wherein there is no need for removing the latency, and there is thus no need for the latency removal container 15.
  • the new TMP process is also significantly influenced by the properties of the wood chips, particularly the dry matter content. This is taken into account in the control parameters of the process, particularly in the refining conditions.
  • the fibrous raw material for the TMP process is cellulose based raw material, for example wood, preferably softwood and particularly spruce.
  • the target is a fiber distribution having a high content of long fibers and a low content of fines. It is also possible to use hardwood, for example aspen and birch. Wood chips are made of wood by methods known as such. The wood chips have preferably been chipped and sieved in such a way that the chips sup- plied into the preheating silo 10 are substantially elongated in shape.
  • the chips used as raw material are not washed with water, wherein an unnecessary drop in the dry mat- ter content of the chips is avoided, and thereby also unnecessary heating or application of energy for removing moisture.
  • the chips are fed into a refiner under a suitable pressure, particularly under an elevated pressure, wherein the preheater 12 of prior art is not necessary.
  • the chips are refined in the first refiner by applying relatively little energy, wherein the energy applied is not sufficient to overheat or ignite the chips in the refiner, and the addition of water into the refiner is avoided.
  • a suitable coarseness of the refined pulp is achieved already in the first refiner, and the refined pulp is dried downstream of the first refiner.
  • the dry matter content of the refined pulp downstream of the first refiner is preferably more than 60%. This drying can also be performed with the second refiner.
  • the second refiner is thus used as a through drying machine.
  • the drying can be performed in the second refiner, so that it will not be necessary to modify the system of prior art and to include a separate drier.
  • refiner lines of prior art can be converted to a separate fibre board pulp line at very low invest- ment costs, or refiners of prior art can be applied in the production process of wool boards.
  • the heat released with vapour in the process is recovered. If a separate drier is used, the drying is accomplished, for example, by means of hot air.
  • the chips are blown by means of a blowing device to a separator, for example by means of hot air produced by a fan to an air density separator (ADS) 20, in which impurities, such as rocks and bits of iron, are separated from the chips.
  • ADS air density separator
  • the chips are dried by the hot air which is provided by means of a heat exchanger, in which the air is heated by means of vapour obtained from the refiners. This separation replaces the washing with water by means of corresponding equipment 11 known from the process steps of prior art (cf. Fig. 1b).
  • the dry matter content of the raw material used is significant.
  • the most common raw materials are fresh chips, with a dry matter content of about 45%, and dry chips, with a dry matter content of about 89%.
  • the chips Downstream of the air separator 20, the chips are guided to, for example, a screw conveyor and from there to a preheater 12.
  • the chips are preheated under a pressure of, for example, 80 to 150 kPa and at a temperature of 117 to 128°C.
  • vapour 2b or 2c obtained from the refiner.
  • the preheating temperature and pressure correspond to each other according to the saturated water vapour pressure.
  • the preheating pressure is 170 kPa, wherein the temperature is about 130°C, because such a selection enables the use of high energy in the refiner, wherein the once-refined pulp to be made comprises long fibers.
  • FIG. 3 A second embodiment is shown in Fig. 3.
  • preheating in the preheater 12 can be replaced by increasing the feed pressure used in the refiner 13, wherein the temperature of the refiner also rises in a way corresponding to the vapour pressure.
  • a refiner feed pressure of 220 kPa the corresponding temperature being about 136°C
  • separate preheating will not be necessary. This is not possible in all TMP processes, but in many new processes it is possible to increase the refiner feed pressure and thereby to bypass the preheating and to transfer the chips to the refiner 13 directly from the air separator 20 by applying, for example, a screw conveyor.
  • the first refiner is a single disc refiner (SD), which is a disc refiner or a conical refiner, and in which one disc rotates, the other being stationary.
  • SD disc refiner
  • the second refiner shown is also a single disc refiner.
  • the specific energy applied for the first refiner 13 is 833 kWh per ton or lower, in some cases only about 80 kWh per ton, without dilution waters and under a high pressure of 300 to 400 kPa, wherein the temperature is 143 to 151 °C, and a low blade rotation speed, for example 1000 to 1200 rpm, is applied.
  • Specific energy refers to the quantity of energy used in a refiner per ton of raw material fed into the refiner. Compared to a conventional TMP process, in which the energy consumption is in the order of 2.0 to 2.2 MWh per ton (typically divided between two refiners), the heat formation is considerably lower in this embodiment.
  • the chips are dried during the refining. No dilution water is added into the refining, because the water contained in the chips and the water of the vapour are sufficient to make the chips a good fibrous raw material for thermal insulation.
  • the chips do not burn in the blade gap, because the requirements of the fibrous raw material for thermal insulation allow the use of a large blade gap and thereby said low specific energy level of the refiner.
  • the rotational speed of the refiners is typically 1500 to 1800 rpm. In these embodi- ments, a lower rotational speed gives coarser once-refined pulp containing longer fibers and having desired properties.
