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    • 专利摘要:

    公开号:AT510109A2
    申请号:T0909210
    申请日:2010-02-24
    公开日:2012-01-15
    发明作者:Esa Viljakainen
    申请人:Metso Paper Inc；
    IPC主号:
    专利说明:

    «* ♦ * * • *« * * * 70774 31/31 • · · * * * * * * * * * * »» * * * * * * 1
    The present invention relates to the grinding of wood chips or Zelistofffasern. More specifically, the present invention relates to a method for grinding wood chips or pulp fibers according to the preamble of independent claim 1 and a system for grinding wood chips or pulp fibers according to the preamble of independent claim 12. Furthermore, the present invention relates to a refiner for grinding Wood chips or pulp fibers according to the preamble of independent claim 24.
    In the context of the present invention, the milling process generally takes place in at least two successive milling stages which pass through the wood chips or pulp fibers with the aid of a carrier medium, the actual grinding taking place in a plate gap extending between or between a stator-rotor unit two rotor units of a refiner is located, wherein the stator-rotor unit or the rotor units comprise grinding segments. However, the refiner according to the present invention can also be applied in a one-step milling process.
    The first step towards improved refining, coupled with heat recovery, was to pressurize the refiner. The first took place at Kaipola Mills on a pilot scale in 1976. This improvement rapidly spread and in 1977 a new TMP plant was delivered and commissioned at Kaipola Mills (United Paper Mills). The TMT plant with a capacity of 300 t / day was equipped with a pressurized first stage and a non-pressurized second stage. After the good experience in Kaipola Mills, heat recovery as a clean steam for the paper machine became a standard concept for today's TMP plants.
    In general, the actual grinding takes place in a plate gap between a stator of a refiner and a rotor unit of a refiner or between two rotor units of a refiner, wherein both the stator unit and the rotor grinding segments with different geometric shapes include to specifically the flow phenomena, the specific energy consumption (SEV), the properties of the pulp and the distribution of wood chips or pulp fibers.
    A typical grinding process is a thermo-mechanical grinding process, or TMP process, or a chemo-thermo-mechanical grinding process, or CTMP process, wherein the multi-stage grinding process in one, two or three grinding stages in a TMP or a CTMP Mainline takes place. The refiners can be single-disc refiner (SD refiner), two-disc refiner (DD refiner), cone refiner (CD refiner) or twin refiner. The actual grinding takes place in a plate gap, which is located between a stator of the refiner and a rotor of the refiner or between two rotors of the refiner, wherein the one or more rotors can rotate between 1500 U / min and 1800 U / min. Both the stator unit and the rotor, which are preferably made of a special alloy, include refining segments having different geometrical shapes to specifically control the flow phenomena, the specific energy consumption (SEV), the properties of the pulp and the distribution of wood chips or pulp fibers to influence.
    The carrier medium introduced into the refiner for transporting preheated chips in the process is usually water or another fluid. Grind segments have different geometric shapes that have a specific impact on mass and vapor flow phenomena, SEV, pulp fiber distribution, and pulp properties.
    The "AS publication titled" MEASURED MASS AND HEAT BALANCE OF THE TANDEM TMP LINE "by Esa Viljakainen, Finland, by Roland Pehrsson, Finland, by Timo Sopanen, Finland, and by Markku Perkola, Finland, discloses the basics of designing a TMP Mahlungsstrecke. In general, this publication describes the overall technical picture of the TMP grinding line in the TMP plant Jämsänkoski. The results and calculations are based on * * • «* * •« • · · * * 3 '
    Measurements using conventional flow, pressure and temperature indicators and the process control system of the TMP plant. The TMP plant with five refiner lines (SD-60, 6.5 MW) was put into operation in 1981 and has a capacity of 575 t / day. A sixth refiner line was added in 1984. The TMP plant produces either dithionite or peroxide bleached TMP for PM4 and / or PM5. In 1985, PM4 produced various coated wood grade offset paper grades, and PM5 produced SC magazine paper grades. The heat recovery included a finned heat exchanger for converting high pressure contaminated steam into clean steam and a heat exchanger for heating process water with the contaminated low pressure steam. The recovered clean steam was used in the PM5. A proportion of 50 to 60% of the total steam requirement was recovered from the TMP vapor. The heat from the low-pressure heat recovery was used to heat the feedwater of an auxiliary power plant.
    Various options for TMP heat recovery are considered. The heat recovery for the paper machine could be increased to 70% of the total energy requirement of the grinding. The basic concept of TMP recovery was based on the fact that about 70% of the waste heat of the main line refiners can be recovered as clean steam for the paper machine. In practice, this has been proven in many installations. However, if more efficient heat recovery is needed, we also need to know more about the heat losses and heat balance of a TMP plant.
    In this case of a TMP plant disclosed in the "ΤΑΡΡΓ publication, various process values were obtained by means of the process control and information system {Honeywell TDC-2000). The flow measurements were made using venturi tubes, rotameters, and orifice flowmeters. Due to the liquid condensate droplets transported by the steam, some difficulties arose especially in the measurements of process steam flows. The flow measurements of the flow measurements of the flowmeter.
    Fiber flow between the refiners also failed due to failed venturi tube measurements. The production rate was correlated with the speeds of the feed screw of the preheater. If necessary, the pressure values were obtained by means of the monitoring system. Temperatures were measured using thermocouples and thermometers. The substance densities of the different fiber flows were calculated on the basis of separate samples and laboratory tests. The temperatures of dilution water (for cyclone spray and dilution in the refiner) and white water were 61 ° C. The average production rate during the tests was 102 ± 2 t / day, and the energy values for the main line refiner's SEV and the Canadian Standard Freeness (CSF) value during the three days of the experiment were: SEV - 2045 kWh / t and CSF - 105 ml, respectively ,
    US Patent No. 7300540 discloses a system and method for a TMP refining process of wood chips. According to the teachings of this publication, the chips are prepared for grinding by being exposed to a steam environment to soften the chips, destructively restructure the softened chips and dewater to a solids density of over 55%, and the destructured and dewatered chips to a stock consistency be diluted in the range of about 30 to 55%. The material is partially shredded by the destructuring. This diluted material is passed into a rotary primary refiner, with each of the opposed discs having an inner ring pattern of rods and grooves and an outer ring pattern of rods and grooves. The partially shredded carvings are substantially completely frayed by the destructuring in the inner ring, and the resulting fibers are fibrillated in the outer ring. Compressive destructuring, dewatering and dilution may be implemented entirely in a single integrated plant part immediately before the primary refiner, and both defibering and fibrillation are accomplished between only a single set of relatively rotating disks in the primary refiner.
