• 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 present invention relates to the field of heat treatment of a product to be dewatered such as sludge from a wastewater treatment die. The present invention relates more particularly to a method and a drying installation of such a product for carrying out a hydrothermal carbonization operation on reactor 1 followed by a filtering and drying operation, preferably on a heated press-filter 6. To dry this product in the heated filter press 6, circulates a heat transfer fluid from a heat exchanger 2. The heat exchanger 2 is arranged to transfer to the coolant at least a portion of the heat contained in the product to be dewatered leaving reactor 1.
    公开号:FR3035190A1
    申请号:FR1553500
    申请日:2015-04-20
    公开日:2016-10-21
    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 heat treatment of a product to be dewatered such as sludge from a water treatment sector. waste.
    [0002] The present invention relates more particularly to a method of drying such a product by hydrothermal carbonization and by filtering. The present invention also relates to a drying installation for implementing such a method.
    [0003] STATE OF THE PRIOR ART In the prior art, a drying process combining a hydrothermal carbonization operation and a filtering operation is known. Document WO 2015/008219 A1 describes an installation comprising a reactor and a filtering medium connected in series. A product to be dewatered type sludge can be introduced into the reactor and is kept under pressure at a temperature close to 200 ° C so as to perform said hydrothermal carbonization operation. In this installation, the carbonized product leaving the reactor is successively cooled, decompressed and filtered.
    [0004] A disadvantage of this type of facilities and processes is that they do not allow drying a product to be dehydrated to a dryness value for optimal thermal recovery of this product, typically a dryness of 90%. An object of the present invention is to provide a method and a drying installation optimizing the energy consumption while being able to dry a product to be dehydrated to a dryness value of between 50 and 95% depending on the final needs. SUMMARY OF THE INVENTION This object is achieved with a method of drying a product to be dewatered, comprising moving the product to be dewatered in an industrial process path, said path comprising a reactor and a heat exchanger. the path further comprising a mechanical compression system, the method comprising: a thermal conditioning step, hydrothermal carbonization type, during which the product to be dehydrated in the reactor is maintained at a carbonization pressure P0, preferably between 0.6 and 3.5 MPa, and at a carbonization temperature TO, preferably between 140 and 300 ° C., a heat transfer stage during which, via the heat exchanger, heat, is transferred to a coolant, for example water, at least a portion of the heat contained in the product to be dehydrated having undergone the conditioning step t hermetic, a step of mechanical dehydration during which: o is introduced into the mechanical compression system the dehydrated product having undergone the heat conditioning step and the heat transfer step, where the product to be dehydrated is compressed contained in the mechanical compression system 20 by application of a dehydration pressure P1, preferably greater than 0.5 MPa, and a liquid fraction of the product to be dehydrated is discharged, the liquid fraction being separated from the product to be dehydrated under effect of its compression, and a heating step during which the product to be dehydrated is transferred to at least a portion of the heat contained in the heat transfer fluid having undergone the heat transfer step, this heating step being carried out jointly or after the mechanical dehydration step. Preferably, the mechanical compression system is a heating press-filter comprising at least two trays and: during the mechanical dehydration stage, the compression of the product to be dehydrated is carried out against at least one of said trays, and during the heating step, the heat transfer fluid 5 having undergone the heat transfer step is circulated in channels formed in at least one of said trays, this at least one of said trays corresponding preferably to the at least one said trays against which the product to be dehydrated is compressed.
    [0005] Such a drying process makes it possible to recover energy evacuated by the heat exchanger and to use this recovered heat to dry the product to be dehydrated in the heated filter press. In known methods of the state of the prior art as represented by the document WO 2015/008219 A1, this evacuated energy is lost. Consequently, the present invention makes it possible to optimize the energy consumption by reusing this evacuated energy. In addition, the use of a heated filter press is particularly advantageous for drying a carbonized product, that is to say having undergone a hydrothermal carbonization type thermal conditioning step.
