• 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:
    In a process for reclaiming wet organic components containing wastes, especially sludges in a cement clinker production plant, in which raw meal preheated in countercurrent to the hot exhaust gases of a clinker furnace (2) in a preheater (3) and calcined in an alternative fuel calciner (4 ) is calcined, the wet wastes are dried using a hot gas generated from the preheater waste heat in a drying unit (18) and the dried waste and the dryer exhaust gases are discharged from the drying unit (18), wherein the dryer exhaust gases are introduced into the calciner (4) ,
    公开号:AT512113A1
    申请号:T1566/2011
    申请日:2011-10-25
    公开日:2013-05-15
    发明作者:Urs Gasser
    申请人:Holcim Technology Ltd；
    IPC主号:
    专利说明:

    The invention relates to a method for processing wet, organic components containing waste materials, especially sludges in one
    A cement clinker production plant in which raw meal is preheated in countercurrent to the hot exhaust gases of a clinker kiln in a preheater and calcined in an alternative fuel fired calciner, wherein the wet wastes are dried in a drying aggregate using a hot gas generated from the preheater waste heat and the dried wastes and the dryer exhaust gases are discharged from the drying unit.
    The invention further relates to a device for processing wet organic components containing waste materials, in particular sludges in a cement clinker production plant comprising a clinker kiln, at the output end of which a clinker cooler is connected and at the discharge side end a calciner and a preheater are arranged, in which raw meal · is preheated and calcined in countercurrent to the hot exhaust gases of the clinker furnace, and a wet waste drying unit connected to a hot gas line fed by waste heat from the preheater and followed by a separator for separating the drying waste gases from the dried waste is.
    Wet wastes in the context of the invention are those having a water content of> 50% by weight. 30% understood. For example, wet waste containing organic components comes from refineries or coal mines.
    In order to be able to use such waste materials, in particular sludges, which in the worst case have a proportion of volatile organic components of only 0.1 to 0.3%, as alternative fuels in the cement industry, a pretreatment or workup including drying and possibly a grinding required to make it a high quality, powdered and easily dosed, ie dry, get fuel. For example, a ball mill with oversized drying chamber and downstream sifter and filter is suitable. However, the following difficulties arise when energetic synergies with a
    Would like to use the cement clinker production process. In order to ensure that the drying leads to a sufficient reduction of the water content even with a high water content of the wet waste, a high hot gas temperature, which can be regulated depending on the water content, is required. The hot gas must be as inert as possible for safety reasons, with an O2 content of less than 5% is sought. This means that a simple hot gas generator with air dilution is not suitable.
    Typically, therefore, the drying takes place using high-quality expensive fuels, such as natural gas or diesel. It would be more economical to use the waste heat from the preheater of the cement clinker production plant for drying.
    Another difficulty lies in the fact that the volatile organic components formed during drying must be removed from the dryer exhaust gases, inter alia, for reasons of environmental protection and for reasons of odor nuisance. This necessarily requires a downstream
    Oxidation state, i. a thermal cleaning of the drying exhaust gas, which brings with it an additional energy requirement. The use of the dryer exhaust gases with their high water content as combustion air in the main firing of the clinker kiln is not allowed due to the resulting strong cooling of the main flame or the sintering zone. The simple return of the dryer exhaust gases into the clinker furnace via the clinker cooler air blower therefore falls away as a solution for the removal of the volatile organic components.
    In the production of cement clinker raw meal is preheated, residue dried, calcined, fired to clinker and then cooled. After this drying process operating plants consist of preheater, calciner,
    Tertiary air duct, rotary kiln and clinker cooler. The energy input for the conversion in such plants by fuel supply in the rotary kiln and in the calciner. The air heated in the clinker cooler is fed partly as so-called secondary air to the rotary kiln and partly as so-called tertiary air to the calciner. The exhaust gases of the rotary kiln are passed through an oven inlet chamber and a flow restriction, the so-called gutter, to the calciner, flow through this and are discharged together with the calciner generated in the flue gas consisting of flue gas of calciner fuel and CO 2 in the preheater.