    US Patent No. 6458245 discloses a CTMP grinding process of wood chips. An absorbent, chemo-thermo-mechanical pulp made
    Lignocellulosic material with a wood yield of over 88%, a low resin content of less than 0.15%, a long fiber content of over 70%, a short fiber content of less than 10% and a cockroach content of less than 10% 3 is provided in accordance with the teachings of this publication. The process for producing the pulp comprises the steps of impregnating, preheating, defibering and washing the material. The impregnation and heating of the chips takes place in one and the same container over a combined period of not more than 2 minutes, preferably not more than 1 minute, more preferably not more than 0.5 minutes, using a warm impregnating liquid having a temperature of at least 100 ° C., preferably at least 130 ° C, and preferably at substantially the same temperature as in the preheating process; and the preheating of the chips is carried out at a temperature between 150 ° C and 175 ° C, preferably between 160 ° C and 170 ° C. The defibering is done with an energy input of at most half the energy input required for defibering when preheating and defibering is performed at 135 ° C.
    The high power consumption (SEV) in mechanical pulp processing has always been considered a serious drawback and a major problem for all mechanical pulp pulping processes, such as the TMP and CTMP grinding processes, especially in the case of softwood species (WH). However, due to the rising raw material and capital costs, mechanical pulp processing is more favorable compared to chemical pulp processing. In particular, the TMP process and the CMTP process are becoming increasingly popular - on the one hand because of their good fiber properties, and partly because of the high value of the recovered steam.
    Due to the high degree of turbulence, the energy efficiency is quite low. It is estimated by various sources that less than 5% of the primary energy flows into the actual fiber processing. The remaining energy flows into the evaporation of the dilution water, into friction and other losses.
    One of the main reasons for a high SEV is the "backflow" steam that flows backwards out of the plate gap against the pulp or pulp feed causing a high degree of "useless" turbulence and mixing. This return steam is formed by evaporation of dilution water in the grinding zone. Some studies (Esko Härkönen, JAMA project 1992-1999) indicate that 50% of the total energy consumed in this "mixing and inflow zone and only 50% consumed in the actual refining zone. Several other studies (Hans-Olof Backlund, Lic Thesis) indicate that 85% is consumed in the refining zone.
    The grinding process according to the prior art additionally has the disadvantage, irrespective of the carrier medium, that the wood chips or fibers transported by means of the carrier medium tend to form layers on the inner wall of the refiner housing and deposit the outlet or exit the refiner to block or block. There is reason to believe that the narrow flow channels or passages for the mixture of carrier medium and wood chips or fibers through the refiner cause compaction of the carrier medium, causing the transported chips or fibers to become moist and therefore as layers deposit and accumulate on the walls of the refiner housing and block or block the outlet or outlet of the refiner.
    A main object of the present invention is to eliminate or at least substantially mitigate the problems and disadvantages of the prior art. In accordance with one aspect of the present invention, a second object of the present invention is to provide a new and inventive method for grinding chips or fibers. According to a second aspect of the present invention, a third object of the present invention is to provide a new and inventive system for grinding wood chips or fibers. According to a third aspect of the present invention, a fourth object of the present invention is to eliminate or alleviate a back-flow phenomenon caused by the evaporation of water used as the carrier medium in the mashing process according to the * *
    State of the art is used. According to a fourth aspect of the present invention, a fifth object of the present invention is to lower the high SEV of the grinding process according to the prior art. According to a fifth aspect of the present invention, a sixth object of the present invention is to ensure that the inside of a refiner and in particular the exit zone or the exit area remain clean and free.
    In general, the objects of the present invention can be realized by means of the method, the essential features of which are defined in the characterizing part of independent claim 1. The other and essential features of the method according to the present invention are defined in the dependent claims 2 to 11.
    In general, the objects of the present invention can also be realized by the system whose essential features are defined in the characterizing part of independent claim 12. The other and essential features of the system according to the present invention are defined in the dependent claims 13 to 23.
    In general, the objects of the present invention can also be realized by the refiner, the essential features of which are defined in the characterizing part of independent claim 24. The other and essential features of the refiner according to the present invention are defined in the dependent claims 25 to 29.
    The present invention is thus based on the basic idea that no dilution fluid or water is used, but that the dilution fluid is replaced by a gaseous carrier medium or by a vaporous medium in the grinding process, which is a multi-stage or a single-stage TMP grinding process multistage or one-step CTMP grinding process. According to the present invention, water vapor is used as the vaporous carrier medium, and compressed air (or a mixture of air and steam) is used as the gaseous carrier medium.
    Preferably, a split carrier medium supply to the input side and the output side of the refiner is used.
    According to a preferred embodiment of the present invention, the supply of the vaporous / gaseous carrier medium is divided into at least two parts. Preferably, a first portion of the vapor / gas is provided in front of the stator-rotor unit or rotor units, i. H. on the input side, introduced into the refiner, and a second part of the vapor / gas is fed to the stator-rotor unit or units, i.e., the rotor. H. on the exit side, introduced into the refiner. On the exit side of the refiner steam / gas can be directed to an outer area of the refiner housing, in particular to an exit area of the refiner, to avoid stagnant areas in which ground pulp may accumulate and clog the refiner. On the exit side of the refiner, steam / gas can be introduced into a blow line (flow line) connecting successive refiner. On the input side of the refiner steam / gas can be introduced into a supply line (inlet line) of the refiner. On the input side of the refiner steam / gas can be introduced into a crushing zone in the housing of the refiner in front of the stator-rotor unit or the rotor units.
