• 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:
    The invention relates to a thermal drying process for pasty products, in particular waste sludge, as well as to a band dryer employing such a process. The principle is to compartmentalize the drying operations and to use, for each of these successive operations, a different air quality: (i) hot air to "grab" the sludge, (ii) low temperature air, then (iii) ) cold air to cool down the sludge before extraction. The present invention provides looping air supply circuits to optimize the energy consumption of the dryer by re-use of energy produced within these circuits. In addition, these loops can recover energy at low temperature fatal or cheap, further optimizing the consumption of the dryer.
    公开号:FR3024725A1
    申请号:FR1457707
    申请日:2014-08-08
    公开日:2016-02-12
    发明作者:Pierre Emmanuel Pardo
    申请人:Degremont SA；
    IPC主号:
    专利说明:

    [0001] The present invention relates to the field of thermal drying of pasty products, for example but not limited to sludge from sewage treatment plants. .
    [0002] State of the Prior Art Waste sludge comprises water and dry matter. The dryness of a sludge indicates its dry matter content. Typically, a mud is pasty when its dryness is between 10 and 25%, it is said to be solid when its dryness is between 25 and 85%, and it is said to be dry when its dryness is greater than 85%. The drying of residual sludge, that is to say their transformation into dry sludge, is useful for their recovery. In particular, dried sludge does not ferment, which favors the conditions of their storage, and they can serve as spreading product or be burned as fuel. Several prior art thermal drying methods are known in the prior art for evaporating the water contained in sludge using the following types of dryer: direct contact dryers performing convective drying by putting a hot fluid, typically a gas, directly in contact with sludge, the indirect contact driers performing conductive drying by transmitting a drying heat to sludge through a wall heated by a coolant, typically a gas or liquid, mixed dryers implementing the principles of dryers with direct contact and indirect contact. The main disadvantage of thermal drying is that its implementation involves a significant energy expenditure, which entails significant operating costs. Typically, current dryers require for the drying of waste sludge an energy of about 900-1100 kWh / TEE (Tons of Evaporated Water). One widely used type of direct contact dryer is a 5-strip dryer. Typically, a belt dryer comprises one or more conveyor belts on which sludge to be dried is placed, where they are subjected to a flow of hot air applied in parallel or perpendicular to their direction of travel. In general, the sludge is previously shaped using an extruder or a granulator to increase the exchange surface. Strip dryers are very robust and easy to operate. However, they have several drawbacks or limitations: to obtain a sludge having a given dryness at the outlet of the dryer, the use of a low drying temperature involves the use of a large dryer stirring a large quantity of air. which generates high electrical consumption, they do not prevent the risk of self-heating sludge because their temperature output dryer can hardly be reduced below 30 ° C to the extent that drying is achieved by flow hot air. Another disadvantage of known belt dryers is that sludge can clog the conveyor belts when the input sludge has insufficient dryness and when the drying temperature used in the dryer is low.
    [0003] Indeed, during its drying, a sludge passes through a plastic phase, typically corresponding to a dryness of 45-55%, during which it becomes viscous and sticky. To overcome this drawback, it is known to recirculate a portion of the sludge, either to prevent them from undergoing the plastic phase within a dryer, or to prepare the sludge upstream so that they are compatible with the technology. drying used. However, recirculation is complicated and difficult to manage. EP 0 781 741 B1 describes a thermal drying system for reducing energy expenditure by reusing a portion of the energy used in a first drying stage. The first stage performs a pre-evaporation step. The second stage of this drying system consists of a belt dryer which reuses the energy of the first stage. Such a drying system with pre-evaporation of sludge makes it possible to obtain reduced consumption of 700-800 kWh / TEE. However, such a two-stage drying system has several drawbacks: it implements two dryers, corresponding respectively to the first stage and the second drying stage, and involves performing a sludge extrusion operation between the two dryers, which requires a high ventilation of this room, energy closures are not optimized taking into account the dryness of the sludge at the end of pre-evaporation stage, typically 40-60%, and the drying temperature required in the second stage, typically 120 ° C, to dry the sludge. Also known in the prior art are drying processes in which low temperature calories, typically 50-90 ° C, of "fatal" heat, i.e. residual in other devices cogeneration, heat pump, boiler, ...), are used to heat a drying fluid of a thermal dryer. However, the fatal heat is generally insufficient to completely dry sludge in strip dryers. The energy consumption of known drying processes using fatal energy therefore remains important.
    [0004] An object of the present invention is to provide a strip thermal drying process optimizing energy consumption. Another object of the present invention is to provide a strip thermal drying process for reducing the size of a strip dryer. Yet another object of the present invention is to provide a strip thermal drying process for strongly cooling sludge before storage. The present invention also aims to provide a strip thermal drying method for drying sludge with low dryness. Another object of the present invention is to provide a strip thermal drying method adapted to any type of sludge, for example but not limited to poorly dehydrated sludge.
    [0005] Yet another object of the present invention is to provide a strip thermal drying process in which the drying of sludge is secured, in particular to prevent risks of self-heating. DESCRIPTION OF THE INVENTION This objective is achieved with a method of thermal drying of pasty products, in particular of waste sludge, comprising: a step of deposition of the pasty products on at least one conveyor belt, the deposition being carried out in a module of input, a step of moving the pasty products from the input module 20 to an output module, the displacement of the pasty products being achieved by moving the at least one conveyor belt, a step of extracting the products at least one conveyor belt, the extraction being carried out in the output module, characterized in that it further comprises, during the displacement step: a high temperature drying step in which the products The pastes are subjected to a high temperature air flow within at least one high temperature drying compartment, followed by a low temperature drying step. wherein the pasty products are subjected to a low temperature airflow within at least one low temperature drying compartment, the low temperature airflow having a lower temperature than the air flow at high temperature, the low temperature drying step occurring after the high temperature drying step. The distribution of the drying operation in several stages and using different air qualities within several compartments makes it possible, when the drying is carried out using a belt dryer, to supply the dryer with low-dry sludge that could not have been dried in a belt dryer without performing a sludge recirculation operation, optimizing the size of the belt dryer. According to an advantageous feature, the air at high temperature is at a temperature above 100 ° C, preferably in the range of 100 to 200 ° C, upon its arrival on pasty products in the at least one drying compartment. at high temperature. According to another advantageous feature, the low temperature air is at a temperature in the range of 20 to 90 ° C upon arrival on the pasty products in the at least one low temperature drying compartment. According to yet another advantageous feature, the pasty products have a dryness of the order of 25-50%, preferably 25-35%, when they pass from the drying step at high temperature to the drying step at 25 low temperature. In an advantageous embodiment, the temperature of the air at low temperature is increased with heat recovered in the air flow exiting the at least one drying chamber at high temperature. In particular, the recovered heat advantageously comprises condensation heat of the moisture contained in the airflow leaving the at least one high temperature drying compartment. It is also possible to heat the drying air at low temperature with fatal heat. These last features make it possible to reduce the energy consumption of a belt dryer. Preferably, the method further comprises successively: a step of drying the air flow at low temperature after contact with the pasty products, a step of heating the dried air flow by passing this flow in thermal contact of a heat pump condenser, this heating step generating a heated air flow, a step of reusing the heated air flow as low temperature air flow. According to an advantageous feature, for the dewatering step the air flow at low temperature is passed through the evaporator of the heat pump.