    [0006] Indeed, the drying by filter press heating generally causes difficulties in terms of: heat transfer from the heating plate (s) to the product to be dehydrated contained in the heated filter press, and (d) evacuation of the water vapor generated in the heating filter press during such drying. When the dewatered product is a sewage sludge entering the heated press filter with a dryness of 20%, the heating time required to reach a dryness of 90% can be extremely long, typically twelve hours. Thus, the design of a heated filter press is more conditioned by its drying function than by its filtration function. This results in a relatively rare implementation of drying by filter press heating. However, when the amount of water to be evaporated is low, this phenomenon is minimized. In this respect, it is advantageous to use a heated filter press to dry a carbonized product during a prior hydrothermal carbonization step, the carbonized product introduced into the heated filter press being able to dry out. between 50 and 65%. The thermal consumption of a heated filter press is of the order of 1000 kWh / tEE for drying a sludge having about 20% dryness, of which about 15% comes from the heating stage itself. In the present process, it is estimated that the consumption to dry a sludge having about 65% dryness is of the order of 363 kWH / tMS. By estimating an available energy at the outlet of the reactor (temperature of the carbonized product) of 175-350 kWh / tMS, it is possible to cover the energy requirements to carry out the heating step. Preferably, the product to be dewatered is a sewage sludge resulting from a wastewater treatment.
    [0007] Advantageously, the heat transfer step can be carried out by circulating: the coolant and the product to be dehydrated in the heat exchanger, and the heat transfer fluid in a circulation loop, preferably closed, passing through the heat exchanger, the heat transfer fluid being circulated in the circulation loop by driving a circulation pump, and the circulation pump and / or the heat exchanger can be controlled to lower the temperature of the product to be dehydrated to a filtration temperature T1, preferably less than 90 ° C, preferably between 50 and 70 ° C. On the one hand, such a T1 filtration temperature is compatible with some heated filter press technologies, particularly with membrane heated filter press membrane materials. On the other hand, such a filtration temperature T1 optimizes the filterability of the filter press and heating energy consumption of this equipment. According to an advantageous characteristic, at least a portion of the heat transfer fluid which has undergone the heat transfer step can be stored in a flask, and the heat transfer fluid used during the heating step is, at least in part , taken from this balloon.
    [0008] Such a balloon makes it possible to store at least a portion of the heat required to carry out the heating step with the heating filter press. Such storage is particularly advantageous in view of the nature of the hydrothermal carbonization operation, which may be continuous or discontinuous, and the discontinuous nature of the operation of the heating filter press. According to another advantageous characteristic, it is possible to heat the coolant before it is used in the heating step by means of an additional heat source, for example a boiler. Such an additional heat source makes it possible to complete the need for the heated filter-press to carry out the heating step, depending on the size of the balloon.
    [0009] Advantageously, during the mechanical dehydration step, an internal space of the mechanical compression system accommodating the product to be dehydrated can be depressed and the gases or vapors thus extracted can be channeled to a steam treatment system. Such a method thus makes it possible to manage the odors emitted by the use of the heated filter press, in particular when the product to be dewatered is a sewage sludge. According to yet another advantageous characteristic, a heating time D0 is preferably set, the heating duration D0 corresponding to the duration of implementation of the heating step, so that the dryness of the product to be dehydrated contained in the mechanical compression system reaches or exceeds a final dryness Sf, preferably between 50 and 95%, at the end of this heating step. Such a characteristic makes it possible to dry the product to be dehydrated according to the final needs, and thus to optimize the energy consumption of the process.
    [0010] The present invention also relates to a drying installation comprising: a reactor arranged to store the product to be dehydrated and maintain it at a carbonization pressure PO, preferably between 0.6 and 3.5 MPa, and at a carbonization temperature TO, preferably between 140 and 300 ° C, and a heat exchanger arranged to transfer to a heat transfer fluid at least a portion of the heat contained in the product to be dewatered leaving the reactor, characterized in that it comprises furthermore: a mechanical compression system comprising: an interior space arranged to receive the product to be dehydrated; a compression means, for example a membrane, capable of compressing the product to be dehydrated contained in the mechanical compression system; a filtrate outlet outlet arranged to evacuate a liquid fraction of the product to be dehydrated during its compression, heating means e arranged to transfer to the product to be dehydrated, within the mechanical compression system or downstream of the mechanical compression system, at least a portion of the heat contained in the heat transfer fluid from the heat exchanger.