    The preheater usually consists of one or more strands and each strand of several cyclone stages, which can each be designed as a floating gas heat exchanger. The dry cement raw meal is fed to the riser of the uppermost cyclone stage, passes through the cyclone stages from top to bottom and is passed from the penultimate (second lowest) cyclone stage into the calciner. In the calciner, the hot raw meal is almost completely deacidified and flows with the calciner exhaust gas in the lowest cyclone stage, is deposited there, fed to the kiln inlet chamber and passes through it as hot meal in the rotary kiln. The hot meal is remuxed in the rotary kiln and burned to clinker during the sintering process.
    The invention now aims to wet waste, especially sludge with a high proportion of volatile organic components, in the context of a
    To work up a cement clinker production process in order to obtain an alternative fuel, wherein for the processing as possible no additional primary fuel use for drying or air purification should be required. Furthermore, the invention should make do with as few structural adaptations of the existing system components.
    To achieve this object, the invention according to a first aspect in a method of the type mentioned is essentially that the dryer exhaust gases are introduced into the calciner. Characterized in that the dryer exhaust gases are passed into the calciner, and preferably preferably substantially exclusively in the calciner, the organic components contained in the dryer exhaust gases are thermally utilized without additional primary fuel use. Since the dryer exhaust gases can have a temperature of less than 100 ° C, the introduction into the calciner leads to a significant cooling in the calciner, which is generally undesirable. The cooling can be avoided in a simple manner by increasing the fuel input in the calciner, the additional amount of fuel can be largely or even exclusively formed by alternative fuels. With the invention, a heat cycle is thus generated in the cement clinker production plant, which is integrated into the conventional gas stream. The heat cycle consists of the hot gas flow, with which the waste heat from the preheater is made available to the drying unit, the exhaust gas flow of the drying unit, which is passed into the calciner, and the calciner exhaust gas flow, which flows into the preheater. The circuit is thereby deprived of heat when passing through the drying unit. Due to the additional introduction of alternative fuels in the calciner, heat is supplied to the circuit to approximately the same extent, so that the total consumption of primary fuel is the same as in a comparable cement kiln plant which has no integrated waste material processing. This means that the primary fuel requirement required in conventional slurry drying and oxidation plants in the invention is completely substituted by alternative fuel. The recycling has the further advantage that an inert atmosphere in the drying unit is ensured without much effort, since the removed from the preheater hot gases always contain less than 5% oxygen.
    In order to reduce the construction costs for the supply of the dryer exhaust gases in the calciner, it is preferred that the introduction of the drying gases into the calciner with the tertiary air takes place. Thus, the tertiary air channel is utilized to introduce the dryer exhaust gases, eliminating the need for a separate feed line into the calciner. * ψ · · · · ♦ · · «· ··· ·· ♦♦ · ·
    In principle, it is conceivable to introduce the dryer exhaust gases directly into the calciner, i. without thermal treatment. However, the direct introduction via tertiary air increases the total heat consumption of the plant, as the dryer exhaust gases are relatively low temperatures (150 ° C and below). An improvement in cost-effectiveness is achieved in this context according to a preferred procedure in that the dryer exhaust gases are passed through the clinker cooler before being introduced into the calciner. As a result, the temperature of the dryer exhaust gases is increased by utilizing the heat of the clinker, and depending on the amount of exhaust gas from the dryer preferably to temperatures of at least 300 ° C. The introduction of the dryer exhaust gases in the clinker cooler, for example, via one of those blowers through which otherwise ambient air is sucked into the clinker cooler. The dryer exhaust gases leave the clinker cooler via the same outlet opening in the radiator ceiling, through which the remaining tertiary air is drawn off and subsequently fed to the calciner.
