• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    SAMMAN DRAGThe invention relates to a process for drying goods, in particular wood, with hot air, where the drying is divided into at least a first and second sub-process (A, B), in parallel or inseries with each other, and the circulating strains (2) of the two subprocesses in the respectivedrying chambers are conditioned to substantially different water temperatures (TvA) and (TvB), respectively. For reduced energy input, the circulating air (2) in subprocess (A) is assigned a higher water temperature (TvA) than the circulating air in the second subprocess (B) and that enthalpy in the circulating air in the first subprocess (A) is recovered and & errors to the secondsubprocesses (B).(Fig. 1)
    公开号:SE1350429A1
    申请号:SE1350429
    申请日:2013-04-08
    公开日:2014-10-09
    发明作者:Robert Larsson
    申请人:Valutec Ab；
    IPC主号:
    专利说明:

    INProcedure for drying a dryer with hot airThe present invention relates to a process for drying a drying goods, in particular piles collected in stacks, by rewinding with circulating air stream, the condition of whichbrought ante for the quality of the dry goods lamped dry and know temperature through fill supply of heatto the circulating air stream and venting moisture away therefrom. The invention also relates to a duct dryer operating with an externally closed drying duct through which wood in the form of batches of stacked wood with Arline intervals, so-called traction intervals are advanced.
    Air is used as heat-transferring and moisture-transporting drying medium, whichwith a certain temperature, humidity and flow rate are circulated through the dryer withhelped by flattening. The drying air is heated by means of an air heating device which comprises a heating coil. The drying air is brought through the goods to see if moisture and water evaporate from the goods and are taken up by the drying air. In order for the gradually dehumidified drying air circulating in the drying chamber to be able to absorb more water from the goods, it must be dehumidified, which is normaltakes place through ventilation, whereby the air is diluted with cold relatively dry outdoor air - father air.
    When drying travirke, either batch dryers, so-called chamber dryers or progressive dryers, also called duct dryers or continuous walking dryers. In the chamber dryer, the drying takes place in batches in closed chambers. The dryer is filled with wood and the drying then continues until the entire batch is completely dried. In duct dryers or continuoushiking dryers, a stack of wood is loaded at a time and fed step by step through the dryer.
    The drying climate is varied in zones along the drying channel. The drying climate is constantly varied and the drying process is adapted to the wood in the dryer, the desired finished moisture ratio and the desired final quality. The climate of the drying chamber is controlled by regulating a predetermined parameter such as dry and known temperature. The dry temperature is controlled bycontrol of emitted heat from a heating coil while wet temperature is controlled by controlof the degree of opening of ventilation shutters and any watering or steaming equipment. The temperature difference between a dry thermometer and a wet thermometer reflects the relative humidity, whereby a relatively small temperature difference meant a relatively high humidity. In order for the wood to dry, the water that is bound is requiredin and around the cells are transported out of the tree. How fast this happens depends primarily ontemperature and current psychrometer difference, ie. the difference between dry and water temperature, the moisture content of the wood and the air velocity.
    It is {cant that the energy consumption of a drying plant during drying can be reduced by dividing the drying plant into a number of sub-zones and in the most possible way to recoverheat content Iran one zone to another zone that has a momentarily greater heat demand.
    Usually a heat exchanger is used in which the ventilation is carried out in such a way that all the exhaust air (with a higher temperature) from a zone may give off a part of its enthalpy to thePan's draft Valutec2inlet supply air (with lower temperature) to another zone. For efficient energy utilization, in the case of duct dryers, it is advisable to arrange the drying duct in two drying zones in the form of a preheating zone and a main drying zone. With the help of heat exchangers, the heat energy is transferred in the exhaust air, which is ventilated out of the main dryer, to the preheating zone inwhich wood is preheated before it is fed into the main drying zone for controlled and controlled drying.