    [0006] In a preferred embodiment, the low temperature drying air is set at a desired temperature with a heat pump using the evaporator to cool the pasty products having undergone the low temperature drying step. . Thus, the pasty products come out cooled, which promotes their preservation without risk of self-heating. In addition, the heat thus extracted, raised in temperature by the heat pump, is used to bring the air flow to the desired temperature at low temperature.
    [0007] The operation of the heat pump can advantageously be modulated according to fluctuations in the cost of electrical energy. For example, if the electricity is free at night and pays for the day, the heat pump can be started only at night. It is also possible to use the evaporator of the heat pump for a second condensation step of the water contained in the air flow at low temperature after its contact with the pasty products and having already undergone a first condensation step. Here again, by consuming only the modest energy absorbed by the heat pump, a favorable double thermal effect is obtained in the process. Preferably, the power of the heat pump is regulated so as not to exceed a predetermined high temperature threshold for the air leaving the condenser of the heat pump, and the power of the low temperature drying step is regulated. so as not to go below a low temperature threshold of the evaporator of the heat pump. This keeps the heat pump in a temperature range where it is effective.
    [0008] As already mentioned above, but in a more particular embodiment, the process advantageously comprises, after the low temperature drying step, a cooling step in which the pasty products are subjected to a flow of water. cold air within at least one cooling compartment, the cold air flow having a temperature below the temperature of the low temperature air flow, and, preferably, the pasty products are cooled with refrigeration produced at the evaporator of a heat pump which is used the condenser to heat at least partially one of said air flows. According to an advantageous feature, the cold air is at a temperature in the range of -5 to 30 ° C, preferably in the range of 5 to 20 ° C, at its arrival on the pasty products in the at least one compartment of cooling. In a preferred embodiment, the at least one conveyor belt comprises first and second conveyor belts, and the pasty products are deposited on the first conveyor belt during the deposition step and transferred to the second conveyor belt 3024725 During the moving step, the transfer being carried out in a turning module. Typically, pasty products are transferred to the other conveyor belt while their dryness is greater than about 55%, i.e., when they have passed the plastic phase of their drying. The low temperature drying step is preferably performed in a first low temperature drying compartment prior to transfer and in a second low temperature drying compartment after transfer. During the deposition step, the pasty products are preferably deposited in the form of spaghetti on the at least one conveyor belt.
    [0009] The invention also relates to a dryer for carrying out a process according to one or more of the features described above, this dryer comprising: an input module for feeding pasty products to an upstream end of a treatment path, at least one conveyor belt for receiving the pasty products at the upstream end of the treatment path and moving them along the path of the treatment, an output module for extracting the pasty products at one end downstream of the treatment path, behind the input module along the treatment path, at least one high temperature drying module having at least one high temperature drying compartment and at least one high temperature circuit, the at least one less a high temperature circuit being able to generate a flow of air at high temperature within the at least one high temperature drying compartment, between the high temperature drying module and the output module along the treatment path, at least one low temperature drying module having at least one low temperature drying compartment and at least one low temperature circuit the at least one low temperature circuit being adapted to generate a low temperature air flow within the at least one low temperature drying compartment, the low temperature air flow having a temperature of lower than the air flow at high temperature. According to an advantageous feature, the dryer further comprises, between the low temperature drying module and the output module along the treatment path, at least one cooling module, the at least one cooling module comprising at least one a cooling compartment and at least one cooling circuit, the at least one cooling circuit being able to generate a flow of cold air within the at least one cooling compartment, the cold air flow having a temperature below the temperature of the low temperature air flow. According to another advantageous feature, the dryer further comprises at least one turning module capable of transferring the pasty products from one conveyor belt to another conveyor belt at a certain stage along the treatment path. According to yet another advantageous feature, the two conveyor belts are superimposed.
    [0010] The dryer advantageously comprises thermal insulation means between adjacent compartments. Preferably, the dryer comprises means for maintaining in depression at least part of the compartments.
    [0011] In a preferred embodiment, the at least one high temperature circuit comprises at least one condenser capable of condensing at least a portion of the water contained in the air that has passed through the at least one drying compartment. at high temperature, the at least one condenser 3024725 - 10 - serving as a heating means for the flow of air at low temperature. According to an advantageous feature, the air flow at low temperature is heated by said at least one condenser after undergoing a first reheating. According to another advantageous feature, after the outlet of the drying compartment at low temperature, the air flow at low temperature passes through an evaporator of a heat pump and then for said first heating by the condenser of the heat pump . According to yet another advantageous feature, between the outlet of the low temperature drying compartment and said evaporator, the air flow at low temperature passes through an exchanger, in particular with lost water, to partially condense the water contained in the flow of air at low temperature. Thus, the heat pump can be of lower power. As a result, its condenser has a more moderate temperature and therefore its efficiency is better. According to an advantageous feature, the dryer comprises means for cooling the pasty products leaving the drying compartment at low temperature with cold produced by the condenser of a heat pump, in particular that mentioned above. The dryer may comprise at least one low temperature hot water circuit in which water circulates for heating the air stream at low temperature.
    [0012] Advantageously, the water flowing in the at least one low temperature hot water circuit is heated by the at least one moisture condenser present in the high temperature air stream exiting the high drying compartment. temperature.
    [0013] Alternatively, but preferably cumulatively, the water flowing in the at least one low temperature hot water circuit may also be heated by at least one external energy source which may be of fatal origin.
    [0014] In general, it is preferred that the at least one low temperature circuit comprises: means for drying out the low temperature air stream exiting the low temperature drying compartment, a heat pump of which the condenser is mounted to heat the airflow at low dry temperature. In this case, the evaporator of the heat pump is advantageously mounted to dry the flow of low temperature air leaving the drying compartment at low temperature. Alternatively or cumulatively, the evaporator of the heat pump may also be mounted to produce a cooling air flow of the pasty products exiting the low temperature drying compartment. In one embodiment, the dryer comprises a heat exchanger such as lost water or any other cooling means, to ensure at least a primary condensation of the water contained in the flow of air exiting the drying compartment. low temperature. According to another advantageous feature, the cooling circuit and the low temperature circuit have a common part.