    According to a further embodiment, the supply of the vaporous / gaseous carrier medium can be divided into three parts, wherein a first part of the steam / gas upstream of the stator-rotor unit or the rotor units, i. H. on the input side, is introduced into the refiner and a second part of the vapor / gas after the stator-rotor unit or the rotor units, d. H. is introduced on the output side, in the refiner and a third part of the steam / gas is introduced into a feed line or into an inlet line of the refiner on the input side of the refiner.
    As advantages of the present invention, one can cite the following. Evaporation of dilution water in the refiner is avoided. Primary electrical energy used to evaporate dilution water is minimized or even eliminated. The SEV could be lowered (at least theoretically) to a value of 25% compared to the state of the art, with the energy saving potential being 75% (in WH-TMP). A high consistency of material is achieved during grinding (part of the car- bon or wood containing water is evaporated), which would further increase the efficiency of grinding. The air flow through the refiner can be controlled by a variable compressor speed; This creates new options for the practical refiner control. A lower system temperature can increase the brightness of the pulp after grinding in the main line. Bleaching agents, such as hydrogen peroxide or ozone, could be used in bleaching in the refiner, resulting in capital savings potential. Some extractants, such as pitch, etc., could be oxidized, making extractants more soluble and easier to leach, and would open up further opportunities for using, for example, pinewood as a raw material in woody paper grades.
    With regard to the advantages of the present invention, the following can be cited. In the TMP or CTMP process, some influence can be exerted on the mechanical pulp quality. It can be assumed that WH-TMP is likely to shorten the fiber length, while hardwood CTMP has no effect. Certainly there will be a big impact on the total energy budget of the entire integrated mechanical pulp mill and pulp mill. If less heat is produced in the heat recovery, a corresponding amount of steam must somehow be replaced. This may promote the use of biomaterial or waste recovery as a fuel for heat and power generation in the factory. The primary energy requirement (MWh / t product) for market pulp, paper or cardboard is reduced.
    The above-mentioned characteristics and other relevant features of the present invention are defined in the appended claims and will be described in more detail in the following specific part of the description.
    The present invention will be described in the following specific part of the description of preferred embodiments of the present invention with reference to the accompanying drawings, in which: FIG. 1 shows a grinding process according to the prior art, where the carrier medium is water, FIG. 2 shows the refining process according to a first embodiment of the present invention when compressed air is used as the carrier medium in the refining process, FIG. 3 shows the refining process according to a second embodiment of the present invention when steam is used as the carrier medium in the refining process, FIG. FIG. 4 shows a preferred feeder suitable for feeding the mixture of the chip / fiber material and gaseous / vaporous carrier medium into the refining stages of FIG. 2 or from FIG. 3 could be used, FIG. FIG. 5 shows another preferred feeder, or in other words a modified feeder adapted for feeding the mixture of the pulp / fiber material and the gaseous / vaporous carrier medium into the refining stages of FIG. 2 or from FIG. 3 could be used, and FIG. Figure 6 shows a split carrier media feed embodiment for a refiner. For a better understanding of the basic idea of the present invention, we turn now to FIG. 1, which discloses the TMP grinding line in the Jämsänkoski pulp mill according to the prior art. The TMP line includes a preheat unit 10 and a first refiner 22 and a vapor separator cyclone 23 and a second refiner 32 and a separator such as a strip cyclone 7 and a discharge tube and a receptacle 12 for receiving the separated pulp / pulp material from the strip cyclone 7 For the sake of simplicity, the feeder preceding a grinding stage will hereinafter be referred to as a PeriFeeder, which is the commercial trade name for a feeder preceding the grinding stage.
    The production in a grinding line according to FIG. 1 can be controlled by controlling the speed of the plug screw 1, which introduces wood chips preheated in a preheating unit 10 in a mixture with a temperature of 70 ° C with water in the first grinding stage 2. The degree of refining (eg, Canadian Standard Freeness, CSF) or the power consumption of the first refining stages 2 and the second refining stage 3 can be controlled by adjusting plate columns of the refiner 22, 32. In order to maintain a residence time measured in milliseconds in the plate gap, the pulp is forced out of the plate gap of the refiner 22, 32 by means of dilution water and centrifugal forces. Dilution water is introduced at a temperature of about 83 ° C by means of steam formed in the refiners 22, 32 into both the first refiner 22 and the second refiner 32. The amount of power consumption can also be varied by means of the dilution water, and thus the pulp / pulp layer thickness in the refining zone can be controlled to carry the pulp out of the refiner 22, 32 and into the air at an appropriate flow rate between 20 and 60 m / s Blasleitung 9 to blow.
    According to the basic idea of the present invention, no water is used as a carrier medium for material to be ground in subsequent milling stages. If a gaseous carrier medium such as compressed air or a vaporous carrier medium such as water vapor or a mixture of gas and steam is used for grinding, it is advisable to reconsider handling and tuning. It might be considered that the general control principles described above are retained. If the carrier medium is a gaseous medium such as compressed air or a vaporous carrier medium such as water vapor, however, it is possible to control the flow of the gaseous medium or the vaporous medium by reducing the residence time of chips / pulp in the plate gap of the refiner 22, 32 controls or by controlling the flow velocity in the blowing line 9. It is further preferred that gas or steam is introduced at other points in the system, namely preferably at the supply line 81 of the first grinding stage 2 and the supply line 81 of the second grinding stage 3 and the flow tube 9. In simplified form, the energy consumption depends in the grinding of chips / pulp after "the number of grinding pulses χ of the residence time". Then, the residence time in the refiner 22, 32 can be controlled by means of the gas flow rate or the steam rate. In other words, it is possible to maximize the power consumption of the system for shaping chips and fiber bundles, because, in principle, no energy is consumed for the evaporation of dilution water.
    It is intended to introduce the gas / vapor flow into a refining zone along meal segment grooves of a leaf segment. Ideally, the mass passes through the plate gap of the refiner 22, 32, and the gas / vapor flows into segment grooves of the refiner.
