EP0549577A1 - Process and device for drying solid materials in an indirectly heated fluidized bed. - Google Patents

Process and device for drying solid materials in an indirectly heated fluidized bed.

Info

Publication number
EP0549577A1
EP0549577A1 EP90916213A EP90916213A EP0549577A1 EP 0549577 A1 EP0549577 A1 EP 0549577A1 EP 90916213 A EP90916213 A EP 90916213A EP 90916213 A EP90916213 A EP 90916213A EP 0549577 A1 EP0549577 A1 EP 0549577A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
solid material
steam
solid
discharged
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.)
Granted
Application number
EP90916213A
Other languages
German (de)
French (fr)
Other versions
EP0549577B1 (en
Inventor
Bodo Wolf
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.)
UET UMWELT- UND ENERGIETECHNIK FREIBERG GMBH
Original Assignee
UET UMWELT- und ENERGIETECHNIK GmbH
Umwelt & Energietech
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 UET UMWELT- und ENERGIETECHNIK GmbH, Umwelt & Energietech filed Critical UET UMWELT- und ENERGIETECHNIK GmbH
Publication of EP0549577A1 publication Critical patent/EP0549577A1/en
Application granted granted Critical
Publication of EP0549577B1 publication Critical patent/EP0549577B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • 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
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • F26B3/084—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
    • 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
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed

Definitions

  • the invention relates to a method and a device for drying solid materials, such as lignite, peat, sand, filter cakes from mechanical separation processes and sludges which contain less than 98% by mass of a vaporizable material, for example water, in which an indirectly heated fluidized bed is formed, which contains the solid material whirled up by a fluidizing medium, the fluidizing medium being the vaporizable material in vapor form and in which the dried material discharged from the fluidized bed dryer, optionally after cooling, further processing, Use or landfill, but the vaporized material can be supplied for cleaning, cooling, material use and / or heat energy recovery " and is suitable for use in industry, construction, agriculture and municipal disposal.
  • a vaporizable material for example water
  • Drying processes in particular those which separate water as a vaporizable fraction from solid materials, were of great economic and social importance for industrial production, construction, energy conversion and the disposal of municipalities and businesses. Drying is sometimes as natural or integrated into the process as it is when burning water-containing fuels, e.g. Lignite and sludge,
  • plate and tube dryers i.e. contact dryers
  • contact dryers which are indirectly heated with steam, as described by Krug and Nauendorf in the book “Lignite Briquetting” Volume 1, Drying Section, VEB German Publishing House for the Raw Material Industry, Leipzig, 1984, 1. Edition, have been described in detail.
  • turbine extraction or counterpressure steam as a heat energy carrier for drying, which indirectly transfers its latent heat energy to the coal through condensation after it has been converted to saturated steam, for example, by injecting condensate, the known principle of "power Heat coupling "and a lowering of the fuel requirement attributable to drying.
  • power Heat coupling the known principle of "power Heat coupling” and a lowering of the fuel requirement attributable to drying.
  • the comparable sum of the flue gas emissions occurring during the individual refining and utilization sections could therefore fall to approximately 1.3 times the minimum required by natural law.
  • drag air since "drag air" is used in most cases, these advantages are not effective.
  • DD-PS 67 770 discloses a method and a device for predrying water-containing solid fuels, in particular soft lignite, in which the lignite is dried in a steam boiler in a fluidized bed dryer heated directly with steam before it is burned.
  • turbine extraction steam or counterpressure steam should be used and the principle of cogeneration should therefore be used.
  • DD-PS 67770 it is assumed that any suitable fluidizing medium, including steam, can be used to stir up the lignite above the fluidized bed in the fluidized bed dryer.
  • REPLACEMENT LEAF US Pat. No. 3,800,427 describes an indirectly heated fluidized bed drying process in which the lignite is whirled up with water vapor, so that the drying takes place in a water vapor atmosphere.
  • the invention is based on the fact that the lignite is heated in the steam atmosphere to such an extent that sulfur compounds split off, which accumulate on additives which may be present in the fluidized bed at the same time.
  • DE-PS 29 01 723 extends the use of a fluidized bed, which is indirectly heated with steam and fluidized with steam, to dry solid materials which contain less than 95% by mass of a vaporizable material.
  • the vaporizable material can also be other materials, such as solvents, which, in their vapor form as a fluidizing medium and in their saturated vapor form using different partial pressures, are also heat energy sources for the indirect heating of the fluidized bed.
  • DE-PS 29 01 723 restricts the permissible temperature of the fluidized bed in comparison to US-PS 38 00 427 and specifies that this is substantially below the decomposition temperature of the solid matter, so that the steam discharged from the fluidized bed dryer in the should consist essentially of the vaporizable material without contamination by other gaseous substances.
  • the table completely contains the vapor of the evaporable material emerging from the fluidized bed dryer.
  • the aim of the invention is to recover the predominant portion of the thermal energy used for drying and to reduce the emissions resulting from drying by evaporation, evaporation, pyrolysis, degassing and gasification, in particular those which cannot be condensed at ambient temperature.
  • the invention is based on the object, taking into account the technically realizable and reworkable principles of drying technology, a process and the device required for realizing the process for drying solid materials in a fluidized bed, the bed whose indirectly heated fluidized bed is preferably dried Solid material itself is formed, which is whirled up by the vaporizable material in vapor form, to achieve the goal of the invention in practical operation.
  • the decisive factor for the solution of the task is the knowledge gained that the conversion of the vaporizable portion of a solid material or sludge into its vapor form in a gas phase, which is formed by the vaporizable portion of the solid material, is dependent on an isobaric process sequence on a substance-specific boiling curve that characterizes the solid material of the material to be evaporated, which fixes the necessary temperature of the solid material depending on the proportion of the evaporable material in the solid material.
  • the temperature of the fluidized bed is therefore set as a function of the desired mass fraction of evaporable material in the solid material discharged from the fluidized bed by supplying solid material with a higher mass fraction of evaporable material for the removal and removal of dried solid material from the fluidized bed so that it corresponds to the substance-specific boiling temperature of the vaporizable material in the solid material discharged from the fluidized bed, so that the vapor discharged from the fluidized bed dryer also includes the gaseous substances of the vaporizable material and other gaseous impurities which are fed to the fluidized bed dryer, for example with the solid material contains only the volatile constituents of the solid fractions of the solid material or the sludge below this boiling temperature.
  • the steam discharged from the fluidized bed dryer is cooled indirectly, so that it condenses while releasing its latent heat energy and the gaseous substances contained in the steam of the vaporizable material, other gaseous impurities and decomposition products of the solids content, which at Ambient temperature is not condensable and is not soluble in the condensate of the vaporizable material, separated from the steam and then released into the environment or a landfill and / or other gas purification.
  • the method according to the invention normally requires the provision of the solid material to be dried in particulate form, preferably with a grain size of 0 to 10 mm, that is to say as a swirlable bulk material.
  • Solid material in particular sludge products, which are not directly suitable for producing a swirlable bulk material, can be converted into a consistency by admixing already dried solid material, which permits the production of an entry material corresponding to the requirements of the process.
  • Another way of converting solid material to be dried into a form corresponding to the method is to convert it into a pumpable and sprayable sludge form with condensate of the evaporable material. If it is necessary to maintain the bulk of the solid material to be dried, the process can be successfully implemented if the fluidized bed is not from the solid material itself, but from a smaller-sized solid material, which is different from the material to be dried 1. 2 to 5.0 times the density is marked, formed v.rd.