    [0015] DESCRIPTION OF THE FIGURES AND EMBODIMENTS Other advantages and particularities of the invention will appear on reading the detailed description of implementations and embodiments that are in no way limiting, and the following appended drawings: FIG. 1 schematically represents In side elevation 35, a first embodiment of a belt dryer and its aeration circuits according to the invention, and FIG. 2 schematically shows in side elevation a second embodiment of a belt dryer. and its air flow circuits according to the invention.
    [0016] The embodiments described hereinafter being in no way limiting, it will be possible to consider variants of the invention comprising only a selection of characteristics described, isolated from the other characteristics described (even if this selection is isolated within a sentence including these other features), if this selection of features is sufficient to confer a technical advantage or to differentiate the invention from the prior art. This selection comprises at least one characteristic, preferably functional without structural details, or with only a part of the structural details if this part alone is sufficient to confer a technical advantage or to differentiate the invention from the state of the art. earlier. In this document, the term "high-temperature drying compartment" refers to a compartment 20 in which high-temperature air is dispensed, the temperature of which is preferably greater than 100 ° C. and preferably between 100 and 200 ° C. ; low-temperature drying compartment a compartment in which low-temperature air is dispensed, the temperature of which is preferably between 20 and 90 ° C .; cooling compartment a compartment in which is passed cold air, whose temperature is preferably between -5 and 30 ° C, and preferably between 5 and 20 ° C. In addition, the terms "high temperature air", "low temperature air" and "cold air" are relative to each other, that is, the high temperature air has a high temperature. higher than the temperature of the air at low temperature, and the air at low temperature has a temperature above the temperature of the cold air. In the terminology used in this document, a circuit includes pipe loops and connecting elements such as condenser, fan, compartment, etc.
    [0017] FIG. 1 represents a belt dryer comprising an upper band 98 and a lower band 99. This band dryer comprises an inlet module 31 designed to deposit pasty products, in particular waste sludge, having for example a dryness content between 16 and 30%. For example, this module 10 receives dewatered sludge from a storage silo, it transforms these sludge shaped spaghetti (extrusion) and then deposits on the upper band 98 of the dryer belt. The sludge deposited on the upper band 98 in the input module 31 is moved by the upper band 98 to a turning module 32 arranged to pass these sludge from the upper band 98 to the lower band 99. The sludge arrivals on the lower band 99 in the turning module 32 are moved by the lower band 99 to an output module 33 arranged to remove the sludge from the dryer.
    [0018] In the embodiment shown in FIGURE 1, the belt dryer includes a high temperature drying compartment 34 adjacent to the inlet module 31. This high temperature drying chamber performs a high temperature drying step, which is that is, "seizing" the sludge with hot air, to prevent the sludge from flowing on the upper web 98. The high-temperature drying compartment 34 located on the upper web 98 is here superimposed a cooling compartment 35 located on the lower band 99. The cooling compartment 35 allows to strongly cool the sludge before discharge through the outlet module 33 which it is advantageously adjacent. Such cooling allows long-term storage without risk, especially in terms of self-heating. The high-temperature drying compartment 34 and the cooling compartment 35 are separated by a mechanical and thermal insulation board. The belt dryer of FIGURE 1 also includes a low temperature drying compartment 36 between, on the one hand, the high temperature drying and cooling compartments 35 and, on the other hand, the overturning module. 32. The high temperature drying, low temperature drying and cooling compartments 34 receive respective air flows via aeration circuits and a heating system described below. High temperature drying module The high temperature drying module designates the high temperature drying compartment 34 and the high temperature circuit to which it is connected. The high temperature circuit is arranged to flow into the high temperature drying compartment 34 from the hot air through a high temperature inlet loop 1 of this compartment 34. This hot air 20 is heated by any suitable heating system. In the example of FIGURE 1, this heating system comprises a heat source 5 and an exchange system 4 consisting for example of an exchanger with oil, steam or other hot media, of combustion fumes (e.g. engine) or an air vein burner.
    [0019] The principle is to circulate heated air through the heating system 4, 5 in the high temperature circuit by means of a fan 8 to supply the high temperature drying compartment 34 via the high temperature inlet loop 1 with air at low humidity at a temperature preferably greater than 100 ° C, and preferably between 100 and 200 ° C in order to quickly and strongly vaporize the water contained in the sludge located on the upper band 98 in the high temperature drying compartment 34. The still hot and moisture-laden air exiting the high temperature drying compartment 34 through the high temperature exit loop 35 2 is controlled in temperature and humidity so as to have an air 3024725 It is close to saturation, typically at 95 ° C and 95% humidity (see "control" section below). The air leaving the high temperature drying compartment 34 through the high temperature exit loop 2 is then dehumidified by condensing the water it contains in a condenser 3. The condensers used can be direct condensers (atomizing spray). water in the mist in lost water, or water spray in the steam and cooling of this water by an external water circuit and extra water circulating) or indirect condensers (water / steam exchangers). Preferably, the belt dryer is sized to recover a water loop 6 at 40-90 ° C, preferably about 70 ° C to capture substantially all of the heat of condensation relative to the heat of the heat. vaporization of the drying module at high temperature.
    [0020] The dehumidified air exits condenser 3 at a typical temperature of 40-90 ° C and is then reheated by the previously described heating system. Part of the dehumidified air is sucked by the fan 40 for a vacuum of the high temperature drying module and a treatment of odors. Low temperature drying module The low temperature drying module refers to the low temperature drying compartment 36 and the low temperature circuit to which it is connected. Cold air circulating in an intermediate loop 15, typically between -10 ° C. and 30 ° C., and preferably 10 ° C., is heated by means of a refrigerating fluid 19 in an exchanger 16 at a temperature of 10-60 ° C, typically 30 ° C. This air is then reheated in an exchanger 17 by the hot water loop 6 produced by the condenser 3 at 40-90 ° C, typically 70 ° C. This hot, very dry air is discharged into the low temperature drying compartment 36 through a low temperature inlet loop 10 connecting the exchanger 17 to the low temperature drying compartment 36. The air extracted from the compartment The low-temperature drying loop 36 at a low temperature exit loop 11 is cold and wet. The water that this air contains is then condensed in a water exchanger 12, for example lost water 13. The water 13 is said to be "lost" because it enters cold 5 and leaves cold or warm without necessarily having the use of this water. The air thus dried out of the exchanger 12 at a controlled temperature of 1040 ° C, typically 20 ° C. The regulation consists mainly in regulating the flow of lost water. The dried air is then further dewatered by condensing the water it contains in the "evaporator" portion 14 of a heat pump 18 to be cooled to a typical temperature of between -10 ° C and 30 ° C. C, preferably 10 ° C. Part of the air of the low temperature circuit is sucked by the fan 40 in order to keep the low temperature drying module in a vacuum. In the example shown in FIGURE 1, this fan 40 is connected to the low temperature output loop 11. Cooling module The cooling module designates the cooling compartment 35 and the cooling circuit to which it is connected.