    Let us now turn FIG. 2, in which compressed air is used as the carrier medium. A first feeder 21, or in other words the first PeriFeeder 21, which is arranged in connection with the first grinding stage 2 receives via a first carrier medium supply line 81 compressed air, which is used as the carrier medium, and wood chips or pulp fibers to be ground, via the Schnitzel- / Faserzuleitung 11. The first PeriFeeder 21 separates the wood chips or pulp fibers and the compressed air from each other, and the PeriFeeder directs the compressed air and the Schnitzel / fibers separately from each other in the first actual refiner 22. The mixture of compressed air and the chips / Fibers flows via the main flow line 9 from the first refining stage 1 to a second refining stage 2. A second feeder 31, or in other words the second periFeeder arranged in connection with the second refining stage 3, receives the mixture of compressed air and chips / fibers over the main 9 and a we The second PeriFeeder 31 separates the wood chips or pulp fibers and the compressed air from each other, and the second PeriFeeder directs the compressed air and the compressed air
    Chips / fibers separated from each other into the second actual refiner 32. More valuable refiner (not disclosed in FIG.2) may be arranged after the second grinding stage 3. *** "
    When the pulp / fiber material and the compressed air are introduced into the actual refiner 22, 32 separately from each other, they are introduced through the periFeeder 21, 31 into the actual crushing / feeding zone of the refiner. In the actual grinding zone, centrifugal forces push the chip / fiber material into a refining gap of the refiner 22, 32, and the compressed air moves or advances in segment grooves of the refiner 22, 32.
    In the process of FIG. 2, in which compressed air is used as the carrier medium, preheated chips or pulp fibers are introduced through a plug screw 1 into a first periFeder 21, and compressed air is introduced into the first periFeder 21. The supply of the compressed air is preferably accomplished by a compressor 6 which is most preferably a turbo-compressor which increases the pressure of the air to circulate in the process. Thereafter, the first grinding of the mixture of compressed air and wood chips or pulp fibers takes place in a first-stage refiner 22. The mixture is then blown by means of a second PeriFeeder 31 from the first grinding stage 2 into a second grinding stage 3. Further compressed air, if needed, is introduced into the second PeriFeeder 31. The supply of the compressed air is preferably accomplished by a compressor 6 which is most preferably a turbo-compressor which increases the pressure of the air to circulate in the process. Then, the mixture of compressed air and wood chips or pulp fibers in the second stage refiner 32 is further ground. The mixture is then blown into an air separator 4 where air and slices / fiber material are deposited. The chip / fiber material then goes to latency removal and further processing. The compressed air is introduced into an air scrubber 5 where the air is cooled and cleaned of fines / fiber fines. The scrubber is needed to keep the turbine compressor 6 clean. Excess heat from milling can be released to water, which can later be used in the pulp and paper making process.
    Explanation of the Terms of the Process of FIG. 2: make-up water is introduced into the cycle of the heat recovery agent (abbreviation: HR agent) or the air scrubber 5; this may be waste water from the pulp mill or pulp mill white water or fresh water; inert gases are released from the circulation gas flow line to the compressor 6. The inert gases are typically terpenes, predominantly turpentine, which should be removed from the gas stream flowing to the turbine compressor 6. This stream is more like a drain into turpentine recovery or combustion;
    Additional air is introduced into the circulation gas flow line to the compressor 6; It is understood that a certain amount of this kind of air is needed. The additional air could also consist of an inert gas such as CO2 or N2.
    One of the advantages of using this type of inert gas (air, air-steam mixture, etc.) as a carrier medium is the fact that an inert gas-steam mixture under typical Mahlungsbeding (temperature and pressure) above the "gas-vapor saturation point " lies. That is, it is less likely to have a condensing effect during the pressurized refining process.
    When compressed air is used as the carrier medium, the decisive innovations are the use of a separate compressed air supply line 81 and a separate feed line 11 for preheated carcass / fiber material for feeding the first periFeeders 21 of the first grinding stage 2 and also for feeding the compressed air supply line second PeriFeeders 31 of the second grinding stage 3 and in the use of compressed air as a "carrier" medium in both the first grinding stage 2 and in the second stage 3. Furthermore, the compressed air and the PeriFeeder 21, 31 for the supply of wood chips or Pulp fiber used in the subsequent Erststufenrefiner 22 and the second stage refiner 32. Preferably, the periFeeder would be used to introduce the chips / fibers and the compressed air separately into the crushing / feeding zone of the refiner 22, 32. In the actual grinding zone, centrifugal forces press the fiber material into the grinding nip, and the compressed air moves or advances in segment grooves.
    Let us now turn FIG. 3, in which water vapor is used as the vaporous carrier medium. A first periFeeder 21, which is normally used as a cyclone to separate wood chips or the pulp fibers and carrier medium from each other, is used for feeding the first grinding stage 2, and a second periFeeder 31 is used for feeding the second grinding stage 3. Preferably, water vapor is used as a vaporous carrier medium to transport the mixture of water vapor and the wood chips or pulp fibers into and through the subsequent grinding stages 2, 3. The mixture of wood pulp / fiber material and the water vapor is preferably introduced into the comminution / feed zone of the refiner 22, 32 separately from each other through the periFeeder. In the actual grinding zone, centrifugal forces press the fiber material into the grinding nip, and the water vapor moves or advances in segment grooves.
    In the process of FIG. 3, preheated wood chips or pulp fibers are passed through a stuffing screw into a first periFeder 21, and water vapor is directed to the periFeeder. Thereafter, the first grinding of the mixture of water vapor, air and wood chips or pulp fibers in a first stage refiner 22 is carried out. The mixture is then blown from the first grinding stage 2 into a second grinding stage 3 comprising a second periFeder 31. If necessary, more water vapor is directed to the second periFeeder.
    Then, the mixture of water vapor and wood chips or pulp fibers in the second stage refiner 32 is further ground. The mixture is then blown into a vapor separator 4, where the water vapor and the pulp / fiber material are separated from each other. The chip / fiber material then goes into the latency elimination and further processing. The water vapor flows back at least into the first periFeeder of the first cooling stage 911, and optionally water vapor also flows, if necessary, into the second periFeeder of the second refining stage 912, 913. Excess heat from the refining can be diverted to a heat recovery unit in water, later in the pulp and papermaking process can be used.