  • bed material is discharged from the fluidized bed with the dried solid material. This requires the bed material to be separated from the dried, coarse solid material and the bed material to be returned to the fluidized bed.
  • Decisive for the performance of the process is the temperature difference between the required temperature of the fluidized bed and the condensation temperature of the heating steam used for indirect heat transfer, which according to the invention should be between 10 and 150 K.
  • REPLACEMENT LEAF Pressure in the fluidized bed dryer which corresponds approximately to the ambient pressure of the atmosphere, requires the heating steam pressure of 0.2 to 4.0 MPa, which when using steam as heating medium, with slightly overheated heating steam, steam temperatures from 125 to 225 * C results. While high heating steam pressures enable the construction of small dryers, low heating steam pressures and thus low temperature differences between the condensing steam and the fluidized bed ensure good use of the advantages of combined heat and power.
  • the recovery of the predominant portion of the thermal energy used for drying and the separation of the gaseous, non-condensable and insoluble in the condensate contaminants, according to the invention, requires the condensation of the evaporated portion of the solid material. If the fluidized bed dryer operates under steam pressures which correspond to the pressure of the surrounding atmosphere, the substance-dependent condensation temperature determines the temperature level of the heat energy which can be recovered in the process. If the material to be evaporated is water, then the thermal energy recovered under the conditions according to the invention can reach a temperature of over 90'C, suitable for the fulfillment of heating heating and preheating tasks in industrial processes. If there is no need for thermal energy at this temperature level, the steam can be expanded with the release of technical work after appropriate cleaning of dust to such an extent that condensation at ambient temperature is still possible.
  • REPLACEMENT LEAF A further possibility is to increase the steam from the fluidized bed dryer, also after appropriate cleaning of dust, before its condensation by compression so far that the heat of condensation arises at a temperature level which is sufficient to fulfill the intended heat transfer, for example for heating the fluidized bed of the process according to the invention is sufficient.
  • a feed for the solid material to be dried to the fluidized bed dryer with a device for introducing the solid material into the fluidized bed dryer, is provided which is controlled by the fluidized bed temperature in terms of its output and which is based on the mass of the Solid material has at least 1.5 times the performance and, in the case of the introduction of particulate, vortex-capable or slurried solid material, at least 25% and, if lumpy, difficult or non-vortexable solid material is introduced, at least 75% of the surface of the fluidized bed is approximately uniform the entered solid aterial.
  • the fluidized bed covers radiators arranged in the fluidized bed dryer by at least 250 to 1000 mm.
  • Further components of the device are a discharge device for the dried solid material which is controlled in terms of its performance by the predetermined height of the fluidized bed and a mechanical dust separation for lowering the proportion of the grain size less than 0.5 mm with the vapor of the vaporizable material via the discharge discharged dust of the solid material below 10% by mass.
  • the device according to the invention includes a steam return with a compressor which increases the pressure of the steam to such an extent that the device reduces at least twice the amount of steam which is required for the transfer of the solid on the fluidized bed from the fixed bed to the fluidized bed, and a condenser which separates the gaseous impurities from the vapor by condensation of the material evaporated in the fluidized bed and, if appropriate, with the aid of suction of the environment or deodorization and / or other gas cleaning and the condensate via a pump to the condenser and for further processing and use.
  • the device according to the invention can be completed with a single and multi-stage compressor which raises the pressure of the vapor to such an extent that the condensation of the vapor during the temperature level required to fulfill the heat supply task can be carried out, for example for indirect heating of the fluidized bed.
  • the vapor of the evaporable material from the fluidized bed dryer can be fed to a steam turbine system after leaving the dedusting system, in which it is reduced to the extent that technical work is done in the pressure, that condensation at ambient temperature, e.g. 30 "C, is still possible.
  • the task of the example is to produce a dry lignite with a water content of 10 mass% from a raw lignite broken down in a conventional impact hammer mill to a grain size of 0 to 6 mm with a water content of 55% by mass.
  • the raw lignite mass flow is 100 t / h, that of dry lignite correspondingly 50 t / h.
  • a total of 50 t of coal water / h must be evaporated.
  • the calculation of the post-evaporation shows that the water content after discharge from the fluidized bed dryer 2 is reduced by 1.5% by mass, so that the dried coal with a water content of 11.5% by mass is removed from the fluidized bed dryer 2 and in Fluid bed dryer 249.152 kg water / h are to be evaporated.
  • the 2,848 kg of water evaporating per hour outside the fluidized bed dryer are suctioned off and fed as vapors with an air fraction of 2 kg / kg of water vapor to a separate dedusting system 9.
  • coal which corresponds to a volume of 142.9 irr at a cut weight of 0.7 kp / liter, 200 irr air / h are introduced into the fluidized bed dryer 2 in accordance with the stipulations made for the entry element.
  • the coal water in the example the vaporizable material, should contain 20 m 3 of dissolved gaseous impurities, in particular carbon dioxide, so that it is dried by drying in a
  • a heating surface density of 100 irr fluidized bed 5 is to be achieved, ie the fluidized bed dryer 2 has a fluidized bed 5 of approximately 32 m 2 , which with a width of the fluidized bed 5 of 4 m gives a length of 8 m for the fluidized bed 5. If the solid material on the fluidized bed 5 reaches its loosening point at an empty pipe speed of 0.35 m / s, then 80670 irr water vapor, which corresponds to 53.8 t / h, must be recirculated according to the invention.
  • the thermal energy requirement of the fluidized bed drying system according to the invention is 39.3 MW / h th , of which around 30.8 MW / h ⁇ , which is 78% of the thermal energy expended, is recovered in the condenser 18 at a temperature level of up to 95 * C can, with which this objective of the invention is achieved. If the non-condensable gaseous impurities are released into the environment with a saturation temperature of 60'C, around 275 irr / h are emitted.
  • the substance-specific boiling curve of the coal to be dried in the example requires a fluidized bed temperature of 118 ° C.
  • a heating steam with a minimum pressure of 0.59 MPa is required to achieve the temperature difference of 40 K between the fluidized bed 6 and the heating element 7.
  • the fluidized bed height must be regulated by the controlled discharge of dried coal due to the predetermined heating element 7 with a height of 2.0 m and a space between the heating element 7 and the fluidized bed 5 with a height of 250 mm to at least 2500 mm, but a maximum of 3250 mm , are regulated.