    [0011] Preferably, the mechanical compression system is a heating press-filter comprising at least two trays, the compression means being arranged to compress against against at least one of said trays the product to be dehydrated contained in the heating filter-press, 3035190 - 7 and at least one of said trays comprises channels capable of receiving a heating liquid, the installation being arranged so that said heating liquid consists, at least in part, of the coolant coming from the heat exchanger, the heating means 5 comprising said channels. According to an advantageous characteristic, the installation may furthermore comprise an additional heat source capable of heating the heat transfer fluid before it arrives in the heating means.
    [0012] According to another advantageous characteristic, the installation may furthermore comprise a balloon arranged to store, at least in part, the coolant leaving the heat exchanger, upstream of the mechanical compression system. The advantages stated above also apply to such an installation. DESCRIPTION OF THE FIGURES AND EMBODIMENTS Other advantages and particularities of the invention will appear on reading the detailed description of implementations and non-limiting embodiments, and of the attached FIGURE 1 which is a diagrammatic view of the invention. a drying installation according to the invention. The embodiments described hereinafter being in no way limiting, it may be considered in particular variants of the invention comprising only a selection of features described, isolated from the other characteristics described (even if this selection is isolated within a sentence comprising these other features), if this selection of features is sufficient to confer a technical advantage or to differentiate the invention from the state of 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. FIG. 1 illustrates a preferred embodiment of the invention. According to this embodiment, the installation comprises an industrial treatment path in which is moved a product to be dewatered, for example sludge.
    [0013] The product to be dehydrated is preferably a pasty or liquid product, preferably a sludge. By dehydration of the product is meant the loss or elimination (partial or total) of the water of this product, by any process whatsoever. In the following description, the term "sludge" may be replaced by "product to be dehydrated". This path comprises various sludge channeling elements or conduits 9a-9i, as well as various devices or devices that are interconnected by these lines 9a-9i. The sludge arrives via line 9a, with a dryness of, for example, 4 to 25%, in a pump 11 which pressurizes the sludge. The output of the pump 11 is connected to a heating means 12 by the pipe 9b. The heating means 12 is of a type capable of heating the sludge by direct or indirect heat transfer upstream or inside a reactor 1 in which a thermal conditioning step is carried out (which is typically an operation). hydrothermal carbonization). This heating means 12 can carry out heat transfer via a hot thermal fluid, for example oil, steam or superheated water, or by means of a direct injection of 25 different types of steam. In the example of FIG. 1, this heating means 12 heats the sludge by thermal transfer with a hot thermal fluid, for example oil, circulated in a loop 122 by a pump 121. This heating means 12 is preferably a tube exchanger 30 in which the sludge and the thermal fluid are circulated countercurrently. The heating means 12 is connected to the reactor 1 by the pipe 9c. Preferably, an additive is injected into the sludge by any appropriate injection means 14. The additive may consist of any catalyst capable of decomposing the organic material, for example an acid such as sulfuric acid. The injection of additive can be carried out upstream or inside the reactor 1. The reactor 1 is arranged to store the sludge and maintain it at a carbonization pressure PO typically between 0.6 and 3.5 MPa, and at a carbonization temperature T0 typically between 140 and 300 ° C. In a preferred embodiment, the unique function of the reactor 1 is to provide a residence time for submitting the sludge to chemical reactions, typically hydrolysis. Thus, the reactor 1 may alternatively take the form of a baffled chamber or not, cased or not, or for example a tube of sufficient length to ensure the required residence time. It can be mixed or not, operating in batch or continuously. The reactor 1 is preferably surrounded by a casing 13 forming a double wall in which circulates a hot fluid, typically oil, to heat or maintain the temperature of the sludge contained in the reactor 1. The hot fluid is for example set circulating in the double wall through a pump 131 mounted on a loop 132 connected to the double wall.