    The processes described in FIGS. 2 and FIG. 3 may be referred to as a "pneumatic grinding process" due to the vaporous carrier medium such as water vapor or the gaseous carrier medium such as compressed air. Under certain circumstances, the pressure level can be adjusted more or less freely according to the optimal conditions for practice. It is understood that the system temperature should be high enough to soften the lignin, i. h, between 90 ° C and 150 ° C. The circulating vaporous or gaseous medium may be a mixture of compressed air and water vapor.
    Let us turn FIG. 4, in which a PeriFeeder is shown, which comprises separate supply lines, namely a first supply line 11, which is arranged in the region of the circumference supply line for wood chips or pulp fibers, and a second supply line 811, 911, wherein it is a central feed for a gaseous carrier medium such as compressed air or a vaporous medium such as water vapor, which could be used to introduce the mixture of chip / fiber material and the gaseous / vaporous carrier medium into each of the milling stages (see refining steps 2) 3 in FIGS. 2 and 3). The PeriFeeder 21, 31 further comprises a fixed shell member 213 and a rotating spiral blade member 211, which is circumferentially spaced from the core member 212. The rotating blade member 211 causes movement of the chip / fiber material within a stationary shell member 213 and around a central core member 212 in the direction of the refiner 22, 32 which includes a concentric rotor 222 and stator 221 rotating relative to each other actual grinding to accomplish. Grinding segments are connected to the rotor 222 and the stator 221.
    The PeriFeeder 21; 31 works like a cyclone, which wood chips or the pulp fibers, which are fed via the feed line 11 in the PeriFeeder, and 7. The carrier medium, which is supplied via the supply line 811; 911 is fed into the PeriFeeder, and the PeriFeeder is used to feed the refiner 22, 32 to separate the carrier medium and the slab / fiber material through the PeriFeeder into the shredding / feeding zone of the refiner 22, 32 separately , In the actual grinding zone, centrifugal forces push the slab F / fiber material into the grinding nip, and the carrier medium moves or advances in segment grooves.
    Let us now turn FIG. 5, which shows a PeriFeeder comprising separate leads, namely a first circumferentially arranged supply line 11 for wood chips or pulp fibers and a second circumferentially arranged supply line 811, 911 for a gaseous carrier medium such as compressed air or a vaporous medium such as steam, which peri-feeder could be used to feed the mixture of wood pulp / fibrous material and the gaseous / vaporous carrier medium into each of the refining stages (see refining steps 2, 3 in Figures 2 and 3). The PeriFeeder 21, 31 further comprises a stationary shell element 213 and a rotating spiral blade element 211, which is circumferentially spaced from a central core element 212. The rotating blade member 211 causes movement of the chip / fiber material within a stationary shell member 213 and around the core member 212 in the direction of the refiner 22, 32, which includes a concentric rotor 222 and stator 221 rotating relative to each other Grinding to accomplish.
    The PeriFeeder 21; 31 functions like a cyclone, which chips or the pulp fibers, which are fed via the feed line 11 in the PeriFeeder, and the carrier medium, via the supply line 811; 911 is fed into the PeriFeeder, and the PeriFeeder is used to feed the refiner 22, 32 to separate the carrier medium and the chip / fiber material separated by the PeriFeeder into the shredder / feed zone of the refiner 22, 32 to lead. In the actual grinding zone, centrifugal forces push the slab F / fiber material into the grinding nip, and the carrier medium moves or advances in segment grooves.
    The crucial technical difference between the PeriFeeder 21; 31 of the figures FIG. 1 and FIG. 4 and the PeriFeeder 21; 31 of the figures FIG. Figures 2 and 5 concern the leads 811,911; 813, 913 and the flow of the gaseous carrier medium such as compressed air or a vaporous medium in the PeriFeeder 21, which precedes the actual grinding stage 2, 3.
    According to the PeriFeeder embodiment of FIG. 4, the introduction of the gaseous / vaporous support medium is configured to occur centrally through one end of the shell 213 of the PeriFeeders from the supply line 811 via a central core element 212, such as a flow tube, such that the gaseous / vaporous carrier medium is out of the central one Core element just before the core portion 223 of the grinding unit 22 exits. In the PeriFeeder 21, the central core member is surrounded by a spiral blade member 211 spaced from the outer surface of the core member and rotating at a rotational speed between 1500 and 3000 rpm. Consequently, a centrifugal force acts on the material flow of chips / fibers. The centrifugal force tends to separate material portions from one another such that heavier material is forced into a sheet space formed between opposite sides of the spiral blade element 211. The outer surface of the central core member 212 is provided with flow grooves to assist the flow of the gaseous / vaporous material forced into the peri-feeder 21 by the chips / fibers from the washing section towards the center of the grinding unit 22. The disadvantage of the prior art solution, when the carrier medium is water, is the generation of backflow steam which causes reverse flow of steam in the periFeeder, thereby disturbing substantially all control of the refining process.
    According to the PeriFeeder embodiment of FIG. 5, the introduction of the gaseous / vaporous support medium is configured to occur circumferentially through the shell 213 of the peri-spring 211 from the supply conduit 811 and outside of a central core member 212, such as a flow conduit, * * * * * ·· · · * · * · ···. * • * ··· ·· * | Q · * * * 4 »9 ι ....."; : .......... > .. · such that the gaseous / vaporous carrier medium flows away from the outer surface of the central core element to a core region 223 of the grinding unit 22. In the PeriFeeder 21, the central core member is surrounded by a spiral blade member 211 spaced from the outer surface of the core member and rotating at a rotational speed between 1500 and 3000 rpm. Consequently, a strong centrifugal force acts on the material flow of the chips / fibers. Depending on the specific gravity of the carrier medium, the same centrifugal force may also act on the gaseous / vaporous carrier medium. The centrifugal force tends to separate different materials such that heavier material is forced into a sheet space formed between opposite sides of the spiral blade member 211. The outer surface of the central core member 212 is provided with flow grooves for assisting the flow of the gaseous / vaporous material forced into the peri-feeder 21 via the circumferentially-arranged lead 811,911 toward the center of the grinding unit 22. The disadvantage of the prior art solution, when the carrier medium is water, is the generation of backflow steam which causes reverse flow of steam in the periFeeder, thereby disturbing substantially all control of the refining process.
