EP2140217B1 - Procédé pour sécher un matériau humide - Google Patents

Procédé pour sécher un matériau humide Download PDF

Info

Publication number
EP2140217B1
EP2140217B1 EP08714794.8A EP08714794A EP2140217B1 EP 2140217 B1 EP2140217 B1 EP 2140217B1 EP 08714794 A EP08714794 A EP 08714794A EP 2140217 B1 EP2140217 B1 EP 2140217B1
Authority
EP
European Patent Office
Prior art keywords
pressure
wet material
drying
container
condenser
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
EP08714794.8A
Other languages
German (de)
English (en)
Other versions
EP2140217A1 (fr
Inventor
Mark Braendli
Markus Lehmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP2140217A1 publication Critical patent/EP2140217A1/fr
Application granted granted Critical
Publication of EP2140217B1 publication Critical patent/EP2140217B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/005—Treatment of dryer exhaust gases
    • F26B25/006—Separating volatiles, e.g. recovering solvents from dryer exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/18—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact
    • F26B3/20—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor
    • F26B3/205—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source being a heated surface, e.g. a moving belt or conveyor the materials to be dried covering or being mixed with heated inert particles which may be recycled
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B7/00—Drying solid materials or objects by processes using a combination of processes not covered by a single one of groups F26B3/00 and F26B5/00
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B9/00—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards
    • F26B9/06—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards in stationary drums or chambers
    • F26B9/08—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards in stationary drums or chambers including agitating devices, e.g. pneumatic recirculation arrangements
    • F26B9/082—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards in stationary drums or chambers including agitating devices, e.g. pneumatic recirculation arrangements mechanically agitating or recirculating the material being dried
    • F26B9/085—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards in stationary drums or chambers including agitating devices, e.g. pneumatic recirculation arrangements mechanically agitating or recirculating the material being dried moving the material in a substantially vertical sense using conveyors or agitators, e.g. screws or augers with vertical axis, which are positioned inside the drying enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
    • F26B2200/18—Sludges, e.g. sewage, waste, industrial processes, cooling towers