    [0014] Alternatively, a steam injection may also make it possible to maintain the reactor 1 in temperature or pressure. The means for pressurizing the sludge, heating the sludge, keeping it in temperature and decompressing it may take any standard configuration.
    [0015] In particular, the thermal conditioning step can be carried out in different tanks operating in parallel. The carbonized sludge, that is to say having undergone a hydrothermal carbonization operation by staying for example in the reactor 1 at the pressure PO and the carbonizing temperature TO, is conveyed via the pipe 9d to a heat exchanger. heat 2. Typically, the temperature of the carbonized sludge, at the outlet of the reactor 1, is greater than 100 ° C., for example between 100 and 120 ° C. At the outlet of the reactor 1 and upstream of the heat exchanger 2, an additional exchanger (not shown) can be used to recover the heat contained in the sludge for the purposes of the hydrothermal carbonization process. ale. The heat exchanger 2 is arranged to transfer to a heat transfer fluid, this heat transfer fluid being preferably water, at least part of the heat contained in the sludge from the reactor 1, in order to carry out a step of heat transfer. The coolant is circulated by a circulation pump 31 in a circulation loop 32 which passes through the heat exchanger 2.
    [0016] The circulation loop 32 also passes through a balloon 3 so that at least a part of the coolant coming from the heat exchanger 2, heated by heat transfer with the sludge from the reactor 1, is stored in the balloon 3. Preferably, the circulation loop 32 is arranged so that the heat transfer fluid leaving the balloon 3 and going towards the heat exchanger 2 is taken from the bottom part of the balloon 3, and for the heat transfer fluid from of the heat exchanger 2 is injected into the balloon 3 at the top (the top and bottom being in the present description defined so that a direction from top to bottom is parallel to the gravitational attraction terrestrial). Thus, the fraction of heated heat transfer fluid arriving in the heat exchanger 2 gradually warms the heat transfer fluid in the balloon 3 from top to bottom. The balloon 3 is sized to store the heat corresponding to the heating requirement of a heated filter press 6 mounted downstream of the heat exchanger 2 (see below). The balloon 3 is preferably designed to store heat by increasing its average temperature, and not by increasing its volume. In particular, the temperature in the upper part of the flask 3 can fluctuate between 60 and 120 ° C and the average temperature can fluctuate between 50 and 100 ° C, which allows a large heat storage. Preferably, the circulation pump 31 and / or the heat exchanger 2 are piloted to lower the temperature of the sludge leaving the heat exchanger 2 to a filtration temperature T1, preferably less than 90 ° C. preferably between 50 and 70 ° C. To do this, one can for example: 3035190 control the speed of the circulation pump 31, and / or control the heat exchanger 2 by performing the following steps: - take a part of the heat transfer fluid leaving the heat exchanger heat 2 and 5 - reintroduce upstream of the heat exchanger 2 (preferably upstream of the circulation pump 31), via a three-way valve 33, this sampled portion being conveyed to the valve 33 via an auxiliary circuit 331. Preferably, the heat transfer fluid circulates in the heat exchanger 2 against the current of the sludge (contrary to that illustrated in FIG. 1). Preferably, for safety reasons, an air condenser 34 is installed on the circulation loop 32 in order to ensure the cooling of the heat exchanger 2 in the event of non-use of the heating press-filter 6. The outgoing mud of the heat exchanger 2 arrives in a decompression tool 15 through the pipe 9e. Alternatively, the decompression tool 15 may be placed upstream of the heat exchanger 2.