  • coarse feeding or retaining blades are used in the first refiner, wherein the once-refined pulp comprises long fibers, is coarse and free from fines, in which pulp the fibers are flat. What is decisive is the dry matter content achieved at the first refiner.
  • the dry matter content of the chips being 45% and the specific energy of the first refiner being 500 kWh per ton, the dry matter content of 64% for the refined pulp can be achieved; and in a corresponding manner, the dry matter content of the chips being 89% and the specific energy of the first refiner being 83 kWh per ton, the dry matter content of 95% for the refined pulp can be achieved.
  • a screening device 21 is applied downstream of the first refiner, to screen the once-refined pulp coming from the first refiner according to the fiber size. Too large fibers are recirculated and mixed with the chips 1 to be refined again.
  • the screening device 21 is placed upstream of the cyclone, in which vapour is separated from the refined pulp.
  • the screening device is preferably a blow-off pipe screening device which is presented in publication WO 01/42556 A1 and in which coarser fibers and fiber bundles are separated out of the refined pulp by means of a high speed as well as a mixture of refined pulp and, for example, air or vapour.
  • the dry matter content of the once-refined pulp obtained from the first refiner can be higher than 60% but clearly lower than 75%, so that the once-refined pulp has to be dried further. This is, for example, a situation in which the dry matter content of the chips used as raw material is about 45%.
  • the second refiner is applied for drying once-refined pulp to desired dry matter content.
  • a lower specific energy is further applied, for example 125 to 250 kWh per ton.
  • the aim is not to refine the refined pulp but the blade of the refiner is selected so that heat develops in the fibers but the fiber is not modified and the fibre distribution is not affected. Consequently, the blades load the fiber material but no fines are released from the surface of the fibers and the fibers are not fibrillated.
  • the heat and vapour developed in this process dry the once-refined pulp in such a way that downstream of the second refiner, the dry matter content of the refined pulp is at a desired level, preferably higher than 75%.
  • the dry matter content of refined pulp downstream of the first refiner is 64%
  • the specific energy of the second refiner is 250 kWh per ton
  • the resulting dry matter content of the pulp refined by the refiners and dried is 85%.
  • a third embodiment of the process is shown in Fig. 4.
  • the raw material used in it consists of dry chips, and the coarseness and the energy level of the first refiner are set such that by selecting the refining conditions to be suitable, raw material of sufficient quality for thermal insulation is obtained already by the first refiner.
  • the refining of the chips is performed by applying only one refiner.
  • the raw material used consists of sufficiently dry chips, wherein the dry matter content is higher than 45% and the specific energy of the first refiner is low, typically lower than 800 kWh per ton, or preferably lower than 500 kWh per ton.
  • the dry matter content of the refined pulp obtained already from the first refiner is higher than 75%. This is sufficiently dry as raw material for thermal insulation.
  • Such drying can be implemented by known methods (cf. Fig.
  • the drying consumes less energy than the drying of a corresponding quantity of paper pulp.
  • the application of the second refiner as a drier corresponds to said first or second embodiment of the process.
  • the specific energy to be used in the refiners in the different embodiments will depend on the dry matter content of the raw material supplied into the process, as well as on the embodiment itself: whether once-refined pulp is dried further, or whether only one refiner is used. The specific energy of the refiner will be determined according to the raw material.
  • the vapour 2a, 2b and 2c developed in the preheating or in the refiners is utilized for heating the air needed in the air separator 20 and for drying the chips.
  • This is illustrated in Fig. 5, in which air 50 is led via a heat exchanger 51 to the air separator 20.
  • the vapours formed in the refiners are led as a heat source into the same heat exchanger. Thus, no external heating will be necessary.
  • the heat contained in the vapours 2b, 2c from the refiners can also be recovered in a preheater according to the first embodiment (see Fig. 2, pre- heater 12).
  • the heat recovery can naturally be included in the second and third embodiments (see Figs. 3 and 4). Furthermore, the heat recovery can be included in the first embodiment (see Fig. 2) by leading the vapour 2a released from the preheater 12 into the heat exchanger 50.
  • the fibrous raw material 3 for thermal insulation obtained by the above embodiments is light in colour and thereby well suited for the production of thermal insulation boards.
  • the colour is influenced by the process conditions applied and the raw material.
  • the fibrous raw material for thermal insulation obtained from the process is coarse, and its standardized freeness value (CSF, Canadian Standard Freeness) is higher than 750 ml.
  • the fiber distribution is more than 80% of so-called long fibers (+28 mesh as a measurement wire) and less than 5% of so-called fines (200 mesh as a measurement wire), measured by a Bauer McNett fractioning device (BMcN).
  • BcN Bauer McNett fractioning device
  • devices known as such including various conveyors and transfer devices, such as above-mentioned screw conveyors, belt conveyors, transfer devices based on gravity, or devices utilizing air blowing.

