• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
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  • 优先权
    • 专利摘要:
    Method and apparatus for minimizing steam consumption in the production of pulp used for the manufacture of fiberboard and the like, in which chips of cellulosic material are ground in a defibrator or refiner in an environment of saturated steam above 100 DEG C and corresponding steam pressures. The chips are normally presteamed with atmospheric steam separated from the pulp at the discharge end of the defibrating process to a temperature between 90 DEG C and 100 DEG C and compressed and dewatered to a dryness of at least 50% and then passed into a preheater which forms part of the defibrating or refining apparatus, where the compressed and dewatered chips are heated to the desired defibrating or refining temperature, usually ranging between 130 DEG C and 200 DEG C, by a portion of the high-temperature high-pressure steam generated by the heat of friction in the grinding space of the defibrator, which portion, upon discharge from the grinding housing, is separated from the pulp and recirculated under increased pressure above the discharge pressure. If the other portion of the discharged atmospheric steam, upon separation from the pulp, should not have sufficient heat content to presteam the raw chips to the desired temperature, fresh pressurized steam may be added to the recirculated portion of the steam to impart to the other portion of the discharged steam the required capacity.
    公开号:SU850017A3
    申请号:SU772509104
    申请日:1977-08-05
    公开日:1981-07-23
    发明作者:Седерквист Карл；Селандер Стиг；Марешаль Бернар
    申请人:Изель С.А. (Фирма)；
    IPC主号:
    专利说明:

    Union of Soviet
    With socialist
    Republics
    DESCRIBED AND E
    Inventions
    TO THE PATENT
    (11) 850017 (61) Additional to the patent - (22) Stated 05.08.77 (21) 2509104 / 28-12 (23) Priority - (32) 06.08.76 (31) 760884 7-5 (33) Sweden
    Published 2307.81 Bulletin number 27
    Date of publication of the description 07.25.81 (72) Authors of the invention
    Foreigners
    Karl Soderquist, Stig Selander and Bernard Marechal (France) (51) M. Cl. 3
    21 V 1/12 (53) UDC 676.1.021.
    .7 (088.8)
    (71) Applicant
    Foreign company Isel S.A. (France)
    (54) METHOD FOR PRODUCING THERMOMECHANICAL WOOD MASS FOR PRODUCING FIBROUS BOARDS AND DEVICE FOR IMPLEMENTING THE METHOD
    The invention relates to the production of thermomechanical pulp for the manufacture of fiber boards.
    A known method of producing thermomechanical pulp for the manufacture of fiber boards by heating wood chips in a heater, steaming it in a defibrator-heater, feeding compressed wood chips, up to 50% dryness into a defibrator, grinding it in a defibrator at a temperature of 130200 ° C in an atmosphere of saturated steam under pressure and removal of pulp together with steam from the grinding zone.
    A device for implementing this method is also known, comprising a defibrator-heater; screw press, __ defibrator and pulp collector fl}.
    The disadvantage of this method is the significant loss of thermal energy for grinding. 25
    The purpose of the invention is to reduce consumption, steam.
    The goal is achieved by separating part of the steam discharged together with the pulp from the grinding zone, increasing its pressure to a pressure higher than the pressure in the defibrator and directing the steam to steaming the chips.
    Fresh steam is added to the part of the steam aimed at steaming the chips.
    The device has a pressure tank and a compressor, and the pressure tank is installed between the defibrator and the pulp collector and is connected through the compressor to a de-fiber, wood chip heater.
    The drawing shows a device illustrating the proposed method.
    Chip along the conveyor 1 is continuously directed to the chip heater 2, in which the chip runs countercurrently with expansion steam, which has a temperature of 100 ° C and reaches 90-100 ° C when unloaded through the screw press 3.
    From the screw press 3, the heated chips enter the screw press 4, which presses it in the defibrator-heater 5, while the chips are so dehydrated that the dry matter content reaches at least 50%, preferably 55-65%. Squeezed warm water is discharged through line 6.
    Steam is supplied to the defibrator-heater 5 in two ways, partially by removing process steam from the on-tank 7 through the compressor 8 and steam line 9, and partially as fresh steam through the pipe 10, so that the temperature of the chips supplied to the defibrator 11 through the screw press 12 corresponds to the splitting temperature.
    To remove the sucked fiber from the steam, a filter is installed in front of the compressor 8 in the circulation pipe.
    The amount of fresh steam should be set so that the temperature of the chips in front of the chip heater 2 is in the range of 90-100 ° C, which is adjusted using the sensor 13 mounted on the screw press 3. The sensor 13 controls the valve 14.