    A large part of the ambient air sucked into the clinker cooler is introduced into the clinker kiln as so-called secondary air. Now, if the dryer exhaust gases form part of the cooler air, these would partially pass as secondary air in the main flame in the rotary kiln, which can affect the burning process. A preferred development therefore provides that the introduction of the drying exhaust gases into the clinker cooler takes place at a location of the clinker cooler which lies vertically below the tertiary air outlet. By this measure it is favored that the dryer exhaust gases flow through the clinker cooler only in the vertical direction and can be detected mainly by Tertiärluftabzug. • » · · · «··» # · · «« · · ·
    If, as corresponds to a further preferred development, hanging walls in the clinker cooler are arranged in the direction of transport of the clinker before and after the discharge point of the dryer exhaust line, the risk of a part of the dryer exhaust gases entering the secondary air being substantially reduced. For the drying of the wet waste, it is essential that the introduced into the drying unit hot gas has a sufficiently high temperature. The exhaust heat removed at the end of the preheater may not be sufficient for this. A preferred development provides in this context that the discharge of the waste heat of the preheater takes place at at least two different locations of the preheater with mutually different temperature level, so that at least two waste heat flows, and that the temperature of the drying unit fed hot gas by selecting the mixing ratio of the waste heat is set. Thus, if two different temperature levels of the waste heat or the hot gas are available, the possibility is created to regulate the temperature in a simple manner and higher temperatures can be achieved if necessary than with the only withdrawn at the end of the preheater hot gas. In order to obtain waste heat at a higher temperature level from the preheater, it is preferred that the preheater has a plurality of preheater stages and that a waste heat stream of hot gas branched off after the last preheater stage is formed and that the other heat flow is from the outlet of a preheated preheater stage. in particular the first preheater stage diverted hot gas is formed. • · · «« t ·
    The setting of the temperature of the drying unit supplied hot gas is achieved as mentioned by adjusting the flow rates of different hot gases and subsequent mixing of the two hot gas streams. Preference is given to proceeding in such a way that the hot gas streams diverted from the preheater are fed to a mixing cyclone and that the hot flour precipitated in the mixing cyclone is returned to the calciner or the raw meal.
    So that the drying of the wet waste materials is ensured, it is advantageous if the hot gas supplied to the drying unit has a temperature of 300-600 ° C., in particular 500-600 ° C.
    Advantageously, a drying unit is used, which is designed as a grinding dryer, so that both the drying and the grinding can be carried out in an aggregate. It must be ensured that no false air enters the grinding dryer, for which purpose usually an inert sealing gas of low temperature is used. The provision of a sealing gas, which is both inert and cool, is usually only with some procedural effort to deal with. In the context of the present invention, this expense can be significantly reduced in a preferred embodiment by a partial amount of the hot gas is withdrawn before the drying unit and cooled in a heat exchanger with the dryer exhaust gases and that the cooled hot gas is supplied to the drying unit as sealing air.
    To solve the problem underlying the invention is provided according to a second aspect of the invention in a device of the type mentioned that the
    Separator and the calciner are fluidly connected to each other to direct the drying exhaust gases in the calciner. In this case, the fluid connection may either comprise a direct line between the separator and the calciner or lead over existing components and / or internals of the cement clinker production plant. A preferred development provides, for example, that a portion of the fluid connection of the separator with the calciner is formed by a tertiary air channel, which connects the tertiary air outlet of the clinker cooler with the calciner. Furthermore, it can be provided that the fluid connection of the separator with the calciner comprises a dryer exhaust gas line, which opens into the clinker cooler.
    In order to prevent the dryer exhaust gases introduced into the clinker cooler from entering the clinker kiln as secondary air, it is preferably provided that the drier exhaust gas line opens into the clinker cooler at a point which lies below the tertiary air outlet. Another measure is preferably to arrange hanging walls in the transport direction of the clinker before and after the discharge point of the dryer exhaust gas line in the clinker cooler.
    In connection with the extraction or removal of hot gas for the drying unit is preferably provided that the preheater has at least two spaced apart in the flow direction sampling points for branching hot gas via a respective branch line that control members, in particular slide for adjusting the volume flows of the removed hot gas provided are and that the hot gas streams are fed to a mixing device, whose outlet opening with
    - I · · · · · ·: l * * · · ♦ · ················································································································································································································ Hot gas line is connected. Furthermore, it is advantageous if a temperature sensor is provided for measuring the temperature of the hot gas in the hot gas line, the measured values of the temperature sensor being fed to a control device which is connected to the control elements for setting a hot gas temperature of 300-600 ° C., in particular 500 ° -600 ° C. interacts. In the case of a preheater, which has a plurality of preheater stages, in particular suspended gas heat exchangers connected in series, one removal point is preferably arranged after the last preheater stage and the other removal point preferably at the outlet of a preheated preheater stage, in particular the first preheater stage. The mixing device is advantageously formed by a mixing cyclone whose FestStoffaustrag for the excreted hot meal with the calciner or a raw meal or transport is connected.