    In another case, it is possible to mix from the main dryer emitting exhaust air with fresh air from the surrounding atmosphere and use the resulting mixture as supply air to the preheating zone, with the result that the preheating zone works with colder drying air than the main drying zone. The disadvantage of such a procedure with a preheating zone withmoderate drying capacity for sawn troughs is that the risk of drying cracks is great because itthe initial part of the drying process takes place at a relatively low temperature. At this stage of drying, the rigid drying stresses in the wood lead to crack formation, high water temperatures are difficult, the wood then becomes more plastic and the drying stresses are thereby reduced.
    Another complication that can occur when drying wood is that the so-calledThermotolerant stomach fungi due to relatively low temperatures in the preheating stage can tax the wood and form spores during drying. It grows and gives a grass-black discoloration of the wood, which in any case meant that the wood had to be discarded. Through all already initially maintain a relatively hag water temperature of about 50 ° C, meaning that the airdry temperature will vary between 55 and 70 ° C, the living conditions of fungi canand mogel limited. A few hours at these high temperatures is in this part sufficient for all control defta.
    Relatively high energy costs are to be expected in the future and the demand for drying processes with low energy consumption will therefore have to increase sharply. Next comesalso the requirements on the quality of the wood to Increase whereby wood with surface defects in the form of cracks orAcid stains due to mold cannot be accepted.
    A first object of the present invention is therefore to provide a process for drying goods with hot air which is possible in all chamber dryers which duct dryers streamline the drying process and thereby achieve a reducedenergy consumption ,. Another object of the invention is to provide a method fordrying of goods with hot air that makes it possible to avoid wood with surface defects, discolorations or magel. A third object of the invention is to provide a duct dryer which can perform drying with low energy input and makes it possible to avoid wood with surface defects, discolorations.
    These objects of the invention are solved by a process of the kind set forth inclaim 1, a use of the set according to claim 10 and a duct dryer according to claim 11.
    Pan's draft Valutec3The basis for the invention is that a dryer works in the opposite way to what has hitherto been the usual way of drying goods, which especially when it comes to wood meant that in a similar process steps move from a relatively cold drying climate to a warm drying climate. According to the principles of the invention, however, the transformation takes place, namely that underthe process steps range from a relatively warm drying climate to a cold drying climate. The mangathe advantages of drying goods, sarkilt timber, according to this principle will appear in the following.
    An interesting application of the invention consists of a timber drying channel with longitudinal circulation which is divided into two series-connected by a liftable gate.drying zones, where the subsequent second zone is regulated at a tower temperature such asbelow the water temperature in the first zone, and the heat supply for the second sub-process is thanked by all enthalpy, in the form of heat energy from hot moist air from the circulating air in the first zone, Overfors and paralyzed to the second zone via a heating coil arranged in said zone. In addition to energy efficiency has such an arrangementessential benefits which are explained in more detail below.
    An application of the invention in a drying plant with two series-connected processes with different water temperature levels provides - in addition to a substantially reduced heat consumption - an increasingly significant advantage when it comes to drying hay-quality wood in a long-circulation dryer. In a long-distance circulation dryer, the condition of the drying air becomes very highdepending on the evaporation from the wood in the drying channel. Thanks habit a high temperature in itcracks and mold can be avoided in the first zone. Thanks to the habit that no or only a limited amount of air exchange takes place in the first zone, a large part of the energy can be recovered, transferred and used in the subsequent second drying zone. Another advantage is that the Arm storage warehouse in the timber from the first drying zone can be used in the subsequentsecond drying zone.
    The invention will be described in more detail below with reference to the accompanying drawings, in which:Fig. 1 schematically shows a method according to the invention in a first embodiment in which the drying is divided into two sub-processes A, B and the use of a thermal theater extraction system.as Fig. 2 schematically shows a process according to the invention in a second embodiment in which the drying is divided into two sub-processes A, B and a thermal theater recovery system in which a thermal theater recovery system such as Overton heats between the sub-processes through all the different air currents of the subprocesses.
    In Fig. 1, the present invention is shown in a first embodiment as a schematicarrangements that use a liquid medium for all averfora heat between sub-processes. The drying is divided into two sub-processes A and B, respectively, whereby drying in the sub-process APan's draft Valutec4takes place at relatively high water temperature TvA = 50 ° C while drying in sub-process B takes place at relatively low water temperature TvB = 20 ° C. According to the invention, the drying takes place in the sub-process B at a dry temperature TtB which is below the water temperature TvA for drying in the sub-process A, i.e. TtB <TvA. The dry goods 1 in the sub-processes are rewound in separate zones in eachchamber of circulating air drums 2 of drying air, which is provided by means of flakes 3.