    Due to the forced circulation of the steam obtained in the splitting zone, it is directed in the direction of flow with the substance into the pressure tank 7. The substance is blown into excess steam and through the bypass valve 15 and pipe 16 is fed into the pulp collector 17, where the steam and substance are separated apart from each other. The substance is liquefied with return water and discharged through a pipe 18 to prepare a pulp layer, while steam is blown through a blower 19 through a pipe 20 into the chip heater
    2. Released return water can be supplied through line 21 to the pulp collector 17.
    So much fresh steam should be supplied to the defibrator-heater 5 so that the amount of expansion steam when blowing the substance is sufficient to raise the temperature of the introduced chips to 90-100 ° C. Under such conditions, an excess of steam is formed in the defibragor system, which should be removed, which also has a good effect on the removal of substances from the pressure tank 7.
    An example. A pulp is made of wood with a productivity of 5000 kg / h dry matter under the following conditions: weight yield 99%, dry matter content of chips 50%, and inlet temperature 5 ° C, energy consumption 625 kW / h and splitting temperature 171 ° C, which corresponds to steam pressure 785 cc (in k g / cm ' 1 ).
    Heating the supplied wood chips from 5 to 95 ° C gives a steam flow rate of 1233 kg at atmospheric pressure and an appropriate amount of condensate. Wood chips contain 44.5% of dry matter and are released by pressing 2153 kg of water when feeding chips using a screw press 4 into the defibrator-heater 5. The wood chips now contain 55% of dry matter and have a temperature of 95 ° C. To raise the temperature in the defibrator-heater to 171 ° C, you need 492,000 cal, which corresponds to 1004 kg of steam at an absolute pressure of 785 cc.
    80% of the input splitting energy goes into heat, which corresponds to 430000 cal or 877 kg of steam from water with a temperature of 171 ° C. Therefore, 127 kg of steam should be supplied to get enough heat to raise the chip temperature to the value of the splitting temperature. Theoretically, this corresponds to the minimum possible flow rate of steam for splitting, if the chips enter 95 ° C when introduced into the defibrator-heater 5.
    When the finished substance is released under such conditions, only 823 kg of steam is released at atmospheric pressure, so it is necessary to introduce an additional 410 kg of steam in order to heat the chips at the inlet to 95 ° C. It is preferable to supply heat that is insufficient to heat the supplied chips in the form of high-pressure steam to the defibrator-heater 5, since the output of the finished substance is facilitated. Therefore, 522 kg of fresh steam should be supplied to the defibrator under a pressure of 785 cc, which together with the heat generated in the splitting zone gives 1399 kg of steam with a pressure of 785 cc.
    Of this amount of steam, 1004 kg is discharged, and 395 kg is obtained in the Q form of unheated steam, which is carried out with the substance and which, when the pressure drops to atmospheric, gives so much steam that is enough to heat the supplied wood chips to 95 ° C.
    The energy consumption for the furnace of the finished substance is 125 kW / h and the steam consumption is 105 kg at a pressure of 785 cc, i.e. consumption values, which are significantly lower than the values that have so far occurred when splitting wood into fibers.
    . In the splitting process with the lowest possible total energy consumption, the amount of expansion steam is usually sufficient to be able to supply the output substance to the pulp collector 17. Depending on the length of the blowing pipeline, the possible difference in the heights and volumes of the product, the amount of expansion steam may be insufficient in certain cases, so additional steam must be supplied to the splitting unit.
    This occurs mainly by increasing the supply of fresh steam to the defibrator. It is possible to supply steam to the blow pipe and behind the bypass valve, due to which both the quantity and the fall of the transporting steam increase.