    The drying unit is preferably designed as a grinding dryer, wherein the infiltration of false air is preferably prevented by leading away from the hot gas line, a branch line for branching off a portion of the hot gas, which opens into a heatable with the dryer exhaust heat exchanger, so that the branched hot gas cooled with the dryer exhaust gases can be, and that is connected to the heat exchanger, a conduit for supplying the cooled hot gas to sealing air connections of the drying unit.
    The invention will be explained in more detail with reference to an embodiment schematically illustrated in the drawing. In the drawing is a
    Cement clinker production plant presented in which ««
    ············································································································································································································································ Clinker furnace 2 is preheated in a preheater 3 and calcined in a calciner 4. The discharge opening of the calciner 4 is connected to the task end of the clinker furnace 2. The clinker leaves the clinker furnace 2 at the point designated 5 and is cooled in a clinker cooler 6. The cooled clinker leaves the clinker cooler 6 at the point designated 7. The preheater 3 may have one or more preheater strands. In the drawing, a strand is shown. The strand has a plurality of series-connected floating-gas heat exchangers, the first floating-gas heat exchanger having 8, the last floating-gas heat exchanger having 9 and the intervening floating-gas heat exchanger 10. The furnace blower 11 generates the required negative pressure so that the Klinkerofenabgas exiting on the hot meal application side 12 of the clinker furnace 2 through the calciner 4 and the successively connected floating-gas heat exchangers 8, 10 and 9 and the hot gas take-off 13 is pulled. The withdrawn hot gas leaves the clinker production plant after passing a hot gas cleaning 14 via the vent 15.
    The firing of the clinker furnace 2, as shown schematically at 16, fuel supplied. The Brennstoffaufgäbe for the firing of the calciner 4 is shown schematically at 17. For the processing of sludge, a grinding dryer 18 is provided, to which the sludges are abandoned at the point 19. To dry the slurry 18 hot gas is supplied via the hot gas line 20 to the mill. The hot gas line 20 is withdrawn from the preheater 3
    Fed hot gas. The hot gas is withdrawn from the preheater 3 at two removal points. The first removal point 21 is located at the outlet of the first suspended gas heat exchanger 8. The branch line provided for the removal of the hot gas from the heat exchanger strand is designated by 22. In the branch line 22, a control member in the form of a slide 24 is arranged, with which the withdrawn hot gas quantity can be adjusted. The withdrawn at the removal point 21 hot gas is fed to a mixing cyclone 25. A second hot gas stream is withdrawn at the removal point 26, which is located after the last suspended gas heat exchanger 9 and after the furnace blower 11. The corresponding branch line 27 likewise has a control element 28 in the form of a slide in order to be able to control the quantity of hot gas withdrawn at the point 26. Also, the withdrawn at the removal point 26 hot gas stream is fed to the mixing cyclone 25. The hot flour excreted in the mixing cyclone 25 is returned to the process via the solids discharge 29 at a suitable point, for example via the furnace flour feed. The hot gas is withdrawn from the mixing cyclone 25 with the aid of the extraction fan 31 and, as already mentioned, fed to the grinding dryer 18 via the hot gas line 20. About the speed of the exhaust fan 31, the milling dryer 18 made available hot gas quantity can be adjusted.
    The temperature of the hot gas conducted in the hot gas line 20 is measured by means of a temperature sensor 32, the measured values of the temperature sensor being fed to a control device 33. The control device 33 is connected via the control lines 34 and 35 to the control elements 24 and 28, respectively, so that the withdrawn at the sampling points 21 and 26 hot gas quantities can be controlled in dependence on the particular desired temperature.
    The dried and ground sludge exiting the mill-drier 18 is fed to a separator 36 as a separator in which the dried, ground sludge is separated from the drier exhaust gas. The dried and ground sludge is discharged from the separator 36 at 37 and may be either stored for later use as a fuel or added directly via a line 38 to the fuel inlet 16 of the main furnace of the clinker furnace 2. The drier exhaust gas is subsequently passed through a filter 39 in which fuel solids are removed from the drier exhaust gas and also fed to the fuel feed. The cleaned dryer exhaust gas is subsequently passed through the dryer exhaust line 40, ensuring dryer exhaust transport through the blower 41.