    The circulating air in the sub-process A farms on conventional salt with a hot water-supplied heating coil 5. The outside air 6 from the sub-process B can be discharged from the chamber and replaced by fresh supply air 26 which is collected from the surrounding atmosphere. In sub-process A, no air exchange or, if applicable, only a limited one takes place. Subprocess A is workingin all essentials according to the condensation principle whereby in the circulating drying air 2 boundwater vapor is cooled and condensed into a condensate zone by condensation.
    With the aid of a heat theater extraction system, heat can be transferred between the two sub-processes A, B via a heat-carrying liquid medium used / it should be understood that enthalpy is mainly transferred from sub-process A to sub-process B. In the system one in thecondensing heat exchanger 7 arranged in the first sub-process A and a heating coil 8 in the sub-process B. A closed line circuit 9 is arranged to circulate a heat-carrying medium between the condensing heat exchanger 7 in the sub-process A and the heating coil 8 in the sub-process B by means of a circulation pump (not shown). loops 9a, 9b for energy exchange between the circulating drying air in subprocess A and B respectively of the loop9a absorbs heat from condensed water vapor in the drying air in sub-process A and transfers vialoop 9b this heat to the heating coil 8 in subprocess B. The heat consumption for subprocess B is thereby thanked by the enthalpy obtained from condensed water vapor in the circulating air from subprocess A. As the name implies, no or only a limited air exchange with the surrounding atmosphere is required in subprocess A. The combinationof these both arrangements provide an extremely low heat consumption for the drying process as a whole and thanks to the relatively high temperature in sub-process A problems with discoloration and cracks can be avoided. It should be understood that, if necessary, the second drying zone for sub-process B can be equipped with an additional power which can be constituted by a heating coil.
    In Fig. 2, the present invention is shown in a second embodiment as a schematicarrangement as opposed to heat between sub-processes by switching the different air streams of the processes in a heat exchanger of, for example, mofflod or cross-heat type. Just as described above, the drying is divided into two sub-processes A and B respectively / id drying the sub-process A takes place at a relatively high water temperature TvA = 50 ° C while drying in the sub-processB occurs at relatively low water temperature TvB = 20 ° C. According to the invention, the drying takes place insub-process B at a dry temperature TtB which is below the water temperature TvA for drying sub-process A, ie. TtB <TvA. The dry goods 1 in sub-processes A, B are rinsed offPan's draft Valuteccirculating air drums 2, which are produced by means of flakes 3. The circulating air in subprocess A is heated in a conventional manner with a hot water-supplied heating coil 5. The purge air 16 from subprocess A is fed to the heat exchanger 14 in subprocess B and divided after passage into a matte air stream 17 and a condensate stream 18.
    The exhaust air 19 from sub-process B is mixed with the matt air stream 17 at 20 andthe mixture is passed through an external heat exchanger 21, after which the condensate 22 is separated and the matted air stream 23 is divided into a substream 24, which is blown out of the plant and a substream 25, which is used as supply air for the sub-process A with high water temperature. The supply air 26 to sub-process B with low water temperature is preheated inthe heat exchanger 21. The heat color consumption for sub-process B is fully or partially thankedenthalpy in the exhaust air 16 from the sub-process A and no separate external supply air (potassium fresh air from the surrounding atmosphere) to the sub-process A needs to be used. The combination of these bath arrangements provides an extremely low heat consumption for the complex process. It should be submerged if necessary, the second drying zone for sub-process B can be equipped with oneadditional power that can be generated by a heating coil.