    [0021] In the embodiment of FIGURE 1, the cooling circuit is partly common with the low temperature circuit since the air flowing into the cooling compartment 35 is a part of the air coming from the evaporator 14. The heat pump 18. In the embodiment of FIG. 2, the cooling circuit is a loop connecting the evaporator 14 of the heat pump 18 and the inlet of the cooling compartment 35. Heat pump In a In a preferred embodiment, the low temperature circuit comprises a heat pump 18 adapted to preheat the air circulating in the low temperature circuit at the heat exchanger 16 in which the condenser of the heat pump 18 provides heat. heat sensitive to the flow of air at low temperature. The heat pump 18 also makes it possible to condense the water contained in the air circulating in this circuit at a very low temperature at the level of the evaporator 14 so as to obtain an extremely dry air at the level of the low temperature loop. In addition, a portion of the cold air produced at the evaporator 14 supplies the cooling compartment 35 through the intermediate loop 15 to cool substantially. the sludge before its extraction in the output module 33. The use of the heat pump 18 is not obligatory. This contributes to the overall good performance of the belt dryer, in particular by creating a very dry air in the low temperature inlet loop 10 which, once heated, allows the use of a low drying rate, or again by the creation of a very cold air in the intermediate loop 15 which makes it possible to cool the sludge in the cooling compartment 35, and by the use of the calories thus extracted to heat very economically one of the flows, in particular the low temperature flow. The cold air injected into the cooling compartment 35 through the intermediate loop 15 is then conveyed into the low temperature drying compartment 36 by the depression created by the suction of the circulation fan 151.
    [0022] In the embodiment of FIGURE 2, another fan 41 draws a portion of the air leaving the exchanger 12 to pass it through the evaporator 14 of the heat pump 18. The other part air leaving the exchanger 12, intended to constitute the low temperature air flow, by-pass the evaporator 14 and goes directly to the condenser 16 of the heat pump. In the same way as described above, the cold, dry air injected into the cooling compartment 35 is then conveyed into the low temperature drying compartment 36 by the depression created by the suction of the fan 151.
    [0023] The invention also relates to such a dryer without heat pump 18, without refrigerating fluid 19, without evaporator 14 and without condenser 16. 3024725 - 18 - Hydraulic circuits Several hydraulic circuits are used in variants of the belt dryer according to the invention. 'invention. In order to control the optimum power of the heat pump 18 before passing through the condenser 16 of the heat pump 18, the exchanger 12, for example with lost water 13, can be put in place. The hot water loop 6 takes part of the heat of the high temperature circuit via the condenser 3 and heats the air 10 of the circuit at low temperature. External energy can be supplied to the hot water loop 6 by means of fatal heat 7 and / or, for example, a boiler 9. An advantage of the hot water loop 6 is that in case of the possibility of recovering fatal heat 7, the air circulating in the circuit at low temperature can be heated free by the exchanger 17. The operation of the exchanger 12 and the circuit 13 can thus be controlled to allow use maximum of this circuit (see the "regulation" section below). In case of fatal heat known from the outset, the dimensioning of the high temperature drying module 20 is adjusted so as not to consume too much noble energy, unless this noble energy is also fatal. Such a hot water loop 6 can cope with all fatal heat recovery situations if they are known from the design. In addition, it is possible to use more or less fatal heat 7 thanks to the possible regulations, in particular by drying less in the drying module at high temperature. The belt dryer according to the invention may be at one or more stages (FIGURES 1 and 2, there are two stages corresponding to the two bays 9 8, 9 9) in order to optimize its specific consumption.
    [0024] Preferably, it is two stages. Dryer Depression As described above, the dryer is depressed to prevent the spread of odors. This depression can be done by a single fan 40 with a set of valves (not shown) to balance the piping between the low temperature circuit passing through the fan 151 and the high temperature circuit passing through the fan 8, or by a fan dedicated to the depression of each of the circuits.
    [0025] Pressure probes (not shown) may be conveniently placed to provide pressure information within the dryer. Such information is important because, firstly, the dryer must not be in overpressure to avoid possible leakage of odors and, secondly, the dryer must not be too strong depression for avoid any air in the dryer, especially in the input module 31, which would greatly change the heat balance. Thermal and Aeraulic Insulation Increased thermal insulation is provided between the high temperature drying compartment 34 and the cooling compartment 35, at least when the dryer comprises more than one strip, so as not to heat the cooling compartment. 35 for sludge cooling.
    [0026] Between the high temperature drying compartment 34 and the low temperature drying chamber 36, insulation is also provided. The purpose of such an insulation is more to prevent excessive air circulation between these two compartments (cooling of the high temperature drying compartment 34 or loss of heat of the high temperature drying compartment 34 by leakage to the compartment of drying at low temperature 36). It is not necessary to have perfect insulation because even if air passed from the high temperature drying compartment 34 to the low temperature drying compartment 36, this air would participate in sludge drying.
    [0027] Preferably, the depression in the low temperature drying chamber 36 is slightly greater (ie, lower pressure) than that of the high temperature drying compartment 34. Number of tapes A single tape can be put in place . In this case, no turning module 32 is implemented and the cooling compartment 35 with its thermal insulation is placed just after one or more drying modules at low temperature. In the case of several belts, for example three or four belts, the principles of arrangement are comparable: three modules (high-temperature drying, low-temperature drying and cooling) are arranged with air circulation compartment cooling to the low temperature drying compartment, and neutral circulation between the high temperature drying compartment and the low temperature drying compartment with a preference for circulation of the high temperature drying compartment to the drying compartment at a low temperature. low temperature.
    [0028] 15 Air Circulation For high temperature, low temperature or cooling drying modules, air circulation can be either from top to bottom or from bottom to top.