    [0017] In the embodiment of FIGURE 1, the sludge exiting the decompression tool 15 arrives in a storage tank 5 through line 9f. The decompression tool 15, for example a valve, allows the sludge to be sent without spraying into the storage tank 5. According to an advantageous embodiment, a loop 52 connects the balloon 3 and the storage tank 5. This loop 52 is arranged to circulate, by a pump 51, a fraction of the coolant between the tank 3 and the storage tank 5 in a closed circuit, in order to maintain the temperature of the sludge in the storage tank 5. Advantageously this fraction of coolant is removed in the upper portion and reintroduced in the lower part of the balloon 3. A pump 61 takes, through the line 9g, the sludge in the storage tank 5 to introduce it under pressure into the filter The heating press-filter 6 is of a type capable of performing a mechanical dewatering step and a step of heating the sludge. The heated filter press 6 comprises at least two trays, pressed against each other, and an interior space arranged to receive the sludge. The interior space is for example made by one or more filter chambers formed in one or more trays, for example in the form of recesses. An example of trays is described in WO 2004/024290 A1. To carry out the mechanical dewatering step, the heating press-filter 6 comprises a compression means able to compress against the sludge contained in the heating press-filter 6 against at least one of said trays. This compression means is preferably a membrane which is either integrated in a tray (the membrane then being for example polypropylene), or fixed on a tray (the membrane being for example 15 rubber). Preferably, the heating filter press 6 comprises several pairs of trays, one tray of each pair comprising a membrane and the other tray of each pair comprising a filtration chamber. Compression as such is preferably carried out by pressurizing or inflating the membrane (s), for example by compressed air or water under a dehydration pressure P1, preferably greater than 0, 5 MPa, typically 1.5 MPa. Such a compression means is advantageous because it makes it possible to exert a uniform pressure on the sludge contained in the interior space of the heating press-filter 6.
    [0018] The mechanical dewatering step typically comprises: feeding the heated press filter press 6 by the pump 61, for example with a supply pressure of 0.6 or 0.7 MPa; a piston keeps the trays tight against each other; Preforming the sludge (referred to as cake in this step) in the interior space of the heated filter press 6 at that supply pressure; stopping the pumping and inflation of the membranes for example for a period of between 15 and 45 minutes; during this compression step, on the one hand, a liquid fraction of the sludge, called filtrate, is discharged through a filtrate discharge outlet 912, the liquid fraction being separated from the sludge under the slurry. On the other hand, the slurry is compressed against at least one tray, preferably the at least one tray comprising a filter chamber. During the mechanical dehydration step, the internal space of the heating filter-press 6 accommodating the sludge is brought to a vacuum, for example by actuating a fan 63, and the gases or vapors are channeled via a pipe 631. thus extracted to a steam treatment system 632. One or more trays of the heated filter press 6, especially the one or more trays comprising a filtration chamber, comprise channels capable of receiving a heating liquid. Preferably, the installation is arranged so that the heating liquid consists at least in part of the heat transfer fluid from the heat exchanger 2, and preferably from the balloon 3. To do this, it is circulating by a pump 35 the coolant 20 in a loop 36 connecting, in a closed loop, the balloon 3 and the channels. As illustrated in FIG. 1, the heat-transfer fluid thus introduced into the channels is preferably taken from the upper part of the balloon 3, and the heat-transfer fluid leaving the heated press-filter 6 is preferably reintroduced into the lower part of the balloon 3.
    [0019] These arrangements make it possible to carry out a heating step during which the heat transfer fluid is circulated in the channels. The implementation of the hydrothermal carbonization operation can be discontinuous, especially when it is performed in batch, and the availability of heat transfer fluid heated during the heat transfer step can therefore be insufficient to achieve the heating step, the installation preferably comprises an additional heat source 4 adapted to heat the heat transfer fluid before its arrival in the heating press-filter 6. Thus, if necessary, it warms the heat transfer fluid before -30- its circulating in the channels through such an additional heat source 4. This additional heat source 4 is preferably a boiler, preferably mounted on a loop 42 mounted on the balloon 35 so as to: withdrawing from the balloon 3, preferably at the bottom, a fraction of heat transfer fluid contained in the balloon 3, by actuation of a pump 41, warming iron the fraction of heat transfer fluid circulating in the loop 42 by the additional heat source 4, and reintroduce into the balloon 3 this fraction of heat transfer fluid and heated, preferably in the upper part. Advantageously, a heating time D0 is set, the heating time D0 corresponding to the duration of implementation of the heating step, so that the dryness of the product to be dehydrated contained in the heating press-filter 6 reaches or exceeds a final dryness Sf, preferably between 50 and 95%, at the end of this heating step.