    In the embodiments of the figures FIG. 1 / FIG. 4 and FIG. 2 / FIG. 5, the heavier chip / fiber material flows outside the central core member 212 in the spiral blade space of the spiral blade member 211 and flows as a turbulent ring flow to the core portion 223 of the mash unit 22 and outside the outlet portion of the gaseous / vaporous carrier medium stream coming from the interior of the central core member 212 or flow there along and outside the central core element 212. Shortly after the gaseous / vaporous carrier medium has been drained, it is mixed with the pulp / fiber material stream. In the actual grinding stage 2, 3, the various materials flow as they were mixed, while the material fractions are further separated such that the heavier pulp / fiber-containing material from lower parts of the grinding unit 22 into a separate blast line 9, to a Air separator 4 or to a steam scrubber 4 leads, is discharged and the lighter material content of gaseous and vaporous material is discharged from upper parts of the grinding unit. Each blowing line 9 interconnecting successive refining stages 2, 3 is preferably provided with a feed line 912, 914 to keep the lines open while the refining process is active.
    To emphasize the improved SEV achievable by the process, when the carrier medium is a gaseous medium such as compressed air or a vaporous medium such as water vapor, we turn again to the figures: FIG. Figure 1 shows a grinding process according to the prior art, in which the carrier medium is water. The measured material flows and energy balances refer to a TMP process according to the prior art. - FIG. 2, in which the gaseous carrier medium is compressed air, and - FIG. 3, in which the vaporous carrier medium is water vapor and the material flows and energy balances are compared.
    In the case of FIG. 1, the material flows are the following:
    Pulp: water: dilution water: sealing water: total: where 0.11 t / bdt of seal water flow into the process and 310 kPa flows into the heat recovery at a volume flow rate of 1350 m3 / bdt.
    Steam Sealing water: Total: INPUT: 1.00 t / bdt (48%) 1.08 t / bdt 2.82 t / bdt 0.40 t / bdt 5.30 t / bdt EXIT: Pulp: 1.00 t / bdt (36%) water: 1.77 t / bdt 2.24 t / bdt 0.29 t / bdt 5.30 t / bdt TMP vapor (134 ° C,
    In the case of FIG. 1, the energy balance is the following: INPUT:
    Pulp: 1.00 χ 70 χ 1.3 = 91.0 MJ / bdt water: 1.08 χ 70 x 4.2 = 317.5 MJ / bdt dilution water: 2.82 χ 83 χ 4.2 = 983, 1 MJ / bdt
    Sealing water: 0.40 χ 37 χ 4.2 = 62.2 MJ / bdt 1 & 2 SEV: 1,859 x 3600 = 6692,7 MJ / bdt
    Total: 8146.5 MJ / bdt OUTPUT:
    Pulp: 1.00 x 134 x 1.3 = 174.2 MJ / bdt Water: 1.77 χ 134 χ 4.2 = 996.2 MJ / bdt Steam: 2.24 χ 2725 = 6104.0 MJ / bdt
    Grinding / defibration: 0.054 χ 3600 = 194.6 MJ / bdt
    Other losses: 0.188 x 3600 = 677.5 MJ / bdt
    Total: 8146.5 MJ / bdt
    The balance reveals that about 74% of the SEV is consumed in steam production.
    In the case of F! G. 2, where the carrier medium is water vapor, the material flows are as follows: INPUT: pulp: water: "carrier vapor: sealing water total: 1.00 t / bdt (48%) 1.08 t / bdt 1.59 t / bdt 0, 40 t / bdt 4.07 t / bdt OUTPUT: Pulp: Water: Steam: Sealing water: Total: 1.00 t / bdt (65%) 0.54 t / bdt 2.24 t / bdt 0.29 t / bdt 4.07 t / bdt
    It is assumed that the "primary SEV" is spent only for the evaporation of "schnitzelgebundenem water". The steam volume flow rate for heat recovery is 1350 m 3 / bdt (as in the case of the prior art).
    In the case of FIG. 2, the energy balance is the following: INPUT: OUTPUT:
    Pulp: 1.00 χ 70 χ 1.3 = 91.0 MJ / bdt Pulp: 1.00 x 134 χ 1.3 = 174.2 MJ / bdt
    Water: 1.08 χ 70 χ 4.2 = 317.5 MJ / bdt "Carrier vapor 1: 1.59 χ 2725 = 4332.8 MJ / bdt
    Sealing water: 0.40 χ 37 χ 4.2 = 62.2 MJ / bdt 1 & 2 SEV: 0.736 x 3600 = 2650.7 MJ / bdt
    Total: 7454.2 MJ / bdt
    Water: 0.54 χ 134 χ 4.2 = 303.9 MJ / bdt Steam: 2.24 χ 2725 = 6104.0 MJ / bdt
    Grinding / shredding. 0.054 χ 3600 = 194.6 MJ / bdt
    Other losses: 0.188 χ 3600 = 677.5 MJ / bdt
    Total: 7454.2 MJ / bdt
    Considering the above calculations regarding the cases of the figures FIG. 1 and FIG. 2, energy balance calculations reveal a 60% reduction in SEV when the carrier medium is water vapor instead of dilution water, which must be evaporated to produce the necessary amount of steam (in the reference case).
    In the case of FIG. 3, in which the carrier medium is compressed air, the material flows are as follows: INPUT:
    Cellulose:
    Water: "carrier air":
    Seal water:
    Total: 1.00 t / bdt (48%) 1.08 t / bdt 1.59 t / bdt 0.40 t / bdt 4.07 t / bdt OUTPUT:
    Cellulose:
    Water: "Dissolvable": Steam:
    Seal water:
    Total: 1.00 t / bdt (65%) 0.54 t / bdt 1.59 t / bdt 0.65 t / bdt 0.29 t / bdt 4.07 t / bdt
    The volumetric flow rate of the exhaust gas flow is estimated at 1586 m3 / bdt.