    [0029] The air leaving the cooling compartment 35 is directed to the low temperature drying compartment 36 in any zone of this compartment. In addition, the air can flow through the web indifferently from top to bottom, from bottom to top, in the direction of travel of the web or in an opposite direction, and be for example directed by baffles disposed of on both sides of the band in a given compartment. The circuits, especially at high temperature or low temperature, may also include air filters arranged to facilitate unclogging operations or replacement of these filters. Positioning the fans The positioning of the fans 8, 40, 151 on their respective air circuit is not limited to the examples described above. These fans 35 must be able to circulate the air in these circuits and through the exchangers and allow a depression, possibly optimized, in the dryer. The distribution of the air in the high temperature, low temperature and cooling drying modules can be achieved by means of baffles able to distribute the air over the width of the dryer band (s). Furthermore, the high temperature, low temperature drying and cooling modules may consist of identical compartments, and each comprise one or more circulation fans to allow regulation of the air distribution as well as one or more exchangers. Examples of operation Case 1 without free energy and with heat pump In this example, the sludge arrives in the input module 31 with the following characteristics: dryness 20%, temperature 20 ° C, flow rate 2000 kg / h. The drying compartment at high temperature will be dried to a dryness of about 32%, corresponding to a quantity of evaporated water of 750 kg / h. To evaporate this water, the air circuit consists of at least one fan 8 which blows at inlet 1 of the high temperature drying compartment 16 600 Nm3 / h of hot air at 180 ° C. At outlet 2 of the high temperature drying compartment 34, the air has cooled to a temperature of 100 ° C by evaporating water contained in the sludge. In the condenser 3, the loop 6 makes it possible to cool the air of the flow of hot air at a temperature of 80 ° C. The water loop is approximately 75 ° C and has absorbed approximately 626 kW. The hot air is then reheated in the exchange system 4 at 180 ° C, consuming 679 kW via a heat source 5. The water loop 6 warms the air circuit at a low temperature at a temperature of 70 ° C at a flow rate of about 50,000 Nm3 / hr. The outgoing air at 11 of the low temperature drying chamber 36 has a temperature of about 38 ° C and allowed to evaporate all the water to be evaporated which was contained in the sludge to reach the desired dryness.
    [0030] An exchanger 12 supplied with water at 15 ° C makes it possible to reduce the temperature of the air to 20 ° C., which corresponds to the condensation of a large quantity of the water that it contains. In the case where all the air is again dewatered by the heat pump (FIGURE 1), the latter cools the air to a temperature of 10 ° C. and then warms the air up to a temperature of about 32 ° C. About 5,000 Nm3 / h of air is withdrawn at 15 for injection into the cooling compartment 35, and allows the sludge to be cooled to a temperature of about 20 ° C.
    [0031] In this first case, the power consumption of the heat pump is about 70 kWe. The amount of total evaporated water being 1.56 TEE (ton of water evaporated) per hour gives a thermal consumption of 440 kWhth / TEE.
    [0032] 20 Case 2 without free energy and without heat pump Without a heat pump, we will push the drying of the first stage to 35% of dryness increasing the consumption of the first stage of 770 kW approximately. This allows for greater energy recovery on the second stage because it is no longer heated up to 32 ° C by the heat pump but remains at 20 ° C. In this second case, the total thermal consumption is about 500 kWh / TEE and an electrical consumption of 0 (no heat pump).
    [0033] 30 Case 3 with free energy and with heat pump Let's take the case of a free energy from a cogeneration engine that can supply 300 kWhth / TEE, which in our case is 468 kWth. 3024725 - 23 - The best balance of the system is then for a first stage outlet dryness of 26%, requiring a consumption of only 432 kWhth in this first stage.
    [0034] The condensation in the condenser 3 and the addition of dead energy 7 to the water loop 6 makes it possible to meet the needs of the air via the heat exchanger 17 if a heat pump is installed. In this third case, the power consumption of the heat pump is 100 kWe in this case, which gives a thermal consumption of 280 kWh / TEE and 63 kWhe / TEE. Regulation The dryer is sized on the basis of sludge dryness in the inlet module 31, dryness of the sludge at the outlet of the high temperature drying compartment 34 and dryness of the sludge in the sludge module. output 33, so that the energy produced in the condenser 3 is just sufficient to supply the circuit at low temperature 17. Indeed, the optimum of the heat consumption of the dryer is at the point where it is no need to provide outside energy 9 to sufficiently dry the sludge in the low temperature drying compartment. The regulations put in place make it possible to always remain around this optimum while controlling the final dryness of the sludge before extraction from the dryer by the outlet module 33, this depending on the changes in dryness and sludge inlet flow rate. the input module 31. For example, a signal of energy consumption at 9 is given to the dryer, this signal has the effect of increasing within a certain range the air temperature setpoint at the output of the system. exchange 4 in order to increase the drying in the high temperature drying module 34. An on-line meter of the sludge dryness at the outlet module 33 makes it possible to adapt the necessary drying conditions in the low temperature inlet loop. 10 of the low temperature drying compartment 36 and therefore, consequently, the energy demand at 9. In particular, the temperature setpoint in the low temperature input loop 10, o the temperature or humidity setpoint in the low temperature output loop 11 can be set as a function of the dryness of the sludge in the outlet module 33. These setpoints can be controlled by the boiler 9, or any other heating system. additional energy input, which will bring more or less energy. In case of no need for additional energy 9, the installation is regulated automatically. If the water in the loop 6 becomes too hot, for example because the drying requirement of the drying module at low temperature is low (dryness too high) and the air flow in the intermediate loop 15 is decreased, the The condensation in the condenser 3 is less efficient and the heating requirement of the exchange system 4 is lower, automatically decreasing the dryness at the outlet of the high-temperature drying compartment 34. In the event of an excessive increase in the temperature water in the loop 6, for example reaching a state close to the vaporization, or too high temperature at the inlet of the exchange system 4, for example greater than 100 ° C., the temperature setpoint at the outlet of the system exchange 4 by the external energy 5 is automatically controlled to be decreased. In addition, the temperature at the condenser 16 of the heat pump 18 can be measured, for example, on the flow of air leaving the condenser or at the outlet of the condenser for the refrigerant. Indeed, a heat pump is more effective than the temperature difference between the evaporator 14 and the condenser 16 of the heat pump 18 is low. Therefore, for the efficiency of the system, it is better to limit the high temperature of the heat pump, if necessary to complete the heating by another means. As a result, the cold power available at the evaporator of the heat pump is limited. If the temperature increases at the evaporator of the heat pump, it is because the cold power is insufficient to condense the remaining moisture in the air and to produce the cooling air. Since the power required for the cooling air is not directly controllable, the lost water flow rate 13 must be increased to increase drying in the first condensation stage.
    [0035] 5 Control of the heat pump The heat pump 18 takes heat to reach a given set point of cold air temperature (on all or part of the flow). This instruction can come from a sludge temperature measurement in the output module 33.