Definitions

  • the invention relates to a process for drying a pasty wet material, in particular sludge, comprising a dry substance, using a gas-tight, over- and / or vacuum fixed container system, a drying container with the wet material, which can be tempered, a condenser for condensing the comprising vaporized liquid to the condensate, and a vapor space connecting the drying vessel and the condenser.
  • Drying systems for sludge for example sewage sludge
  • sludge for example sewage sludge
  • the sludge to be dried is pre-dried in a preliminary stage with centrifuges until the sludge has a dry matter TS of about 20-40%.
  • This starting material is pasty and very sticky, which makes handling difficult.
  • This wet material can now be burned at high cost in an incinerator. This happens at about 400 ° C and is very unpopular, because often pollutants such as heavy metals are released.
  • a distillation plant will be in the WO 02/09837 which is suitable with known methods for distilling, for example, muddy media.
  • a disadvantage of this method is the high energy consumption that is required for the process.
  • Object of the present invention is to provide a low-energy method for drying a wet material, which does not burden the environment with odor emission or toxins.
  • the idea underlying the invention is that the steam in the vapor space is free of foreign gas except for a small, tolerated residual amount. This is achieved by monitoring the pressure in the vapor space and controlling it so that the drying is always carried out in the region close to the saturation vapor pressure of the liquid to be distilled. For this purpose, the pressure and the temperature in the vapor space must always be determined. If the pressure is too high, it is reduced in such a way that mainly foreign gas is thereby removed. This promotes the efficiency of the condenser and thus the performance of the drying plant with low energy consumption. In addition, the temperature difference between the drying tank and condenser can be kept small.
  • the Fig. 1 shows a simple embodiment of an inventive drying plant.
  • This comprises a container system 1, which is subdivided into the areas drying container 2, condenser 3 and vapor space 6, wherein the container system 1 must be fixed to positive and / or negative pressure.
  • the wet material 4 which comprises the liquid to be distilled Fd and is temperature controlled.
  • the condenser 3 receives the likewise temperature-controllable condensate 5, which is formed by the distillation after condensation.
  • the wet material 4 and the condensate 5 can also be tempered outside the container system 1.
  • the vapor space 6 connects the drying vessel 2 with the condenser 3. It is filled with the vapor Dk to be condensed. This vapor Dk was formed by evaporating the liquid Fd to be distilled from the drying container 2.
  • the vapor space 6 is equipped with a pressure sensor 7 for measuring the mixing pressure pm set in the vapor space 6, with a temperature sensor 8 for measuring the mixing temperature Tm set in the vapor space 6 , as well as with a pressure regulator 9 for adjusting, in particular for reducing the mixing pressure pm in the vapor space 6.
  • the drying container 2 with the wet material 4 is brought to a first temperature T1 and the condenser 3 to a second, lower temperature T2. Subsequently, the mixing pressure pm and the mixing temperature Tm are measured. From the measured mixing temperature Tm, the saturation vapor pressure ps of the liquid Fd at the temperature Tm can be determined.
  • the saturation vapor pressure is a property of a liquid. It describes the maximum vapor pressure at a certain temperature and is often referred to as vapor pressure for short. For example, atoms / molecules escape from pure liquids into the gas phase until a pressure which depends on the type of substance and the equilibrium temperature has been established therein. This pressure is the saturation vapor pressure. It rules when the gas is in thermodynamic equilibrium with the liquid. In this state, the evaporation of the liquid is quantitatively equal to the condensation of the gas. None of the phases grows at the expense of the others, allowing both to coexist stably. One therefore speaks of a dynamic equilibrium.
  • a vapor saturation pressure curve 10 of a substance is plotted as a function of pressure versus temperature, with the liquid phase of the substance in the upper left, the gaseous phase in the lower right of the curve. The phase change occurs in the region of the saturation vapor pressure curve 10.
  • Saturation vapor pressure curves of common substances are known and can be looked up in manuals or interpolated via formulas.