    The clinker cooler 6 has a plurality of blowers 42 and 43, the dryer exhaust line 40 being connected to the blower 43 so that the dryer exhaust gas is supplied to the clinker cooler 6. The dryer exhaust gas passes through the clinker cooler 6 essentially in the vertical direction and leaves the clinker cooler 6 via the tertiary air outlet 44. In order to prevent the dryer exhaust gas introduced into the clinker cooler 6 from entering the clinker cooler 2 as secondary air, 43 hanging walls 45 are provided before and after the blower 43 arranged. The extracted via the Tertiärluftabzug 44 dryer exhaust gas is introduced together with a portion of the introduced via the blower 42 in the clinker cooler 6 ambient air into the tertiary air duct 46, wherein the 14
    Tertiary air duct 46 in the calciner 4 opens. The dryer exhaust gas introduced into the calciner 4 in this manner is further heated by the calciner firing, with the calciner firing being mainly operated with alternative fuels. This completes the additional heat cycle formed by the integration of the waste treatment according to the invention into the cement clinker production plant. In this heating circuit, the introduced into the calciner 4 dryer exhaust gas is heated in the calciner to temperatures of 700 to 900, in particular 850 ° C and accordingly, the withdrawn at the removal point 21 hot gas has a temperature of about 850 ° C. After passing through the preheater 3, the hot gas at the removal point 26 has a temperature of 250 to 350 ° C, in particular 300 ° C. By selecting the mixing ratio between the hot gas withdrawn at the removal point 21 and the hot gas withdrawn at the removal point 26, the hot gas temperature supplied to the grinding dryer 18 can be set between 250 ° C. and 850 ° C. In practice, however, the temperature of the hot gas supplied to the grinding drier 18 is mostly limited by the temperature resistance of the discharge fan 31, so that maximum temperatures of 550 ° C are realistic. The withdrawn at the outlet of the separator dryer exhaust gas has a temperature of about 100 ° C. By passing the drier exhaust gas through the clinker cooler 6, the temperature of the drier exhaust gas can be raised to values of 300 to 400 ° C, in particular 350 ° C, so that the additional heat required in the calciner, which is required by the introduction of the Is minimized, wherein this additional heat requirement can be easily covered by an increase in the calciner 4 introduced amount of alternative fuels.
    If desired, a subset of the dryer exhaust gas via a branch line 47, bypassing the clinker cooler 6 and the tertiary air duct 46 are abandoned directly. The control member 48 serves to adjust the branched off via the branch line 47 hot gas.
    The sealing air required for the operation of the grinding dryer 18 is formed by a branched off via the line 49 from the hot gas line 20 subset. The hot gas branched off via the line 49 is fed to a heat exchanger 50, in which it is cooled down to values of below 100 ° C. with the dryer exhaust gas. The cooled hot gas is fed to the grinding dryer 18 as sealing air via the sealing air connections 51,
    The modifications of the clinker production plant required for the waste processing according to the invention are limited to the hot gas connections at the removal point 21 and at the removal point 26, the arrangement of the tertiary air removal at the radiator cover and the larger calciner volume. It may also be necessary to have a larger tertiary air duct cross section. The waste processing according to the invention is the most economical way to use large amounts of sludge with a high content of organic components and water. The only real alternative would be to introduce the sludge directly into the calciner, but this would present unpredictable problems in terms of crop variation.
    权利要求:
    Claims (21)
    [1]
    1. A method for processing wet, organic component-containing waste, in particular sludges in a cement clinker production plant, in which raw meal is preheated in countercurrent to the hot exhaust gases of a clinker furnace in a preheater and calcined in an alternative fuel-fired calciner, wherein the wet Waste materials are dried using a hot gas generated from the preheater waste heat in a drying unit and the dried waste and the dryer exhaust gases are discharged from the drying unit, characterized in that the dryer exhaust gases are introduced into the calciner.
    [2]
    2. The method according to claim 1, characterized in that the introduction of the drying exhaust gases takes place in the calciner with the tertiary air.
    [3]
    3. The method according to claim 1 or 2, characterized in that the drying exhaust gases are passed through the clinker cooler before being introduced into the calciner.
    [4]
    4. The method according to claim 3, characterized in that the introduction of the dryer exhaust gases takes place in the clinker cooler at a position of the clinker cooler, which is vertically below the Tertiärluftabzuges.