Landscapes

  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Mechanical Engineering (AREA)
  • Paper (AREA)

Abstract

L'invention concerne un système et un procédé de production d'une matière première fibreuse pour isolation thermique par un procédé thermomécanique. Pendant la production, des copeaux à base de cellulose (1) sont transportés depuis un stockage (10) vers l'élimination des impuretés ; les impuretés sont séparées des copeaux (20), et les copeaux purifiés sont transportés vers un premier raffineur (13) ; et les copeaux sont raffinés pour former une pâte raffinée au moins dans le premier raffineur. La teneur en matière sèche de la pâte raffinée en aval du premier raffineur est de préférence d'au moins 60 %. Dans un exemple, la matière première finie a un indice d'égouttage, par mesure du CSF (indice d'égouttage Canadien Standard), supérieur à 750 ml, et une teneur en fibres longues, par mesure du BMcN (+28 mesh), supérieure à 85 %, et une teneur en fines (200 mesh) inférieure à 5 %.
PCT/FI2011/050642 2010-07-09 2011-07-07 Procédé et système pour produire une matière première pour isolation thermique Ceased WO2012004459A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20105786 2010-07-09
FI20105786A FI20105786L (fi) 2010-07-09 2010-07-09 Menetelmä ja järjestelmä lämmöneristeen raaka-aineen valmistamiseksi

Publications (1)

Publication Number Publication Date
WO2012004459A1 true WO2012004459A1 (fr) 2012-01-12

Family

ID=42555482

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI2011/050642 Ceased WO2012004459A1 (fr) 2010-07-09 2011-07-07 Procédé et système pour produire une matière première pour isolation thermique

Country Status (2)

Country Link
FI (1) FI20105786L (fr)
WO (1) WO2012004459A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018234097A1 (fr) * 2017-06-20 2018-12-27 Basf Se Procédé d'augmentation du débit et/ou de diminution de l'utilisation d'énergie d'un processus de réduction en pâte
CN110552227A (zh) * 2019-10-09 2019-12-10 黄伟 一种麦草秸秆制浆造纸预处理系统
WO2023177279A1 (fr) * 2022-03-18 2023-09-21 Atvasināta Publiska Persona Latvijas Valsts Koksnes Ķīmijas Institūts Procédé de production d'un matériau d'isolation thermique en vrac à base de lignocellulose
EP4385695A3 (fr) * 2022-11-23 2025-05-21 UPM-Kymmene Corporation Pulpe thermomécanique

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB117086A (en) * 1915-12-23 1919-05-22 Jan Carel Van Wessem Improvements in and relating to the Manufacture of Fibrous Pulp suitable for Paper-Making from Saw-dust and Wood-Waste.
US2872337A (en) * 1953-12-30 1959-02-03 Weyerhaeuser Timber Co Method of coating a felted fibrous mat
US4012279A (en) * 1973-12-28 1977-03-15 Stig Selander Process of producing pulp, for manufacture of fiberboard, in a closed backwater system
US4407771A (en) * 1982-04-26 1983-10-04 The Celotex Corporation Blow line addition of isocyanate binder in fiberboard manufacture
US4457804A (en) * 1976-03-19 1984-07-03 Reinhall Rolf Bertil Apparatus for producing fiber pulp from fibrous lignocellulose containing material
EP0572388B1 (fr) * 1990-02-13 1995-05-10 Mölnlycke AB Procede de fabrication de pate chimiothermomecanique