  • a desired pressure range 11 is calculated.
  • the mixing pressure pm should preferably be in the vapor space 6, at the associated mixing temperature Tm, so that the distillation, and thus the drying, optimally, i. as energy-efficient and efficient as possible.
  • the target pressure range 11 is above the saturation vapor pressure curve, since it includes the amount of pressure-increasing foreign gas. It is limited by a lower pressure limit p1 and an upper pressure limit p2, as in Fig. 2 shown.
  • the lower pressure limit p1 is at least 0.1% above the saturation vapor pressure ps and the upper pressure limit p2 is at most 6% above the saturation vapor pressure ps.
  • the mixing pressure pm is compared with the target pressure region 11. At the beginning of the process, the mixing pressure pm will be far above the target pressure range 11.
  • the mixing pressure pm is reduced by the pressure regulator 9 until it reaches the lower pressure limit p1.
  • This is preferably done with the pressure regulator 9, which may be a pump. As soon as the pressure limit p1 has been reached, the pressure regulator 9 is turned off.
  • the desired, process-optimal mixing pressure automatically sets itself without the intervention of the pressure regulator 9, even if the temperature of the medium to be vaporized or of the medium to be condensed changes.
  • the mixing temperature Tm and the mixing pressure pm are constantly monitored until the mixing pressure pm has reached the upper pressure limit p2.
  • the pressure can increase because, for example, the container system 1 or another component of the system have a small leak, whereby foreign gas can penetrate into the vapor space 6, or because foreign gases have dissolved from other substances of the plant or from the wet material 4.
  • the pressure in the vapor space 6 is switched on by switching on the pressure regulator resp. the pump 9 lowered again.
  • the pressure regulator 9 can be switched off again. Now the drying runs again with optimal parameters. These processes can be continued as long as wet material 4 can be supplied and condensate 5 can be removed.
  • the quality of the condensation depends largely on the foreign gas content.
  • a foreign gas component in the vapor space of individual per mils can cause condensation already reduce by 20 to 50%. Therefore, the mixing pressure is constantly monitored and compared with the target pressure range 11.
  • the foreign gas accumulates at the end of the condensation path, since it is flushed by the gas flow, which flows from the wet material 4 through the vapor space 6 to the condensate 5, but ultimately can not condense. Therefore, it is advantageous to suck the vapor at the end of the condensation path in the condenser 3, directly in the condensate 5. In this way, the highest concentration of foreign gas can be removed from the container system 1 in reducing the mixing pressure pm. On the other hand, care should be taken that the falling in droplets condensate not directly into the suction flow of the pressure regulator resp. the pump 9 device. This can be achieved by a protective cover 19.
  • the target pressure range 11 should not be too close to the saturation vapor pressure curve 10, since otherwise too much of the vapor Dk to be condensed is sucked out by the pump 9 when the mixing pressure pm is reduced. It has proved to be advantageous to select the lower pressure limit p1 preferably at least 0.2% and the upper pressure limit p2 preferably at most 4% above the saturation vapor pressure ps.
  • the method according to the invention always monitors the prevailing mixing pressure pm in the vapor space 6 and compares this with the nominal pressure range 11, in order to regulate the mixing pressure pm as required.
  • Conventional methods usually continuously suck gas from the steam space, which on the one hand a lot of energy must be expended and on the other hand much of the energetically valuable condensate is unnecessarily removed from the steam room.
  • the present method works most of the time without a vacuum pump, since this must be turned on only temporarily and only briefly.
  • the temperature difference T1-T2 between the drying tank 2 and the condenser 3 can be selected to be particularly small with this inventive method and is preferably between 1K and 10K, ideally between 1K and 3K. This is a tremendous energetic benefit because it requires little energy to create the temperature difference.
  • the drying and / or the condensation can be promoted by enlarging the surfaces of the wet material 4 in the drying container 2 and / or the surface of the condensate 5 in the condenser 3.