    In the case of FIG. 3, the energy balance is the following: INPUT:
    Pulp: 1.00 χ 70 χ 1.3 = 91.0 MJ / bdt OUTPUT:
    Pulp: 1.00 χ 134 χ 1.3 = 174.2 MJ / bdt
    Water: 1.08 χ 70 χ 4.2 = 317.5 MJ / bdt
    Carrier air: 1.59 χ 134 χ 1 = 213.1 MJ / bdt
    Sealing water 0.40 χ 37 χ 4.2 = 62.2 MJ / bdt 1 & 2 SEV: 0.736 x 3600 = 2650.8 MJ / bdt
    Total: 3334.6 MJ / bdt
    Water: 0.54 χ 134 χ 4.2 = 303.9 MJ / bdt
    Carrier air: 1.59 χ 134 χ 1 = 213.1 MJ / bdt
    Steam: 0.65 χ 2725 = 1771.3 MJ / bdt
    Grinding / defibration: 0.054 χ 3600 = 194.6 MJ / bdt
    Other losses: 0.188 x 3600 = 677.5 MJ / bdt
    Total: 3334.6 MJ / bdt
    Considering the above calculations regarding the cases of the figures FIG. 1 and FIG. 2, energy balance calculations reveal a 60% decrease in SEV when the carrier medium is compressed air instead of dilution water, which must be evaporated to produce the necessary amount of steam (in the reference case).
    Considering the above calculations regarding the cases of the figures FIG. 2 and FIG. 3, there is basically no difference in using "steam or air" as the carrier medium. Energy balance calculations reveal a 60% decrease in SEV when the carrier medium is water vapor or compressed air instead of water. Furthermore, it should be noted that the choice of the carrier medium has no influence on the base material and the energy balance. About 60% of the primary SEV is still consumed by water evaporation.
    The present invention has been described above only by means of its preferred embodiments, and various modifications as well as alternatives and equivalently equivalent solutions may be made within the scope defined by the appended claims and within the spirit and spirit of the present invention.
    Innsbruck, on 30, August 2011
    权利要求:
    Claims (30)
    [1]
    1. A method for grinding wood chips or pulp fibers, wherein the method in at least two successive Mahlungsstufen (2, 3) takes place, through which the wood chips or pulp fibers are transported through a carrier medium, wherein the actual grinding takes place in a plate gap, the is located between a stator-rotor unit (221, 222) or between two rotor units of a refiner (22, 32), wherein the stator-rotor unit comprises grinding segments, characterized in that a gaseous carrier medium or a vaporous carrier medium in the successive Grinding stages (2, 3) is used to transport the mixture of carrier medium and chips / fibers in the grinding process, and that the chips / fibers and the gaseous or vaporous carrier medium separated by a feed device (21, 31) in the refiner (22, 32) are initiated.
    [2]
    2. The method according to claim 1, characterized in that a gaseous carrier medium or a vaporous carrier medium is used in the successive stages to transport the mixture of carrier medium and chips / fibers in the grinding process, and that the fibers and the gaseous or vaporous Carrier medium separated by a mechanical separation device, which serves as the feed device (21, 31) are introduced into the refiner (22, 32).
    [3]
    3. The method according to claim 1 and / or 2, characterized in that a gaseous carrier medium or a vaporous carrier medium is used in the successive stages to transport the mixture of carrier medium and chips / fibers in the grinding process, and that the mechanical separation device (21, 31) for the chips or fibers and the gaseous or vaporous carrier medium, such as a PeriFeeder, is used to introduce the chips / fibers and the gaseous or vaporous carrier medium separately into a refiner (22, 32) ,
    [4]
    4. The method according to claim 1, characterized in that the gaseous carrier medium or the vaporous carrier medium is used in the successive milling stages of the milling process, which is preferably a TMP or a CTMP grinding process, to the mixture of carrier medium and chips or the fibers to be transported in and between the successive refining stages, and that a feeder, preferably a mechanical separator (21, 31) for the chips or fibers and the gaseous or vaporous carrier medium, such as a PeriFeeder, is used for this purpose to separate the chips or fibers and the gaseous or vaporous carrier medium separately into a refiner (22, 32).
    [5]
    Method according to one of the preceding claims 1 to 4, characterized in that the supply of the vaporous / gaseous carrier medium is divided into at least two parts, wherein a part (811, 813; 911, 913) of the vapor / gas in the refiner ( 22, 32) in front of the stator-rotor unit (221, 222) or the rotor units, d. H. on the input side, and a second part (812, 814, 815, 816, 912, 914) of the steam / gas in the refiner (22, 32) after the stator-rotor unit (221, 222) or the Rotor units, d. H. on the output side, is initiated.
    [6]
    6. The method according to claim 5, characterized in that from the second part of the steam / gas supply, the steam / gas through a first supply line (812, 814, 912, 914) through an outer wall of the refiner housing, most preferably to an exit region of the Refiners (22, 32) on the output side of the refiner, is initiated.
    [7]
    7. The method according to claim 6, characterized in that the steam / gas through a second supply line (815, 816) on the output side of the refiner in a blow pipe (9) or in a Strömungsieitung, the successive refiner (22, 32) interconnected , is initiated.
    [8]
    8. The method according to any one of claims 1 to 4, characterized in that the steam / gas on the input side of the refiner in a feed line (811, 813, 911, 913) or in an inlet line of the refiner (22, 32) is eingeieitet.
    [9]
    9. The method according to claim 8, characterized in that the steam / gas is introduced into a crushing zone, which is arranged in the interior of the housing of the refiner on the input side of the refiner (22, 32) and the stator-rotor unit (221.222 ) or the rotor units.
    [10]
    10. The method according to any one of the preceding claims 1 to 9, characterized in that compressed air or a mixture of air and steam is used as the gaseous carrier medium.
    [11]
    11. The method according to any one of the preceding claims 1 to 9, characterized in that water vapor is used as the vaporous carrier medium.
    [12]
    12. A system for grinding wood chips or pulp fibers, wherein the system comprises at least two successive Mahlungsstufen (2, 3) through which the wood chips or pulp fibers are transported through a support medium, the actual grinding takes place in a plate gap, which is between a Stator rotor unit (221, 222) or between two rotor units of a refiner (22, 32) is located, wherein the stator-rotor unit comprises Mahlsegmente, characterized in that the carrier medium, a gaseous carrier medium or a vaporous carrier medium for transporting the mixture of carrier medium and chips / fibers in the grinding process, and that a feed device (21, 31) for the separate introduction of Schnitzei / fibers and the gaseous or vaporous carrier medium in the refiner (22, 32) is provided.