    [0020] When the mechanical dehydration and heating steps are completed, the dewatered sludge contained in the heated filter press 6, ie the sludge having undergone these steps, is discharged from the heating press filter 6 through an outlet 9 With respect to the heated press-filter 6 and the implementation of the mechanical dehydration and heating steps, the means for pressurizing, filtering, heating, depressurizing, resuming the pressure of the filter press, and Dehydrated sludge, treat gases or vapors can take any standard configuration. Thus, the heating filter press 6 implemented in this installation can be of any known type, for example of the type described in WO 98/25684. The control of the various devices or devices described above is ensured by any appropriate control device 7 such as a central computer unit or an electronic console provided with separate control means for each type of device or device such as pumps, valves, reactor (eg temperature, pressure), fan (eg flow), etc. (Such control being represented by dashed lines in FIGURE 1). In a non-illustrated embodiment, the heated filter press 6 is replaced by a mechanical compression system such as a simple filter press (not shown), or by a piston press whose output is directed to means such as a low temperature dryer (not shown, and preferably located downstream of the filter press). This low temperature dryer may be of the strip type, for example as marketed by the company STC. Such a belt dryer allows sludge to be dried with a low temperature heat source, typically less than 90 ° C. An installation according to such an embodiment makes it possible to heat the sludge within such a low temperature dryer by transferring recovered heat (preferably by the heat exchanger 2) into the sludge having undergone the conditioning stage. thermal. Of course, the invention is not limited to the examples that 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 can be associated with each other in various combinations in that they are not incompatible or exclusive of each other.
    权利要求:
    Claims (12)
    [0001]
    REVENDICATIONS1. A method of drying a product to be dewatered, comprising moving the product to be dewatered in an industrial process path (9a-9i, 11, 12, 1, 2, 15, 5, 61, 6), said path comprising a reactor (1) and a heat exchanger (2), characterized in that this path further comprises a mechanical compression system (6), and in that this method comprises: - a thermal conditioning step during which is maintained the product to be dehydrated in the reactor (1) at a carbonization pressure P0, preferably between 0.6 and 3.5 MPa, and at a carbonization temperature TO, preferably between 140 and 300 ° C, a step heat transfer during which, through the heat exchanger (2), is transferred to a heat transfer fluid at least a portion of the heat contained in the product to be dehydrated having undergone the thermal conditioning step , a step of mechanical dehydration during which: the product to be dehydrated having undergone the thermal conditioning step and the heat transfer step are introduced into the mechanical compression system (6), where the product to be dehydrated contained in the system is compressed. mechanical compression (6) by application of a dehydration pressure P1, preferably greater than 0.5 MPa, and a liquid fraction of the product to be dehydrated is discharged, the liquid fraction being separated from the product to be dehydrated under the effect of its compression, and a heating step during which is transferred to the product to be dehydrated at least a portion of the heat contained in the heat transfer fluid having undergone the heat transfer step, this heating step being performed jointly or after the mechanical dehydration step. 3035190 - 17-
    [0002]
    2. Method according to claim 1, characterized in that the product to be dewatered is a sewage sludge from a wastewater treatment. 5
    [0003]
    3. Method according to claim 1 or 2, characterized in that the mechanical compression system (6) is a heating press-filter comprising at least two trays and in that: during the mechanical dewatering step, the compression of the The product to be dehydrated is produced against at least one of said trays, and during the heating step, the heat transfer fluid which has undergone the heat transfer step is circulated in channels formed in at least one of said trays. 15
    [0004]
    4. Method according to one of claims 1 to 3, characterized in that carries out the heat transfer step by circulating: the coolant and the product to be dehydrated in the heat exchanger (2), and the coolant in a circulation loop (32) passing through the heat exchanger (2), the coolant being circulated in the circulation loop (32) by driving a circulation pump (31) and controlling the circulation pump (31) and / or the heat exchanger (2) to lower the temperature of the product to be dehydrated to a filtration temperature T1, preferably less than 90 ° C, preferably between 50 and 70 ° C.