  • a surface enlargement can be achieved, for example, by a fine spraying of the condensate 5.
  • a dedicated nozzle of a Zersprühiki 15 in the condenser 3 can produce every second a surface of several square meters, at which the condensed vapor Dk can condense.
  • the spraying is arranged in such a direction-oriented manner that optimum mixing of the steam in the vapor space 6 is achieved. This is important in order to achieve the greatest possible heat transfer between the wet material 4 and the steam in the vapor space 6.
  • a fan 16 may be placed in the vapor space 6 to achieve the desired mixing of the vapor.
  • the drive of this fan 16 can be done by the sprayed mass flow of the medium to be evaporated or the sprayed condensate.
  • a heater 13 in the region of the drying container 2 and a cooling 14 in the region of the supply lines 12 of Zersprühwent 15 from the condenser 3 provide for reaching the set temperatures T1 and T2 in the drying tank 2 and the condenser 3.
  • the temperature regulating units 13 and 14 also be arranged directly in the wet material 4 and 5 in the condensate.
  • the surface enlargement can also be achieved by introducing a surface-enlarging, porous filling packing in the condenser 3. These allow a maximum temperature equalization in the condenser between the mixed steam and the condensate.
  • the surface enlargement of the wet material 4 in the drying container 2 can be achieved by mixing the wet material 4 under a granular carrier 17.
  • This carrier 17 absorbs a portion of the liquid of the wet material 4, which thereby becomes drier and thus less sticky. This is important because the stickiness of wet material 4 used here is usually so high that it settles on all surfaces of the system and even makes cleaning almost impossible.
  • This carrier 17 can consist of the dry substance TS, which is contained in the pasty wet material 4. This has the advantage that the dry material no longer has to be separated during the removal.
  • the carrier 17 consists of an abrasive material, in particular wood chips, plastic granules or pebble-shaped rock. As a result, all surfaces of the system are continually cleaned. Often the dry matter TS is already abrasive. The use of a foreign material for the carrier 17 is thus not mandatory. A core size between 0.5 and 30mm has proven to be suitable.
  • the carrier 17 is mixed in the preheated state with the wet material 4. This preheating can take place inside or outside of the drying container 2.
  • the mixture of carrier 17 and wet material 4 with the optimum amount of energy for example, carried out as follows:
  • the drying container 2 has a heater 13 in its jacket and is filled with the carrier 17, which may be the dry substance and is brought to the desired temperature ,
  • the carrier 17 which may be the dry substance and is brought to the desired temperature
  • wet material 4 is brought and brought in a further conveyor system 21 in the drying container 2.
  • one or more screw conveyors or, in particular, heating screw conveyors 22 continuously mix some wet material 4 under the abundant carrier 17.
  • the mixing and connection takes place until the mixture with the low wet content is ejected into the drying container 2.
  • the temperature and pressure conditions now promote drying, whereby the mixture dries very quickly.
  • the heat energy introduced in the carrier 17 should correspond to that energy which is required for the drying of the wet material 4.
  • the control of the cooling curve prevents wetting.
  • unused energy remains stored in the carrier 17.
  • the drying container 2 can be filled at intervals.
  • the removed content is then separated into dry matter TS and carrier 17, if they are not the same materials.
  • a sorting plant can then sort the dry substance TS into usable and non-utilisable masses, for example based on the particle size. Part of the dry substance TS or specially separated material, for example dust, can then be added to the wet starting material again. Also, the carrier 17 can be re-introduced into the system after removal.
  • the method can run in a continuous mode, as in Fig. 2 shown. Dry contents from the drying container 2 is brought through a conveying and lock system 23 and thereby brought externally by a heater 13 to the desired temperature. Since this material is dry, no evaporation takes place when they are heated. In a storage container 24, this material can be stored until it is used. If necessary, it is added back to the drying container 2 by the conveying and lock system 23. This is the case, for example, when the temperature in the drying tank 2 is too low.
  • external or external heating can be used additionally or alternatively to the internal heating of the drying container.