    [0036] The heating in the condenser 16 of the heat pump 18 is not controlled but is a consequence of the operation of the heat pump 18. The condensation in the exchanger 12 is controlled in order to have a set temperature output of operator-dependent condensation to have drier air which will allow better drying. It will also be possible to adopt a temperature dependent on the desired temperature of the air at the outlet of the heat pump 18. Other regulations such as the speed of displacement of a strip 20 can be put in place, in particular when the dryer comprises many floors. The dryer of the present invention, having a plurality of separate heat loops, provides multiple modulation and final dryness control parameters while consuming a minimum of energy. Of course, the invention is not limited to the examples which have just been described and many adjustments can be made to these examples without departing from the scope of the invention. In addition, the various features, shapes, variants and embodiments of the invention may be associated with each other in various combinations to the extent that they are not incompatible or exclusive of each other. 35
    权利要求:
    Claims (37)
    [0001]
    REVENDICATIONS1. Process for the thermal drying of pasty products, in particular waste sludge, comprising: a step of depositing the pasty products on at least one conveyor belt (98), the deposit being produced in an input module (31), a step of moving the pasty products from the input module (31) to an output module (33), the displacement of the pasty products being achieved by moving the at least one conveyor belt (98, 99), a step of extraction of the pasty products from the at least one conveyor belt (99), the extraction being carried out in the output module (33), characterized in that it further comprises, during the step of moving: a step at high temperature in which the pasty products are subjected to a flow of air at high temperature (1) within at least one high temperature drying compartment (34), then a low temperature drying step in which p pasty products are subjected to a low temperature airflow (10) within at least one low temperature drying compartment (36), the low temperature airflow (10) having a temperature below the high temperature air flow (1), the low temperature drying step occurring after the high temperature drying step.
    [0002]
    2. Method according to claim 1, characterized in that increases the temperature of the air at low temperature (10) with heat (6) recovered in the air flow (2) out of the minus one high temperature drying compartment (34).
    [0003]
    3. Method according to claim 2, characterized in that the recovered heat (6) comprises moisture condensation heat contained in the air flow (2) coming out of the at least one high temperature drying compartment (34).
    [0004]
    4. A method according to one of claims 1 to 3, further comprising, after the step of drying at low temperature, a cooling step in which the pasty products are subjected to a cold air flow (15) at within at least one cooling compartment (35), the cold airflow (15) having a temperature below the temperature of the low temperature airflow (10). 10
    [0005]
    5. Method according to claim 4, characterized in that the pasty products are cooled with cold produced at the evaporator (14) of a heat pump (18) which is used the condenser (16) to heat the one of said air flows. 15
    [0006]
    6. Method according to one of claims 1 to 5, characterized in that the drying air is heated at low temperature with a heat pump (18) which is used the evaporator (14) to cool the pasty products having undergone the drying step at low temperature. 20
    [0007]
    7. Method according to claim 6, characterized in that the evaporator (14) of the heat pump (18) is also used for a second condensation step of the water contained in the low airflow. temperature having already undergone a first condensation step. 25
    [0008]
    8. Method according to claim 7, characterized in that regulates the power of the heat pump (18) to not exceed a predetermined high temperature threshold for the air leaving the condenser (16) of the heat pump (18), and in that the power of the low-temperature drying step is controlled to not exceed a low temperature threshold of the evaporator (14) of the heat pump (18).
    [0009]
    9. Method according to one of claims 1 to 8, wherein the low temperature air (10) is heated with fatal heat (7). 3024725 - 28 -
    [0010]
    10. A method according to one of claims 1 to 9, further comprising successively: a dewatering step of the air flow at low temperature (11) after its contact with the pasty products, a step of heating of the flow of dry air by passing this flow into thermal contact of the condenser (16) of a heat pump (18), this heating step generating a heated air flow, a step of reuse of the flow heated air as low temperature airflow.
    [0011]
    11. The method of claim 10, characterized in that for the dewatering step is passed the air flow at low temperature by the evaporator (14) of the heat pump (18). 15
    [0012]
    12. Method according to one of claims 1 to 11, characterized in that the high temperature air (1) is at a temperature above 100 ° C, preferably in the range of 100 to 200 ° C, at its temperature. arriving at the pasty products in the at least one high temperature drying compartment (34).
    [0013]
    13. Method according to one of claims 1 to 12, characterized in that the low temperature air (10) is at a temperature in the range of 20 to 90 ° C on arrival on pasty products in the minus a low temperature drying compartment (36).
    [0014]
    Process according to one of Claims 4 to 13, characterized in that the cold air (15) is at a temperature in the range of -5 to 30 ° C, preferably in the range of 5 to 20 ° C at its arrival on the pasty products 30 in the at least one cooling compartment (35).
    [0015]
    15. Method according to one of claims 1 to 14, characterized in that the pasty products have a dryness of the order of 25-50%, preferably 2535%, when they go from the drying stage to high temperature at step 35 of drying at low temperature. 3024725 - 29 -
    [0016]
    16. Method according to one of claims 1 to 15, characterized in that the pasty products are deposited on a conveyor belt (98) during the deposition step and transferred to at least one other conveyor belt (99) during the displacement step, the transfer being performed in a turning module (32), the pasty products being transferred to the at least one other conveyor belt (99) while their dryness is greater than about 55%. 10
    [0017]
    17. The method of claim 16, characterized in that the low temperature drying step is performed in a first low temperature drying compartment before the transfer and in a second low temperature drying compartment after the transfer. 15
    [0018]
    18. Method according to one of claims 1 to 17, characterized in that, during the deposition step, depositing the pasty products in the form of spaghetti on the at least one conveyor belt (98).
    [0019]
    19. Dryer for carrying out a process according to one of claims 1 to 18, comprising: an input module (31) for feeding pasty products to an upstream end of a treatment path at least one conveyor belt (98, 99) for receiving the pasty products at the upstream end of the treatment path and moving them along the treatment path, an output module (33) for extracting the products. pasted at a downstream end of the treatment path, behind the inlet module (31) along the treatment path, at least one high temperature drying module having at least one high temperature drying compartment (34) and at least one high temperature circuit, the at least one high temperature circuit being adapted to generate a high temperature air flow (1) within the at least one high temperature drying compartment (34), 3024725 - 30 - between the module of drying at high temperature and the output module along the treatment path, at least one low temperature drying module having at least one low temperature drying compartment (36) and at least one low temperature circuit, the at least one low temperature circuit being capable of generating a low temperature air flow (10) within the at least one low temperature drying compartment (36), the low temperature air flow ( 10) having a lower temperature than the high temperature air flow (1). 10
    [0020]
    20. Dryer according to claim 19, further comprising, between the low temperature drying module and the output module (33) along the treatment path, at least one cooling module, the at least one cooling module. comprising at least one cooling compartment (35) and at least one cooling circuit, the at least one cooling circuit being adapted to generate a cold air flow (15) within the at least one compartment of cooling, the cold air flow (15) having a temperature below the temperature of the low temperature air flow (10). 20
    [0021]
    21. Dryer according to claim 19 or 20, further comprising at least one turning module (32) adapted to transfer the pasty products of a conveyor belt (98) to another conveyor belt (99) at a certain stage along of the treatment path. 25
    [0022]
    22. Dryer according to claim 21, characterized in that the two conveyor belts (98, 99) are superimposed.
    [0023]
    23. Dryer according to one of claims 19 to 22, characterized in that it comprises thermal insulation means between adjacent compartments.