    When applying the invention in a long-circulation channel with series-connected zones for drying wood, the drying channel is divided by means of a liftable gate 100 into two adjacent zones I and II which are indicated by dashed contour lines in Fig. 1. As described above, sub-process A is regulated on a high water temperature, e.g. 50 ° C, and zone H asdescribed above for subprocess B at a low water temperature, e.g. 20 ° C. Zone II is challenging asa duct, where the circulating air flows through the wood in countercurrent to the direction of transport of the wood and co-current in the first zone I. It should be understood that the stated direction of the circulating streams is only exemplary and in practice can be varied. The circulating air in zone I farms in a conventional way in heating batteries 5. The drying air in zone Iis dehumidified by passing a condensate heat exchanger located in the circulation stream in zone I.7, where the condensate formed gives off heat to a heat-carrying liquid medium passing through the condensate heat exchanger. The heat given off by frail zone I is transferred via a liquid medium to the heating coil 8 in zone II. Since the drying in sub-process B takes place at a dry temperature TtB which is below the water temperature TvA for drying in sub-process A, ie. TtB <TvA,there is usually no need for additional heat supply from external cold in zone II.
    It should be understood that an embodiment of the invention could comprise a combination of the two exemplary embodiments of the invention described above with reference to Figs. 1 and 2. That is to say according to heat theater recovery systems which partly transfer heat from sub-process A to sub-process B via a heat-carrying liquid medium , partly oneheat theater recovery systems such as Overfor heat from subprocess A to subprocess B through all Axle the different air streams of both subprocesses or to mix these. Furthermore, it should be understood that the invention is applicable to which dryer systems can be divided intoPan's draft Valutec6at least two sub-processes A, B, and regardless of whether the processes are connected in parallel or series with each other for heat transfer. The invention is not limited to what is described above and that shown in the drawings, but can be changed and modified in a number of different ways within the scope of the inventive concept stated in the appended claims.
    Pan's draft Valutec
    权利要求:
    Claims (12)
    [1]
    7 PATE NTKRAV Procedure The drying of goods with hot air is carried out, where the drying is divided into at least a first and second sub-process (A, B), in parallel or in series with each other, and the circulating streams (2) of the two sub-processes in each drying chamber are conditioned to substantially different water temperatures. (TvA) and (TvB), respectively, due to the fact that the circulating air (2) in the first sub-process (A) is assigned a higher water temperature (TvA) to the circulating air in the second sub-process (B) and that enthalpy in the circulating air in the the first sub-process (A) is recovered and transferred to the second sub-process (B).
    [2]
    A method according to claim 1, wherein the second sub-process (B) is assigned a dry temperature (TtB) which is lower than the water temperature (TvA) in the first sub-process (A).
    [3]
    A method according to claim 1, wherein enthalpy in the circulating air in the first sub-process (A) is recovered and transferred to the second sub-process (B) by heat-exchanging circulating air (2) in the two sub-processes (A, B).
    [4]
    A method according to any one of claims 1 - 3, wherein the circulating air (2) in the first sub-process (A) is dehumidified by cooling the vapor vapor bound in the circulating air and causing it to condense in the drying chamber of the sub-process (A).
    [5]
    Method according to claim 4, wherein the drying chamber of the first sub-process (A) is equipped with a condensation heat exchanger (7) with which the circulating air (2) in the first sub-process (A) can be caused to condense out, the drying chamber of the second sub-process (B) is equipped with a heating coil (8) with which the circulating air (2) in the second sub-process (B) drying chamber can be heated, and that a heat-carrying medium is circulated between the condensate heat exchanger (7) in the first sub-process (A) and the heating coil (8) in the second sub-process ( B).
    [6]
    A method according to claim 1, wherein enthalpy of the circulating air in the two sub-processes (A, B) is recovered and transferred by mixing exhaust air strains from the two sub-processes with each other and passing them through the heat exchangers (21) common to the processes. the supply air (26) undergoes the second sub-process (B) and after passage of the heat exchanger (21) the supply air becomes the first sub-process (A). Pan's draft Valutec 8
    [7]
    A method according to claim 6, wherein heat is transferred between the two sub-processes (A, B) by using a heat exchanger (14, 21) of, for example, counterflow or cross-heat type to% / axis air streams comprising supply and exhaust air (25, 26; 16, 19) between the sub-processes.