  • a great advantage of the system described and the method described is that with the heating of the dry material can be entered heat, which can not be used directly, but also at a later time for drying. It can thus be introduced around the clock heat for drying, resulting in a higher drying productivity compared to processes that rely on the presence of personnel or are subject to limited drying times.
  • the described method, operated on the described plant can also react quickly to changes in the sludge composition (water content, tackiness), the heating temperature and the heating power without sacrificing the drying quality. since the relevant quantities are only the temperature gradient T1-T2 between the drying vessel 2 and the condenser 3 and the stored thermal energy.
  • a further improvement of the plant can be achieved by the method in two or more such container systems 1 is performed, wherein the temperature ranges T1, T2 of the individual container systems 1 differ so that they adjoin one another.
  • the energy for controlling the temperature of a drying container 2 or capacitor 3 is at least partially obtained directly or indirectly via heat exchangers from the energy of another drying container 2 or capacitor 3, whose temperature is to be changed.
  • the external gas release can be carried out by means of a vacuum jet pump, which is driven either with the condensate 5 to be sprayed the same or a cooler stage, with steam of another stage or with ambient air.
  • each a heat exchanger 20 between a condensate 5 and a Wet material 4 of a following container system 1 or a series of preceding stages is arranged if they are to have the same temperatures.
  • plate heat exchangers are used for this purpose.
  • the drying containers 2 and / or condensers 3 of the various container systems 1, 1 ',... Can in particular be arranged one above the other. Particularly suitable is a horizontal arrangement of the capacitors and a vertical arrangement of the drying container.
  • the necessary connections between the individual container components are each achieved with steam pipes.
  • the advantage lies especially in the low-energy drying process, since the energy can be used optimally.
  • the (plate) heat exchangers used can be arranged inside or outside the container system 1. Reasons for the external arrangement are above all the better access for cleaning the heat exchanger.
  • container systems 1 and / or other components of the system can be made preferably entirely or mainly from inexpensive plastic.
  • the container system 1 must preferably be stable only to overpressure or to negative pressure, not both. This allows a cost-effective design of the container system 1. It may for example consist of a technical plastic film, which is supported on a solid framework, which is disposed inside or outside the film. The underpressures do not have to be that strong. For water, the absolute vapor saturation pressure at 50 ° C is still 123 mbar (relative -877 mbar). Therefore, the requirement of tear resistance to the film is still in an area where materials are available at reasonable prices.
  • the pressure regulator 9 in this case is a valve that can vent gas from the vapor space into the environment when the pressure should be lowered.
  • the overpressure can be caused by a pump or by heating.
  • the tank system need only be stable at the same time when working around the normal pressure, ie in the case of water in the range of 100 ° C.
  • the drying vessel 2 is flooded in the wet material and / or the condenser 3 is arranged flooded in the condensate of the wet material in the condensate 5.
  • the process described is carried out in a standard container, preferably in an ISO container (20 or 40 feet standard container), in which the system is located and which may be part of the system.
  • a standard container preferably in an ISO container (20 or 40 feet standard container), in which the system is located and which may be part of the system.
  • ISO container 20 or 40 feet standard container
  • Such containers are inexpensive to purchase, are ideal for transport and are available in dense (leak-free) versions.
  • the transport from the place of manufacture to the place of operation of the plant can be carried out so easily and inexpensively by container ship or by truck.
  • this facilitates the maintenance, since, if the distillation is carried out in a remote location to the civilian population, the container can again be conveniently transported to a service center on a truck.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Drying Of Solid Materials (AREA)
  • Treatment Of Sludge (AREA)