    [5]
    5. The method according to any one of claims 1 to 4, characterized in that the derivation of the waste heat of the preheater at at least two different locations of the preheater with · * ····· i · * ··· · »» «· IT · English:. German: v3.espacenet.com/textdoc DB = EPODOC & ... PN = EP0458651. English:. German: v3.espacenet.com/textdoc Drying unit supplied hot gas is set by selecting the mixing ratio of the waste heat streams.
    [6]
    6. The method according to claim 5, characterized in that the preheater has a plurality of preheater stages and a waste heat stream of branched after the last preheater stage hot gas is formed and that the other heat flow formed at the outlet of a vorgereihten preheater stage, in particular the first preheater stage branched hot gas becomes.
    [7]
    7. The method according to claim 5 or 6, characterized in that the diverted from the preheater hot gas streams are fed to a mixing cyclone and that the precipitated in the mixing cyclone hot meal is returned to the calciner or the raw meal.
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that the drying unit supplied hot gas has a temperature of 300 - 600 ° C, in particular 500 ° -600 ° C.
    [9]
    9. The method according to any one of claims 1 to 8, characterized in that a partial amount of the hot gas is withdrawn before the drying unit and is cooled in a heat exchanger with the dryer exhaust gases and that the cooled hot gas is supplied to the drying unit as sealing air.


    [10]
    10. The method according to any one of claims 1 to 9, characterized in that the drying unit is designed as a grinding dryer.
    [11]
    11. A device for reprocessing wet, organic components containing waste materials, especially sludges in a cement clinker production plant, in particular for carrying out the method according to one of claims 1 to 10, comprising a clinker furnace (2), at its output end a clinker cooler (6} is connected and a calciner (4) and a preheater (3) are arranged at its feed side end, in which raw meal is preheated and calcined in countercurrent to the hot exhaust gases of the clinker furnace (2), and a wet waste drying unit (18) is connected to a hot gas line (20), which is fed by waste heat from the preheater (3), and is followed by a separator (36) for separating the drying waste gases from the dried waste, characterized in that the separator (36) and the Calculator (4) are fluidly connected to each other to the drying exhaust gases in the calciner (4) to le ites.
    [12]
    12. The device according to claim 11, characterized in that a portion of the fluid connection of the separator (36) with the calciner (4) by a Tertiärluftkanal (46) is formed, the Tertiärluftabzug (44) of the clinker cooler (6) with the calciner (4) connects.
    [13]
    13. The apparatus according to claim 12, characterized in that the fluid connection of the separator (36) with the calciner (4) comprises a dryer exhaust line (40) which opens into the clinker cooler (6). 19


    [14]
    14. The apparatus according to claim 13, characterized in that the dryer exhaust line (40) at a point in the clinker cooler (6) opens, which is below the Tertiärluftabzuges (44).
    [15]
    15. Device according to one of claims 11 to 14, characterized in that the preheater (3) at least two spaced apart in the flow direction of withdrawal points (21,26) for branching off hot gas via a respective branch line (22,27) that control elements ( 24,28), in particular slides are provided for adjusting the volume flows of the withdrawn hot gas and that the hot gas streams are fed to a mixing device (25) whose outlet opening is connected to the hot gas line (20).
    [16]
    16. The device according to claim 15, characterized in that a temperature sensor (32) for measuring the temperature of the hot gas in the hot gas line (20) is provided, wherein the measured values of the temperature sensor (32) of a control device (33) are supplied with the Control elements (24,28) for adjusting a hot gas temperature of 300-600 ° C, in particular 500 ° - 60QaC cooperates.
    [17]
    17. The apparatus of claim 15 or 16, characterized in that the preheater (3) has a plurality of successively connected preheater stages (8,9,10), in particular suspended gas heat exchangers and a removal point (26) after the last preheater stage (9) and the other removal point (21) is arranged at the outlet of an upstream preheater stage, in particular the first preheater stage (8). t 20


    [18]
    18. The apparatus of claim 15, 16 or 17, characterized in that the mixing device (25) is formed by a mixing cyclone whose solids discharge (29) for the precipitated hot meal with the calciner (4) or a Rohmehlaufgabe- or -transporting device (12 ) connected is.
    [19]
    19. The device according to one of claims 11 to 18, characterized in that of the hot gas line (20) leads away a branch line (49) for branching off a portion of the hot gas, which opens into a heatable with the dryer exhaust heat exchanger (50), so that the branched off Hot gas can be cooled with the dryer exhaust gases, and that to the heat exchanger (50) a line for supplying the cooled hot gas to sealing air connections (51) of the drying unit (18) is connected.