    Method for the production of thermomechanical pulp for the manufacture of fiber boards, by
    权利要求:
    Claims (3)
    [1]
    the porous tank 7 through the compressor 8 and the steam line 9, and partly as fresh steam through the pipe 10, so that the temperature of the chips fed to the defibrator 11 through the screw-press 12 corresponds to the splitting temperature. In order to remove the suction fiber from the steam, a filter in the circulation pipe is installed in front of the compressor 8. The amount of fresh steam should be set so that the chip temperature in front of the chip heater 2 is within the EO-CW, which is controlled by the sensor 13 mounted on the screw press 3, the sensor 13 controls the valve 14. Due to the forced circulation the steam produced in the splitting zone is directed in the direction of flow along with the substance to the pressure tank 7. The substance is blown up into excess steam and through the discharge valve 15 and the pipe 16 is fed into the pulp collector 17, where the steam and the substance are separated g from each other. The substance is liquefied with reverse water and discharged through pipe 18 to prepare a layer of pulp, while steam is blown with blower 19 through pipe 20 into chip preheater 2. The released return water can be fed through pipe 21 to the pulp collector 17. The defibrator-preheater 5 should be supplied with so much fresh steam, so that the amount of expansion vapor when purging the substance is sufficient to raise the temperature of the introduced chips to 90-100 °. Under these conditions, the defibr Ator formed excess steam which must be vented, which also affects the good material removal from the pressure vessel 7, Example. The pulp is made from wood with a capacity of 5,000 kg / h of dry matter under the following conditions: a weight output of 99%, a dry matter content of chips of 50%, and an inlet temperature of 5 s, an energy consumption of 625 kW / h, and a splitting temperature of 171 ° C, which corresponds to a vapor pressure of 785 knz (in kg / cm). Heating the supplied chips from 5 to 95 ° C gives steam consumption of 1233 kg at atmospheric pressure and a corresponding amount of condensate. Chips contain 44.5% of dry matter and, when pressing, 2153 kg of water are released when chips are supplied using screw-press 4 to defibrator-heater 5. The filed chips now contain 55% of dry matter and have a temperature. In order to raise the temperature in the defibrator heater to 171 ° C, 492,000 calories are needed, which corresponds to 1004 kg of steam at an absolute pressure of 785 cu. 80% of the input splitting energy is converted into heat, which corresponds to 430000 cal or 877 kg of steam from water with a temperature. Thus, 127 kg of steam must be supplied in order to obtain sufficient heat to raise the chip temperature to the splitting temperature value. Theoretically, this corresponds to the minimum possible steam consumption for splitting, if the chips, when introduced into the defibrator-heater 5, have a temperature of 95 C. When the finished substance leaves, under such conditions only 823 kg of steam is released at atmospheric pressure, therefore, an additional 410 kg of steam must be introduced to heat the chips at the inlet to 95 ° C. It is preferable to supply the heat lacking for heating the supplied chips in the form of high-pressure steam to the defibrator-preheater 5, since this facilitates the removal of the finished substance. Therefore, 522 kg of fresh steam at a pressure of 785 kHz should be fed into the defibrator, which, together with the heat generated in the splitting zone, yields 1399 kg of steam at a pressure of 785 kHz. Of this amount, 1004 kg of steam is removed, and 395 kg is produced as an underheated steam, which is carried with the substance and which, when the pressure drops to atmospheric, gives so much steam that is sufficient to heat the supplied chips to. The energy consumption for the furnace of the finished substance is obtained 125 kW / h and the steam consumption of 105 kg at a pressure of 785 kW, i.e. consumption values that are significantly lower than the values that have so far occurred when splitting wood into fibers. In the splitting process, with as low total energy consumption as possible, the amount of expansion steam is usually sufficient to be able to feed the material to the collection 17 of the pulp. Depending on the length of the pipeline to be blown out, the possible difference in heights and production volumes, the amount of expansion steam may be insufficient in certain cases, therefore additional steam must be supplied to the splitting unit. This is mainly due to an increase in the supply of fresh steam to the defibrator. It is possible to supply steam to the blow pipe and to the relief valve, due to which both the amount and the drop of transporting steam increase. The invention The method of production of thermomechanical wood pulp for the manufacture of fiber plates, by heating the chips in a preheater, steaming it in a deflector underheater, feeding chips, pressed to 50% dryness, in a defibrator, grinding it in a fibrator at a temperature of 130-200 an atmosphere of saturated steam under pressure and removal of the fibrous mass together with steam from the grinding zone, characterized in that, in order to reduce steam consumption, a part of the steam is removed along with the pulp from the grinding zone , increase its pressure to a pressure higher than the pressure in the defibrator and direct the steam to the steaming steam.
    [2]
    2. A method according to claim 1, characterized in that fresh steam is added to a part of the steam directed to the steaming of the chips,
    [3]
    3. A device for carrying out the method according to claim 1, comprising a split heater, a defibrator heater, a screw press, a defibrator and a collection of fibrous mass, characterized in that it has a pressure distributor and compressor, the pressure tank being installed between the defibrator and collection container pulp and is connected through a compressor with a chipboard preheater. Sources of information taken into account in the examination 1. Patent-UK 1412608, cl. B 02 C 7/00, 1975.
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    引用文献:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE7608847A|SE413784B|1976-08-06|1976-08-06|SET AND DEVICE TO USE IN DEFIBRATION ZONE DEVELOPED HEAT TO MINIMIZE CONSUMPTION WHEN PREPARING MASS FOR FIBER DISC|
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