Claims (18)

  1. Procédé de séchage d'une matière humide pâteuse (4), en particulier de la boue, contenant une substance sèche TS mélangée à un liquide à évaporer Fd, en utilisant un système de cuve étanche (1) au gaz et résistant à la surpression et/ou la dépression qui comprend une cuve de séchage (2) contenant la matière humide (4) qui peut être tempérée, un condensateur (3) pour condenser le liquide Fd devenu de la vapeur en formant du condensat (5) et une cellule de vapeur (6) reliant la cuve de séchage (2) et le condensateur (3), la cellule de vapeur (6) étant équipée. D'un capteur de pression (7) pour mesurer la pression mixte pm s'établissant à l'intérieur et un régulateur de pression (9), caractérisé par les étapes opératoires consistant en ce que
    a) la cuve de séchage (2) est amenée avec la matière humide (4) à une première température T1 et le condensateur (3) à une seconde température T2 plus basse ;
    b) la pression mixte pm et la température mixte Tm sont mesurées ;
    c) la pression de vapeur de saturation ps du liquide Fd pour la température mixte mesurée Tm est déterminée ;
    d) on calcule une plage de pression théorique (11) qui est limitée par une limite inférieure de pression p1 qui se situe au moins 0,1 % au-dessus de la pression de vapeur de saturation ps et une limite supérieure de pression p2 qui se situe au plus 6 % au-dessus de la pression de vapeur de saturation ;
    e) la pression mixte pm est comparée à la plage de pression théorique (11) ;
    f) la pression mixte pm est réduite précisément par le régulateur de pression (9) jusqu'à ce qu'il ait atteint la limite inférieure de pression p1 ;
    g) les étapes b) à e) sont répétées jusqu'à ce que la pression mixte pm ait atteint la limite supérieure de pression p2 ;
    h) les étapes f) et g) sont répétées jusqu'à ce que le séchage doive être arrêté ;
    sachant que, lors de la réduction de pression dans l'étape f), des gaz sont aspirés à l'extrémité du parcours de condensation dans le condensateur (3) afin d'éliminer autant de gaz extérieur que possible du système de cuve (1).
  2. Procédé selon une des revendications précédentes, caractérisé en ce que les surfaces de la matière humide (4) dans la cuve de séchage (2) et/ou la surface du condensat (5) dans le condensateur (3) sont agrandis, de préférence par pulvérisation du condensat (5).
  3. Procédé selon la revendication 2 ou 3, caractérisé en ce que l'agrandissement de surface de la matière humide (4) dans la cuve de séchage (2) est obtenu en mélangeant la matière humide (4) sous un support de type granulé (17).
  4. Procédé selon la revendication 4, caractérisé en ce que le support (17) est composé de la substance sèche TS qui est contenue dans la matière humide pâteuse (4) ou d'un matériau abrasif, en particulier de copeaux de bois, granulés de plastique ou de pierres de type diatomée.
  5. Procédé selon la revendication 3 ou 4, caractérisé en ce que le support (17) est mélangé à l'état préchauffé avec la matière humide (4), le support (17) étant amené à l'é tat préchauffé de préférence à l'intérieur et/ou à l'extérieur de la cuve de séchage (2).
  6. Procédé selon la revendication 5, caractérisé en ce que l'énergie thermique incorporée dans le support (17) équivaut à l'énergie qui est nécessaire pour le séchage de la matière humide (4).
  7. Procédé selon une des revendications 3 à 6, caractérisé en ce que le support (17) est mélangé à la matière (4) dans une ou plusieurs vis de convoyage, en particulier le convoyeur à vis chauffant 22.
  8. Procédé selon une des revendications précédentes, caractérisé en ce que ce procédé fonctionne en marche continue.
  9. Procédé selon une des revendications 1 à 6, caractérisé en ce que la cuve de séchage (2) est remplie par intervalles et/ou qu'une partie du contenu est prélevée par intervalles dans la cuve de séchage (2).
  10. Procédé selon la revendication 9, caractérisé en ce que le contenu prélevé est divisé en substance sèche TS et en support (17).
  11. Procédé selon une des revendications précédentes, caractérisé en ce que les circuits sont fermés, ce qui a pour effet que l'ensemble du procédé ne provoque pas d'émission d'odeurs tant que la pompe à vide ne fonctionne pas.
  12. Procédé selon la revendication 2, caractérisé en ce que l'agrandissement de surface dans le condensateur (3) est obtenu en incorporant un joint de remplissage poreux agrandissant la surface.
  13. Procédé selon une des revendications précédentes, caractérisé en ce que la vapeur répartie dans la cellule de vapeur (6) est brassée par un ventilateur (16), l'entraînement du ventilateur (16) étant assuré de préférence par le débit volumique pulvérisé du fluide à évaporer ou du condensat pulvérisé à l'intérieur.
  14. Procédé selon la revendication 2, caractérisé en ce que l'élimination du gaz extérieur dans l'étape f) est faite grâce à une pompe d'injection à vide qui est entraînée avec le condensat à pulvériser (5) du même niveau ou d'un niveau plus froid.
  15. Procédé selon une des revendications précédentes, caractérisé en ce que le procédé est réalisé dans deux systèmes de cuve (1) de ce type ou davantage, les plages de température T1, T2 du système de cuve distinct à (1) se différenciant par le fait qu'elles sont voisines et l'énergie de chauffage d'une cuve de séchage (2) ou d'un condensateur (3) étant de préférence produite au moins partiellement directement ou indirectement par le biais d'échangeurs thermiques, en particulier d'échangeurs thermiques à plaques, à partir de l'énergie d'une autre cuve de séchage (2) ou d'un autre condensateur (3) dont la température doit être modifiée.
  16. Procédé selon une des revendications précédentes, caractérisé en ce que le système de cuve (1) et les canalisations sont composés totalement ou principalement de matière plastique.
  17. Procédé selon une des revendications précédentes, caractérisé en ce que la cuve de séchage (2) est disposée dans la matière humide et/ou le condensateur (3) dans le condensat dans la matière humide (4) ou immergée dans le condensat (5).
  18. Procédé selon une des revendications précédentes, caractérisé en ce que le procédé est réalisé dans un container ISO.
EP08714794.8A 2007-04-04 2008-04-01 Procédé pour sécher un matériau humide Active EP2140217B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH5482007 2007-04-04
PCT/CH2008/000144 WO2008122137A1 (fr) 2007-04-04 2008-04-01 Procédé pour sécher un matériau humide