    [13]
    13. System according to claim 12, characterized in that the feeding device for the separate introduction of the chips or fibers and the gaseous or vaporous carrier medium into the refiner (22, 32) is a mechanical separating device.
    [14]
    14. System according to claim 12 and / or 13, characterized in that the carrier medium for transporting the mixture of carrier medium and wood chips or pulp fibers in the grinding process of a gaseous carrier medium or a vaporous carrier medium is composed, and that each of the successive Mahlungsstufen a feeder in Form of a mechanical separator for the chips or fibers and the gaseous carrier medium or the vaporous carrier medium, ie a PeriFeeder, for the separate introduction of the chips or fibers and the gaseous or vaporous carrier medium into a crushing or feeding zone of a refiner in each grinding stage.
    [15]
    15. System according to one of the preceding claims 12 to 14, characterized in that the at least one or two successive milling stages Mahlungsprozess is preferably a thermo-mechanical (TMP) or a chemo-thermo-mechanical (CTMP) grinding process.
    [16]
    16. A system according to any one of the preceding claims 12 to 15, characterized in that the carrier medium for transporting the mixture of carrier medium and chips or fibers in the grinding process in the successive stages of the TMP or CTMP grinding process path from a gaseous carrier medium or a vapor-like Carrier medium is composed.
    [17]
    A system according to any one of the preceding claims 12-16, characterized in that the supply of the vaporous / gaseous carrier medium into the refiner is divided into at least two parts, a first part (811, 813, 814, 815, 911, 913) of the supply the steam / gas in the refiner in front of the stator-rotor unit (221, 222) or the rotor units, d. H. on the input side, and a second part (812, 814; 912, 914) of the supply of the vapor / gas into the refiner downstream of the stator-rotor unit (221, 222) or the rotor units, d. H. on the output side, one is conductive.
    [18]
    18. System according to claim 17, characterized in that from the second part of the steam / gas supply, the steam / gas through a first supply line (812, 814; 912, 914) through an outer wall of the refiner housing, most preferably to an exit region of the Refiners (22, 32) on the output side of the refiner, can be introduced.
    [19]
    19. System according to claim 17, characterized in that from the second part of the steam / gas supply, the steam / gas through a second supply line (815, 816) on the output side of the refiner in a blowing line (9) or in a flow line, through the successive refiner (22, 32) are interconnected, can be introduced.
    [20]
    20. System according to claim 17, characterized in that the steam / gas on the input side of the refiner via a feed line (811,911) or an inlet line into the refiner (22, 32) can be introduced.
    [21]
    21. System according to claim 20, characterized in that the steam / gas is arranged in a comminuting zone of the refiner (22, 32) which is arranged on the input side of the refiner in front of the stator-rotor unit (221, 222) or the rotor units, can be introduced.
    [22]
    22. System according to any one of the preceding claims 12 to 21, characterized in that the gaseous carrier medium is compressed air or a mixture of air and steam.
    [23]
    23. System according to any one of the preceding claims 12 to 21, characterized in that the vaporous carrier medium is water vapor.
    [24]
    24. A refiner for refining wood chips or pulp fibers, comprising a housing surrounding a stator-rotor unit (221, 222) or rotor units, a separate feeder on the input side of the stator-rotor unit or the rotor units for introducing a carrier medium and the chips / Fasem in the refiner and a discharge device on the output side of the stator-rotor unit or the rotor units for discharging the ground chips / fibers with the carrier medium from the refiner, wherein the Schnitzel / fibers pass through the refiner (2, 3) by means of a carrier medium wherein the actual grinding takes place in a plate gap which is located between a stator-rotor unit (221, 222) or between two rotor units of a refiner (22, 32), wherein the stator-rotor unit or the rotor units comprise grinding segments, characterized in that a split supply of the carrier medium is provided, wherein a first of the stator-rotor unit (2 21,222) or the rotor units preceding supply (811, 813; 911, 913) of the carrier medium is arranged on the input side of the refiner (22, 32) and at least one second supply (812, 814; 912, 914) of the carrier medium after the stator-rotor unit (221, 222) or the rotor units on the output side of the refiner (22, 32) is arranged.
    [25]
    25. Refiner according to claim 24, characterized in that the supply of the vaporous / gaseous carrier medium into the refiner is divided into at least two parts, wherein a first part (811, 813, 814, 815, 911, 913) of the supply of the vapor / gas in the refiner in front of the stator-rotor unit (221, 222) or the rotor units, d. H. on the input side, and a second part (812, 814; 912, 914) of the supply of the vapor / gas into the refiner after the stator-rotor unit (221, 222) or the rotor units, i. on the output side, can be introduced.
    [26]
    26. Refiner according to claim 25, characterized in that from the second part of the steam / gas supply, the steam / gas through a first supply line (812, 814, 912, 914) through an outer wall of the refiner housing, most preferably to an exit region of the Refiners (22, 32) on the output side of the refiner, can be introduced.
    [27]
    27. Refiner according to claim 26, characterized in that from the second part of the steam / gas supply, the steam / gas through a second supply line (815, 816) on the output side of the refiner in a blow pipe (9) or in a flow line, through the successive refiner (22, 32) are interconnected, can be introduced.
    [28]
    28. Refiner according to one of the preceding claims 24 to 27, characterized in that the steam / gas on the input side of the refiner via a feed line (811,911) or an inlet line into the refiner (22, 32) can be introduced.
    [29]
    29. Refiner according to claim 28, characterized in that the steam / gas in a crushing zone of the refiner (22, 32), which is arranged on the input side of the refiner in front of the stator-rotor unit (221.222) or the rotor units, can be introduced , Innsbruck, on
    [30]
    August 30, 2011
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    同族专利:
    公开号 | 公开日
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FI20090103A|FI122243B|2009-03-17|2009-03-17|Method and system for grinding wood chips or pulp fibers|
    PCT/FI2010/050134|WO2010106220A1|2009-03-17|2010-02-24|Method, system and refiner for refining of wood chips or pulp fibers|
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