    [20]
    20. Device according to one of claims 11 to 19, characterized in that the drying unit (18) is designed as a grinding dryer.
    [21]
    21. Device according to one of claims 11 to 18, characterized in that in the transport direction of the clinker before and after the discharge point of the dryer exhaust line (40) hanging walls (45) in the clinker cooler (6) are arranged. Vienna, 25.10.2011 Applicant

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    同族专利:
    公开号 | 公开日
    US20150020407A1|2015-01-22|
    MX2014005092A|2015-02-10|
    CA3018510A1|2013-05-02|
    AT512113B1|2016-06-15|
    US9453677B2|2016-09-27|
    US20140259732A1|2014-09-18|
    US9273904B2|2016-03-01|
    EP2786974B1|2015-12-23|
    EP2771302A2|2014-09-03|
    ES2563278T3|2016-03-14|
    CN104053636A|2014-09-17|
    AR088519A1|2014-06-18|
    BR112014009931A2|2017-04-25|
    CN104259174A|2015-01-07|
    RU2573657C2|2016-01-27|
    RU2014121107A|2015-12-10|
    AU2014203327B2|2016-04-21|
    EP2786974A1|2014-10-08|
    AU2014203327A1|2014-07-10|
    EP2771302B1|2016-05-25|
    MX361582B|2018-12-11|
    CA2853672A1|2013-05-02|
    RU2658695C1|2018-06-22|
    AU2012328115A1|2014-06-12|
    ES2581732T3|2016-09-07|
    WO2013061127A2|2013-05-02|
    WO2013061127A3|2014-05-01|
    AU2012328115B2|2015-10-29|
    CN104053636B|2017-05-10|
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    法律状态:
    2018-06-15| MM01| Lapse because of not paying annual fees|Effective date: 20171025 |
    优先权:
    申请号 | 申请日 | 专利标题
    ATA1566/2011A|AT512113B1|2011-10-25|2011-10-25|METHOD AND DEVICE FOR REPROCESSING WET, ORGANIC COMPONENTS CONTAINING WASTE MATERIAL|ATA1566/2011A| AT512113B1|2011-10-25|2011-10-25|METHOD AND DEVICE FOR REPROCESSING WET, ORGANIC COMPONENTS CONTAINING WASTE MATERIAL|
    AU2012328115A| AU2012328115B2|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    ES12791242.6T| ES2581732T3|2011-10-25|2012-10-18|Procedure and device for the treatment of wet waste materials, containing organic components|
    ES14001560.3T| ES2563278T3|2011-10-25|2012-10-18|Procedure and device for the treatment of wet waste materials, containing organic components|
    MX2014005092A| MX361582B|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components.|
    CA3018510A| CA3018510A1|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    US14/354,028| US9273904B2|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    PCT/IB2012/002087| WO2013061127A2|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    CN201410391383.XA| CN104259174B|2011-10-25|2012-10-18|For the method and apparatus reprocessing wet, to comprise organic principle waste material|
    RU2015153125A| RU2658695C1|2011-10-25|2012-10-18|Method and device for processing wet waste containing organic compounds|
    BR112014009931A| BR112014009931A2|2011-10-25|2012-10-18|method and device for reprocessing wet waste materials containing organic components|
    CA2853672A| CA2853672A1|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    RU2014121107/03A| RU2573657C2|2011-10-25|2012-10-18|Method and device for processing wet wastes containing organic compounds|
    CN201280064300.5A| CN104053636B|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    EP12791242.6A| EP2771302B1|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    EP14001560.3A| EP2786974B1|2011-10-25|2012-10-18|Method and device for reprocessing wet waste materials containing organic components|
    ARP120103986A| AR088519A1|2011-10-25|2012-10-24|PROCEDURE AND PROVISION TO PROCESS WASTE MATERIALS CONTAINING HUMED ORGANIC COMPONENTS|
    US14/269,551| US9453677B2|2011-10-25|2014-05-05|Method and device for reprocessing wet waste materials containing organic components|
    AU2014203327A| AU2014203327B2|2011-10-25|2014-06-18|Method and device for reprocessing wet waste materials containing organic components|
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