Publications (2)

Publication Number Publication Date
EP2140217A1 EP2140217A1 (fr) 2010-01-06
EP2140217B1 true EP2140217B1 (fr) 2017-08-30

Family

ID=38283149

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08714794.8A Active EP2140217B1 (fr) 2007-04-04 2008-04-01 Procédé pour sécher un matériau humide

Country Status (5)

Country Link
US (1) US8434241B2 (fr)
EP (1) EP2140217B1 (fr)
ES (1) ES2649288T3 (fr)
HU (1) HUE035231T2 (fr)
WO (1) WO2008122137A1 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PT2361659E (pt) * 2007-04-04 2012-12-03 Markus Lehmann Processo para a destilação de um material de partida e instalação para a execução de um processo deste género
US9067162B2 (en) * 2011-08-10 2015-06-30 Crown Iron Works Company DT vapor wash
CH710735A1 (de) 2015-02-13 2016-08-15 Thermal Purification Tech Ltd Mehrstufige Destillationsanlage, Verfahren zum Betreiben einer solchen und Steuerung dafür.
CH711261A1 (de) 2015-06-30 2016-12-30 Lehmann Markus Anlage zur Durchführung eines kontiunierlichen, mehrstufigen Industrieprozesses.
CH712029A1 (de) 2016-01-12 2017-07-14 Thermal Purification Tech Ltd Nieder-Temperatur-Destillationsanlage.

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1254139A (fr) 1960-04-12 1961-02-17 Leybold Hochvakuum Anlagen Dispositif pour séparer sous vide des vapeurs condensables et procédé pour sa mise en oeuvre
SE331269B (fr) * 1968-10-31 1970-12-21 E Carlsson
DE2811902A1 (de) * 1978-03-18 1979-09-27 Bayer Ag Verfahren und vorrichtung zum entfernen von loesungsmitteln und reagieren von stoffkomponenten bei mehrstoffgemischen
US4153411A (en) * 1978-04-12 1979-05-08 Envirotech Corporation Rotary sludge drying system with sand recycle
CH641133A5 (de) 1979-05-28 1984-02-15 Escher Wyss Ag Verfahren zum verarbeiten von klaerschlamm.
US5490907A (en) * 1989-01-23 1996-02-13 Agglo Inc. Method for treating sludges
DE3902446C1 (fr) 1989-01-27 1990-07-05 Sulzer-Escher Wyss Gmbh, 7980 Ravensburg, De
FR2687079B1 (fr) * 1992-02-12 1994-09-23 Sirven Procede, machine et installation, d'extraction par evaporation des residus solides d'une matiere fluide.
DE19822355A1 (de) 1998-05-19 1999-11-25 Pierre Flecher Feinvakuum-Kondensationsholztrockner mit Warmwasser- und Mikrowellenheizung
AT409421B (de) 1999-02-23 2002-08-26 Wolf Systembau Gmbh & Co Kg Verfahren und vorrichtung zum trocknen von feuchtigkeit enthaltenden produkten
AU2001278340A1 (en) 2000-07-27 2002-02-13 Ips Gmbh Device for distilling a medium
US6971187B1 (en) * 2002-07-18 2005-12-06 University Of Connecticut Automated process control using manometric temperature measurement
EP1551466A2 (fr) * 2002-10-08 2005-07-13 Econova AB Dechets organiques aseptises
KR100541159B1 (ko) * 2004-03-02 2006-01-10 (주)대우건설 마이크로파와 가열을 이용한 하수슬러지 처리장치 및 방법
WO2006000020A1 (fr) 2004-06-29 2006-01-05 European Nickel Plc Lixiviation amelioree de metaux de base
EP1776554A4 (fr) * 2004-08-12 2014-02-19 Cons Technologies Inc Procede d'amendement des sols par des boues deshydratees

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
EP2140217A1 (fr) 2010-01-06
US20100115789A1 (en) 2010-05-13
US8434241B2 (en) 2013-05-07
WO2008122137A1 (fr) 2008-10-16
ES2649288T3 (es) 2018-01-11
HUE035231T2 (hu) 2018-05-02