    [0005]
    5. Method according to one of claims 1 to 4, characterized in that stored in a flask (3) at least a portion of the heat transfer fluid having undergone the heat transfer step, and in that the fluid coolant used during the heating step is at least partly taken from this flask (3). 3035190 - 18-
    [0006]
    6. Method according to one of claims 1 to 5, characterized in that warms the coolant before use in the heating step via an additional heat source (4). 5
    [0007]
    7. Method according to one of claims 1 to 6, characterized in that, during the mechanical dehydration step, an internal space of the mechanical compression system (6) accommodating the product to be dehydrated is depressurized and in that the gases or vapors thus extracted are channeled to a steam treatment system (632). 10
    [0008]
    8. Method according to one of claims 1 to 7, characterized in that a setting of a heating time DO, the heating time DO corresponding to the duration of implementation of the heating step, so that the The dryness of the product to be dewatered in the mechanical compression system (6) reaches or exceeds a final dryness Sf, preferably between 50 and 95%, at the end of this heating step.
    [0009]
    9. Drying plant comprising: a reactor (1) arranged to store the product to be dehydrated and maintain it at a carbonization pressure P0, preferably between 0.6 and 3.5 MPa, and at a carbonization temperature TO , preferably between 140 and 300 ° C, and a heat exchanger (2) arranged to transfer to a heat transfer fluid at least a portion of the heat contained in the product to be dewatered leaving the reactor (1), characterized in that it further comprises: a mechanical compression system (6) comprising: an interior space arranged to receive the product to be dewatered, a compression means capable of compressing the product to be dewatered contained in the mechanical compression system ( 6), 3035190 -19- o a filtrate discharge outlet (9i2) arranged to discharge a liquid fraction of the product to be dehydrated when it compresses the heating means arranged to transfer to the pro to dehydrate, within the mechanical compression system (6) or downstream of the mechanical compression system (6), at least a portion of the heat contained in the heat transfer fluid from the heat exchanger ( 2). 10
    [0010]
    10. Installation according to claim 9, characterized in that the mechanical compression system (6) is a heating press-filter comprising at least two trays, the compression means being arranged to compress against at least one of said trays the product to be dehydrated contained in the heating press-filter (6), and in that at least one of said trays comprises channels capable of receiving a heating liquid, the installation being arranged so that the heating liquid is constituted, at least by part, heat transfer fluid from the heat exchanger (2), the heating means comprising said channels. 20
    [0011]
    11. Installation according to claim 9 or 10, characterized in that it further comprises an additional heat source (4) adapted to heat the heat transfer fluid before its arrival in the heating means.
    [0012]
    12. Installation according to claim 9 or 11, characterized in that it further comprises a balloon (3) arranged to store, at least in part, the coolant leaving the heat exchanger (2), upstream of the mechanical compression system (6). 25 30
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    同族专利:
    公开号 | 公开日
    EP3149420B1|2019-02-13|
    CN106795024B|2021-01-22|
    FR3035190B1|2017-04-28|
    WO2016170464A1|2016-10-27|
    AU2016252369A1|2017-02-09|
    ES2722079T3|2019-08-07|
    US20180179063A1|2018-06-28|
    CN106795024A|2017-05-31|
    US10343917B2|2019-07-09|