    [0024]
    24. Dryer according to one of claims 19 to 23, characterized in that it comprises means (40) for maintaining a depression at least part of the compartments. 3024725 - 31 -
    [0025]
    25. Dryer according to one of claims 19 to 24, characterized in that the at least one high temperature circuit comprises at least one condenser (3) capable of condensing at least a portion of the water contained in the exhaust air (2) within the at least one high temperature drying compartment (34), the at least one condenser (3) serving as a heating means for the low temperature air flow (10) .
    [0026]
    26. Dryer according to claim 25, characterized in that the flow of low temperature air (10) is heated by said at least one condenser (3) after undergoing a first reheating.
    [0027]
    A dryer according to claim 26, characterized in that after the outlet of the low temperature drying compartment (36), the low temperature air flow (11) passes through an evaporator (14) of a heat pump (18) and then for said first heating by the condenser (16) of the heat pump (18).
    [0028]
    28. Dryer according to claim 27, characterized in that, between the outlet 20 of the low temperature drying compartment (36) and said evaporator (14), the low temperature air flow (11) passes through a heat exchanger (12), in particular lost water (13), for partially condensing the water contained in the low temperature air flow (11). 25
    [0029]
    29. Dryer according to one of claims 26 to 28, characterized in that it comprises means for cooling the pasty products leaving the drying compartment at low temperature (36) with cold produced by the evaporator (14) d a heat pump (18). 30
    [0030]
    30. Dryer according to one of claims 19 to 29, characterized in that it comprises at least one low temperature hot water circuit (6) in which water circulates for heating the air flow. at low temperature (10). 3024725 - 32 -
    [0031]
    31. Dryer according to claim 30 and one of claims 25 to 29, characterized in that the water flowing in the at least one low temperature hot water circuit (6) is heated by the at least one condenser (3). 5
    [0032]
    32. Dryer according to claim 30 or 31, characterized in that the water flowing in the at least one low temperature hot water circuit (6) is heated by at least one external energy source (7, 9). .
    [0033]
    A dryer according to one of claims 19 to 32, characterized in that the at least one low temperature circuit comprises: means for drying out the low temperature air flow (11) exiting the drying compartment at a low temperature (36), a heat pump (18), the condenser (16) of which is mounted to heat the air stream at low dry temperature. 15
    [0034]
    34. Dryer according to claim 33, characterized in that the evaporator (14) of the heat pump (18) is mounted to dry the low-temperature air flow (11) leaving the drying compartment at low temperature. (36).
    [0035]
    35. Dryer according to claim 33 or 34, characterized in that the evaporator (14) of the heat pump (18) is mounted to produce a cooling air flow pasty products leaving the drying compartment at low temperature (36).
    [0036]
    36. Dryer according to one of claims 33 to 35, characterized in that it comprises a heat exchanger (12) such as lost water (13), to ensure at least a primary condensation of the water contained in the airflow (11) exiting the low temperature drying compartment (36).
    [0037]
    37. Dryer according to one of claims 20 to 36, characterized in that the cooling circuit and the low temperature circuit have a common part. 20 25 30 35
    类似技术:
    公开号 | 公开日 | 专利标题
    EP3177884B1|2018-12-05|Method and facility for thermally drying pasty products
    EP2504649B1|2014-04-02|Method and facility for drying slurry-like materials, in particular sludge from wastewater treatment plants
    CA2805733A1|2012-02-09|Method and installation for drying sludge
    EP0077715B1|1985-02-20|Modulated dryer for drying grain
    FR2979974A3|2013-03-15|METHOD AND SYSTEM FOR TREATING COMBUSTION GAS FROM A HEAT SOURCE
    FR2994101A1|2014-02-07|Treating warm humid air discharged from grain dryer during process of drying e.g. corn grains, comprises transferring heat to hot air of coolant to condense moisture and/or volatile components, and collecting condensate and particles
    WO2011124806A1|2011-10-13|Seawater desalination plant operating by multiple-effect distillation
    EP0119931B1|1988-09-28|Process and apparatus for continuous drying, adapted to the use of heat pumps
    EP0251936A1|1988-01-07|Process and device vegetable materials with high-pressure steam
    FR2509763A1|1983-01-21|METHOD FOR OPERATING A CALENDER WITH HEATED BOWLS AS WELL AS A CALENDER FOR CARRYING OUT THIS METHOD
    FR3054026A1|2018-01-19|METHOD FOR COOLING AND / OR DRYING GRAINS IN A DRYER, INSTALLATION FOR IMPLEMENTING THE PROCESS
    FR2960870A1|2011-12-09|Drying pasty materials such as sludge from treatment plants, comprises subjecting sludge exiting from electrode hydration to laying operation that is moderated to preserve structure of sludge present in outlet of electro dehydration
    EP0233826B1|1990-04-25|Method and device for the recovery of heat from installations emitting steam-laden hot air and steam, and for increasing the productivity of these installations
    FR3061279B1|2019-09-20|DEVICE FOR THERMALLY DRYING A PRODUCT BY CONVECTION AND HEAT PUMP AND ASSOCIATED METHOD
    FR2965338A1|2012-03-30|Drying humid material e.g. sludge from waste water treatment/compost using air as coolant fluid operating in circuit, by preheating material, introducing fresh air into circuit for circulation, and heating part of air using solar collector
    FR2996292A1|2014-04-04|VENTILATION AND HEATING SYSTEM OF A BUILDING, WITH IMPROVED PERFORMANCE
    FR2476817A2|1981-08-28|Solids dryer fitted with heat economiser - has tower with water spray nozzles from heater spraying over cold air discharge