Similar Documents

Publication Publication Date Title
EP2361659B1 (fr) Procédé pour distiller un matériau de départ et installation pour mettre un tel procédé en oeuvre
DE3902446C1 (fr)
EP2140217B1 (fr) Procédé pour sécher un matériau humide
DE102008063661A1 (de) Trocknen von Fest-Flüssig-Mischsystemen
DE102008056739A1 (de) Verfahren und Vorrichtung zur Trocknung
WO2016016297A1 (fr) Procédé et dispositif de séchage d'un produit à sécher, installation industrielle, papeterie et dispositif de commande
DE60316893T2 (de) Verfahren und Vorrichtung zur Gewinnung einer gereinigten Flüssigkeit
DE69406987T2 (de) Vakuum Konzentrationsanlage
DE69922547T2 (de) Verfahren und vorrichtung zum aufkonzentrieren von feststoffhaltigem schlamm
DE10246599A1 (de) Methode und Apparat zum Ausführen von mehrfachen Reinigungs- und Vakuumtrocknungsvorgängen in geschlossenen Behältern
AT507766A1 (de) Verfahren zur trocknung fester stoffe mit minimalem energieeinsatz
WO2003050046A1 (fr) Procede et dispositif de sechage de boues, en particulier de boues d'eaux usees
EP0030376B1 (fr) Procédé et dispositif de séchage et de réchauffage de charbon humide
EP1674140B1 (fr) Procédé et appareil pour condensation partielle
EP2062963A2 (fr) Procédé et dispositif de traitement à économie d'énergie et écologique de graines oléagineuses
EP0542958B1 (fr) Procede et installation pour le traitement de tourteaux de boue ou de tourteaux presses
DE102006009614A1 (de) Verfahren und Vorrichtung zum Trocknen oder Konzentrieren von Stoffen
DE102016213956B4 (de) Kontakttrockner
EP0752567A1 (fr) Procédé de séchage d'une isolation solide d'un appareil électrique, et dispositif pour la mise en oeuvre de ce procédé
WO2013124140A1 (fr) Séchage de produits alimentaires, notamment de pâtes
DE19542301B4 (de) Verfahren und Einrichtung zum Trocknen von schlammartigem Trockengut, insbesondere Klärschlamm
DE10118580C2 (de) Verfahren zur Behandlung der Atmosphäre in Autoklaven
AT412742B (de) Verfahren zur trocknung von entzündlichem trocknungsgut
EP1433508A1 (fr) Systeme d'extraction a fonctionnement continu et a circuit unique permettant l'extraction de co 2? de matieres premieres vegetales
EP0417592A2 (fr) Dispositif et procédé de récupération de solvants

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20091013

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

INTG Intention to grant announced

Effective date: 20170407

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

RIN1 Information on inventor provided before grant (corrected)

Inventor name: BRAENDLI, MARK

Inventor name: LEHMANN, MARKUS

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 923952

Country of ref document: AT

Kind code of ref document: T

Effective date: 20170915

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502008015573

Country of ref document: DE

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: SCHNEIDER FELDMANN AG PATENT- UND MARKENANWAEL, CH

REG Reference to a national code

Ref country code: NL

Ref legal event code: MP

Effective date: 20170830

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2649288

Country of ref document: ES

Kind code of ref document: T3

Effective date: 20180111

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171130

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171201

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171130

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20171230

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 11

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

REG Reference to a national code

Ref country code: HU

Ref legal event code: AG4A

Ref document number: E035231

Country of ref document: HU

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502008015573

Country of ref document: DE

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20180531

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20180430

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180401

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180430

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180401

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170830

REG Reference to a national code

Ref country code: CH

Ref legal event code: PFA

Owner name: LEHMANN, MARKUS, CH

Free format text: FORMER OWNER: LEHMANN, MARKUS, CH

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230527

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: TR

Payment date: 20240327

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20240423

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20240418

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 20240501

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20240517

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 20240417

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20240430

Year of fee payment: 17

Ref country code: FR

Payment date: 20240423

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: HU

Payment date: 20240502

Year of fee payment: 17