    EP3149420A1|2017-04-05|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE102011055986A1|2011-12-02|2013-06-06|Thomas Reichhart|Hydrothermal carbonization of biomass in continuous flow, comprises feeding biomass by conveyor to a reactor, in which biomass is dehydrated and carbonized, removing carbon slurry fed to outlet by filtering device used for solid separation|
    WO2014178028A1|2013-05-03|2014-11-06|Degremont|Method for ultra-dehydrating thickened or pasty biomass products, and equipment for implementing the method|
    DE102013013724A1|2013-08-20|2015-02-26|Suncoal Industries Gmbh|Method for producing a homogeneous solid from biomass|
    DE58905358D1|1988-05-24|1993-09-30|Siemens Ag|Process and device for drying sewage sludge.|
    US5557873A|1990-10-23|1996-09-24|Pcl/Smi, A Joint Venture|Method of treating sludge containing fibrous material|
    BG62356B1|1996-12-12|1999-09-30|Belchev, Belcho A.|Installation for continuous treatment of liquids and dewatering and drying of the separated nonfiltering solid particles|
    US20060032805A1|2002-09-13|2006-02-16|Hildebrant Mark W|Heating plate for vacuum filter press|
    FR2870154B1|2004-05-13|2012-12-14|Bio 3D Applic|BIO-THERMAL METHOD AND SYSTEM FOR STABILIZING LUMBER|
    US8579999B2|2004-10-12|2013-11-12|Great River Energy|Method of enhancing the quality of high-moisture materials using system heat sources|
    FR2953005B1|2009-11-23|2011-12-09|Degremont|PROCESS AND INSTALLATION FOR DRYING PASTE MATERIALS, IN PARTICULAR SLUDGE OF PURIFICATION STATIONS|
    IT1400509B1|2010-06-22|2013-06-11|Stradi|EQUIPMENT AND METHOD FOR THE DEHYDRATION OF SLUDGE DEHYDRATION TREATMENT.|
    CN103121778A|2012-06-26|2013-05-29|深圳市环源科技发展有限公司|Method for treatment and resource utilization of sludge based on low-pressure catalytic thermal hydrolysis and application of method|
    KR101265740B1|2013-01-16|2013-05-20|배희동|Development of integrated process technology for renewable energy and feed resources production with palm oil mill effluent, palm oil decanter cake, palm kernel shell and palm kernel cake from palm oil mill process|
    FR3008693B1|2013-07-18|2019-05-03|Terranova Energy Gmbh|OPTIMIZED HYDROTHERMAL CARBONIZATION PROCESS AND INSTALLATION FOR ITS IMPLEMENTATION|
    CN103755124A|2014-01-23|2014-04-30|杭州互惠环保科技有限公司|Sludge treatment method based on hydrothermal carbonization|
    US9989310B2|2016-07-15|2018-06-05|Bioleap Inc.|Dryer exhaust heat recovery|CN110127975A|2018-02-09|2019-08-16|聂红军|A kind of sludge treating system and method|
    CN110591783A|2019-08-27|2019-12-20|浙江工业大学|System and method for preparing solid fuel by using kitchen waste after grease removal|
    CN111018297A|2020-01-02|2020-04-17|思庚特新能源科技有限公司|One-stop disposal method for sludge dehydration, drying and thermal cracking|
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    优先权:
    申请号 | 申请日 | 专利标题
    FR1553500A|FR3035190B1|2015-04-20|2015-04-20|METHOD AND INSTALLATION FOR DRYING BY HYDROTHERMAL CARBONIZATION AND FILTRATION|FR1553500A| FR3035190B1|2015-04-20|2015-04-20|METHOD AND INSTALLATION FOR DRYING BY HYDROTHERMAL CARBONIZATION AND FILTRATION|
    EP16723526.6A| EP3149420B1|2015-04-20|2016-04-18|Method and facility for drying by means of hydrothermal carbonization and filtering|
    ES16723526T| ES2722079T3|2015-04-20|2016-04-18|Drying procedure and installation by hydrothermal carbonization and by filtration|
    CN201680002247.4A| CN106795024B|2015-04-20|2016-04-18|Drying method and drying apparatus by hydrothermal carbonization and filtration|
    US15/324,918| US10343917B2|2015-04-20|2016-04-18|Method and facility for drying by means of hydrothermal carbonization and filtering|
    AU2016252369A| AU2016252369A1|2015-04-20|2016-04-18|Method and facility for drying by means of hydrothermal carbonization and filtering|
    PCT/IB2016/052204| WO2016170464A1|2015-04-20|2016-04-18|Method and facility for drying by means of hydrothermal carbonization and filtering|
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