    [8]
    A method according to any one of claims 1 - 8, wherein a heat theater extraction system is used which on the one hand converts heat from the first sub-process (A) to the second sub-process (B) via a heat-carrying medium of, for example, a liquid in which the circulating air (2) in the first the sub-process (A) is dehumidified by cooling and circulating water vapor bound in the circulating air in the drying chamber of the sub-process (A), and a heat theater extraction system which transfers heat from the first sub-process (A) to the second sub-process (B) through the different sub-processes of the two sub-processes. which includes supply and exhaust air (25, 26; 16, 19) between the sub-processes.
    [9]
    A method according to claim 8, wherein enthalpy in the circulating air in the two sub-processes (A, B) is recovered and transferred by mixing (20) exhaust air drums from the two sub-processes and passing a heat exchanger (21) common to the processes for preheating the supply air (26) for the second sub-process (B) and after passage of the heat exchanger (21) provide supply air for the first sub-process (A).
    [10]
    Use of a method according to any one of claims 1 - 9 in the drying of goods (1) in the form of wood in the plurality for energy transfer in parallel or in series connected batch dryers, so-called chamber dryers or continuous walking dryers so-called duct dryers.
    [11]
    11 Channel dryer working with an outwardly closed drying channel through which wood in the form of batches (1) of stacked wood at regular intervals, so-called tensioning intervals are formed so that a set of timber with palastate moist wood is fed into the channel at the same time as a set of wood with ready-dried wood is fed out of the channel, whereby the sets of wood are coated and passed through drying air (2) circulating in the drying channel. 100) with which the drying channel, when the door is closed, is delimited in a first and a second drying zone (I, II) which each form a chamber which works with circulating drying air, the door (100) having open sets of timber (1). ) is allowed to migrate from the first to the second drying zone, that each chamber is assigned equipment (5, 7, 8; 5, 14, 21) which makes it possible to control and regulate the drying climate in such a way that each chamber forms a first and second sub-process (A, B), and which control and regulation equipment is arranged to allocate the circulating air (2) in the first sub-process (A) to a higher Pan draft Valutec 9 water temperature (TvA ) the circulating air in the second sub-process (B), and allow enthalpy in the circulating air in the first sub-process (A) to be recovered and transferred to the second sub-process (B).
    [12]
    The duct tower according to claim 11, wherein the water temperature (TvA) in the first sub-process (A) is higher than the dry temperature (TtB) in the second sub-process (B) Pan's draft Valutec 9 ° C
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    同族专利:
    公开号 | 公开日
    WO2014168559A1|2014-10-16|
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    SE537903C2|2015-11-17|
    PL2984431T3|2020-04-30|
    EP2984431A4|2016-11-16|
    EP2984431A1|2016-02-17|
    引用文献:
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    SE449788B|1982-04-28|1987-05-18|Flaekt Ab|DRYING FOR DISCOVERY MATERIALS|
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    AT510487B1|2010-10-07|2012-09-15|Mci Man Ct Innsbruck Internationale Hochschule Gmbh|DRYING PROCESS AND DRYING SYSTEM|DE102017108699A1|2017-04-24|2018-10-25|Stela Laxhuber Gmbh|Continuous dryer with a heat exchanger|
    DE102017108697A1|2017-04-24|2018-10-25|Stela Laxhuber Gmbh|Continuous dryer with an exhaust air return device|
    BR112020006580A2|2017-11-28|2020-10-06|Etex Building Performance International Sas|plate drying method and arrangement|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE1350429A|SE537903C2|2013-04-08|2013-04-08|Procedure for drying wood with warm air and a duct dryer|SE1350429A| SE537903C2|2013-04-08|2013-04-08|Procedure for drying wood with warm air and a duct dryer|
    PCT/SE2014/050409| WO2014168559A1|2013-04-08|2014-04-03|Method for drying of timber using warm air|
    PL14782103T| PL2984431T3|2013-04-08|2014-04-03|Method for drying of timber using warm air|
    EP14782103.7A| EP2984431B1|2013-04-08|2014-04-03|Method for drying of timber using warm air|
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