    WO2012090135A1|2012-07-05|Method and facility for drying pasty products, in particular wastewater treatment plant sludge
    FR2526139A1|1983-11-04|Drier for plate material - has fans giving top contra-flow air current in three drier zones
    FR2480418A1|1981-10-16|Low temperature dryer with two compartments - has heated air flowing through both sections with articles travelling on conveyor with serpentine path of travel
    FR2960871A1|2011-12-09|Drying pasty materials e.g. sludge from treatment plant, by subjecting sludge exiting from mechanical dehydration by pressing to laying operation that is moderated to preserve structure of sludge present in outlet of mechanical dehydration
    FR2614092A1|1988-10-21|Method and installation for drying a moist product
    FR2510734A1|1983-02-04|Wet scrubber and cooler for exhaust fumes from malt house - recycles wash water through heat exchanger cooled by heat pump evaporator
    FR2778455A1|1999-11-12|Ice rink creation and maintenance using an energy efficient process
    WO2008029023A1|2008-03-13|Effluent treatment method and treatment plant employing such a method
    同族专利:
    公开号 | 公开日
    CN107076513A|2017-08-18|
    EP3177884B1|2018-12-05|
    CN107076513B|2020-02-11|
    EP3177884A1|2017-06-14|
    US10746466B2|2020-08-18|
    ES2714024T3|2019-05-24|
    FR3024725B1|2020-11-13|
    US20170227288A1|2017-08-10|
    WO2016020829A1|2016-02-11|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE19825597A1|1998-06-09|1999-12-16|Alb Klein Umwelttechnik Gmbh|Sludge drying plant operating in two stages and recycling waste heat|
    WO2001058815A2|2000-02-08|2001-08-16|Erich Netzsch Gmbh & Co. Holding Kg|Method and device for drying liquid to damp substances which have already been subjected to preliminary dehydration|
    WO2004046629A1|2002-11-15|2004-06-03|Klein Abwasser- Und Schlammtechnik Gmbh|Method for convection drying|
    WO2011061715A1|2009-11-23|2011-05-26|Degremont|Method and facility for drying slurry-like materials, in particular sludge from wastewater treatment plants|
    DE505017C|1926-11-11|1930-08-12|Werner Brunnschweiler|Channel stage dryer|
    US3066030A|1960-06-13|1962-11-27|Gerber Prod|Method of preparing dried foods|
    FR2302048B1|1975-02-25|1977-10-28|France Luzerne|
    CH609214A5|1976-10-05|1979-02-28|Escher Wyss Gmbh|Gravity drier for free-flowing material, in particular seed kernels|
    GB2064099A|1979-11-29|1981-06-10|Prestcold Ltd|Dehumidifier; Air Conditioner; Drier|
    DE3013703A1|1980-04-10|1981-10-15|Lambrecht, Jürgen, Dipl.-Ing., 8026 Irschenhausen|Multistage grain drying chamber - uses passing of extracted hot air to common heat pump for return through individual channels|
    DE3013820A1|1980-04-10|1981-10-15|Jürgen Dipl.-Ing. 8026 Irschenhausen Lambrecht|Drying system with energy recuperation - uses main heat pump followed by auxiliary modular heat pump units in axial arrangement|
    EP0079523A1|1981-11-06|1983-05-25|Etablissements NEU Société Anonyme dite:|Drying apparatus using several energy sources|
    US4472887A|1982-12-14|1984-09-25|Tagus Ranch|System and method for dehydrating produce|
    AT182571T|1995-12-27|1999-08-15|Innoplana Umwelttechnik Ag|SLUDGE PROCESSING METHOD|
    US6539645B2|2001-01-09|2003-04-01|Mark Savarese|Drying apparatus and methods|
    CN101786784B|2010-03-26|2012-03-28|广州新滔水质净化有限公司|Solar energy and recycled water dual-heat-resource heat pump sludge drying system|
    EP2455526A1|2010-11-17|2012-05-23|BSH Bosch und Siemens Hausgeräte GmbH|Machine comprising a heat pump and related set of processes|
    CN202132965U|2011-07-20|2012-02-01|上海机易电站设备有限公司|Fuel-gas drying direct-firing pulverizing system with lignite-fired fanlike coal pulverizer|
    CN103749670B|2014-01-17|2015-03-18|福建诚德农业机械有限公司|High-efficiency energy-saving grain drying machine and drying method|CN106642146B|2017-02-27|2019-01-15|北京中技圣火环保科技有限公司|A kind of rubbish air-dries processing system and method|
    AT520600B1|2017-10-19|2021-07-15|Muehlboeck Holztrocknungsanlagen Gmbh|Device and method for drying bulk material|
    CN108689578A|2018-06-22|2018-10-23|张传赛|A kind of sludge rapid draing processing unit|
    DE102018133070B4|2018-12-20|2021-08-05|i +M GmbH & Co. KG Innovation und Management|Device for drying sewage sludge|
    CN111847834A|2020-07-21|2020-10-30|上海仁创环境科技有限公司|Cooling drying method and treatment equipment for sludge after heat drying|
    CN112452124A|2020-12-11|2021-03-09|石家庄市新星化炭有限公司|Drying denitration method in carbon black production and carbon black production system|
    法律状态:
    2015-11-12| PLFP| Fee payment|Year of fee payment: 2 |
    2016-02-12| PLSC| Search report ready|Effective date: 20160212 |
    2016-08-01| PLFP| Fee payment|Year of fee payment: 3 |
    2017-07-28| PLFP| Fee payment|Year of fee payment: 4 |
    2018-07-30| PLFP| Fee payment|Year of fee payment: 5 |
    2019-08-26| PLFP| Fee payment|Year of fee payment: 6 |
    2020-08-25| PLFP| Fee payment|Year of fee payment: 7 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1457707A|FR3024725B1|2014-08-08|2014-08-08|PROCESS AND INSTALLATION FOR THERMAL DRYING OF PASTA PRODUCTS|FR1457707A| FR3024725B1|2014-08-08|2014-08-08|PROCESS AND INSTALLATION FOR THERMAL DRYING OF PASTA PRODUCTS|
    US15/501,977| US10746466B2|2014-08-08|2015-08-03|Method and facility for thermally drying pasty products|
    CN201580049021.5A| CN107076513B|2014-08-08|2015-08-03|Method and apparatus for thermal drying of pasty products|
    ES15757343T| ES2714024T3|2014-08-08|2015-08-03|Procedure and installation of thermal drying of pasty products|
    EP15757343.7A| EP3177884B1|2014-08-08|2015-08-03|Method and facility for thermally drying pasty products|
    PCT/IB2015/055887| WO2016020829A1|2014-08-08|2015-08-03|Method and facility for thermally drying pasty products|
    [返回顶部]