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB117086A (en) * 1915-12-23 1919-05-22 Jan Carel Van Wessem Improvements in and relating to the Manufacture of Fibrous Pulp suitable for Paper-Making from Saw-dust and Wood-Waste.
US2872337A (en) * 1953-12-30 1959-02-03 Weyerhaeuser Timber Co Method of coating a felted fibrous mat
US4012279A (en) * 1973-12-28 1977-03-15 Stig Selander Process of producing pulp, for manufacture of fiberboard, in a closed backwater system
US4457804A (en) * 1976-03-19 1984-07-03 Reinhall Rolf Bertil Apparatus for producing fiber pulp from fibrous lignocellulose containing material
US4407771A (en) * 1982-04-26 1983-10-04 The Celotex Corporation Blow line addition of isocyanate binder in fiberboard manufacture
EP0572388B1 (fr) * 1990-02-13 1995-05-10 Mölnlycke AB Procede de fabrication de pate chimiothermomecanique

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018234097A1 (fr) * 2017-06-20 2018-12-27 Basf Se Procédé d'augmentation du débit et/ou de diminution de l'utilisation d'énergie d'un processus de réduction en pâte
CN110770391A (zh) * 2017-06-20 2020-02-07 巴斯夫欧洲公司 提高制浆工艺的吞吐量和/或降低能量使用的方法
CN110770391B (zh) * 2017-06-20 2022-02-11 巴斯夫欧洲公司 提高制浆工艺的吞吐量和/或降低能量使用的方法
US11624153B2 (en) 2017-06-20 2023-04-11 Basf Se Method of increasing the throughput and/or decreasing energy usage of a pulping process
CN110552227A (zh) * 2019-10-09 2019-12-10 黄伟 一种麦草秸秆制浆造纸预处理系统
WO2023177279A1 (fr) * 2022-03-18 2023-09-21 Atvasināta Publiska Persona Latvijas Valsts Koksnes Ķīmijas Institūts Procédé de production d'un matériau d'isolation thermique en vrac à base de lignocellulose
EP4385695A3 (fr) * 2022-11-23 2025-05-21 UPM-Kymmene Corporation Pulpe thermomécanique

Also Published As

Publication number Publication date
FI20105786A7 (fi) 2012-01-10
FI20105786L (fi) 2012-01-10
FI20105786A0 (fi) 2010-07-09

Similar Documents

Publication Publication Date Title
CN108252137B (zh) 高耐破环保牛皮箱板纸的制备工艺
CA2297958C (fr) Procede de pretraitement de matieres contenant des fibres de lignocellulose utile pour procede de fabrication de pate a papier
RU2128258C1 (ru) Способ получения технической целлюлозы из содержащего лигноцеллюлозу волокнистого материала
CN105780570B (zh) 废纸制浆造纸生产方法
RU2581995C2 (ru) Способ получения пульпы с высокой садкостью
JP3085936B2 (ja) ペーパーウェブの製造方法
WO2012004459A1 (fr) Procédé et système pour produire une matière première pour isolation thermique
EP2519689B1 (fr) Procede pour fabriquer un produit contenant des fibres
CN112048928A (zh) 一种干法废纸浆及其制备方法
CA2909030C (fr) Procede de production de biocarburant et utilisation du biocarburant
FI122243B (fi) Menetelmä ja järjestelmä puuhakkeen tai massakuitujen jauhamiseksi
US3245868A (en) Continuous process for the recovery of paper broke containing a wet strength resin
US4372810A (en) Method and device for manufacturing mechanical pulp
CN105729610A (zh) 一种纤维板生产工艺
JP5825125B2 (ja) 古紙パルプの製造方法
US5536371A (en) Papermaking sludge recovery process and apparatus
JP2000343527A (ja) 故紙木質合成粉及びその製造方法並びに装置
US4221630A (en) Wet method of preparing fiberboard products in a substantially closed and balanced white water system
Heinemann et al. Pulp and paper
CN103046417B (zh) 一种低能耗涂布白纸板制浆工艺
US20230118469A1 (en) Method and System for Producing Recycled Fibers for MDF or HDF Production
FI81642B (fi) Matarsystem foer en former vid en torrpappersmaskin.
CN115087776A (zh) 再生芳纶纸的制造方法
EP4385695A2 (fr) Pulpe thermomécanique
US4406734A (en) Method for the manufacture of mechanical pulp

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11803199

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 11803199

Country of ref document: EP

Kind code of ref document: A1