Landscapes

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

Abstract

L'invention concerne un procédé et un dispositif de séchage de matériaux solides. Le but de l'invention est de récupérer l'énergie thermique dépensée pour le séchage et de réduire les émissions produites lors du dégazage et de la gazéification. Il s'agit de créer un procédé et une installation de séchage de matériaux solides qui permettent de mettre en pratique le but de l'invention. A cet effet, le procédé comprend différentes étapes qui concernent la température du lit fluidisé, l'amenée de matières solides ayant une proportion élevée en masse de matériaux évaporables jusqu'au lit fluidisé et l'évacuation des matières solides séchées du lit fluidisé, ainsi que les matières gazeuses faisant partie du matériau évaporable et les autres impuretés gazeuses évacuées avec la vapeur. Le dispositif de mise en oeuvre du procédé comporte une combinaison de plusieurs caractéristiques.The invention relates to a method and a device for drying solid materials. The object of the invention is to recover the thermal energy spent on drying and to reduce the emissions produced during degassing and gasification. This involves creating a method and an installation for drying solid materials which make it possible to put the object of the invention into practice. To this end, the process comprises various stages which relate to the temperature of the fluidized bed, the supply of solid materials having a high proportion by mass of materials which can be evaporated to the fluidized bed and the evacuation of the dried solid materials from the fluidized bed, thus than gaseous materials forming part of the evaporable material and other gaseous impurities discharged with the vapor. The device for implementing the method comprises a combination of several characteristics.

Description

A A
Verfahren und Vorrichtung zum Trocknen von Feststoffmaterialien in einem indirekt beheiztenMethod and device for drying solid materials in an indirectly heated
WirbelschichtbettFluidized bed
Die Erfindung betrifft ein Verfahren und eine Vorrichtung zum Trocknen von Feststoffmaterialien, wie z.B. Braunkohle, Torf, Sand, Filterkuchen aus mechanischen Trennverfahren und von Schlämmen, die weniger als 98 % Masse-% eines ver¬ dampfungsfähigen Materials, z.B. Wasser, enthalten, in dem ein indirekt beheiztes Wirbelschichtbett gebildet wird, das das durch ein Wirbelmedium aufgewirbelte Feststoffmaterial enthält, wobei das Wirbelmedium das verdampfungsfähige Mate¬ rial in Dampfform ist und bei dem das aus dem Wirbel- schichttrockner ausgetragene getrocknete Material, gegebe¬ nenfalls nach Kühlung, einer weiteren Verarbeitung, Nutzung oder Deponie, das verdampfte Material jedoch einer Reini¬ gung, Kühlung, stofflichen Nutzung und/oder Wärmeenergie¬ rückgewinnung zugeführt werden kann"und das geeinget ist zur Anwendung i: der Industrie, dem Bauwesen, der Landwirtschaft sowie der kommunalen Entsorgung.The invention relates to a method and a device for drying solid materials, such as lignite, peat, sand, filter cakes from mechanical separation processes and sludges which contain less than 98% by mass of a vaporizable material, for example water, in which an indirectly heated fluidized bed is formed, which contains the solid material whirled up by a fluidizing medium, the fluidizing medium being the vaporizable material in vapor form and in which the dried material discharged from the fluidized bed dryer, optionally after cooling, further processing, Use or landfill, but the vaporized material can be supplied for cleaning, cooling, material use and / or heat energy recovery " and is suitable for use in industry, construction, agriculture and municipal disposal.
Trocknungsprozesse, insbesondere solche, die Wasser als ver¬ dampfungsfähigen Anteil aus Feststoffmaterialien abtrennen, haßen für die industrielle Produktion, das Bauwesen, die Energieumwandlung und die Entsorgung von Kommunen und Betrieben große ökonomische und gesellschaftliche Bedeutung. Die Trocknung ist teilweise so selbstverständlich oder so in die Prozeßabläufe integriert, wie bei der Verbrennung was¬ serhaltiger Brennstoffe, z.B. Braunkohle und von Schlämmen,Drying processes, in particular those which separate water as a vaporizable fraction from solid materials, were of great economic and social importance for industrial production, construction, energy conversion and the disposal of municipalities and businesses. Drying is sometimes as natural or integrated into the process as it is when burning water-containing fuels, e.g. Lignite and sludge,
ERSATZBLATT daß die von ihr durch erhöhten Energiebedarf und erhöhte Emission verursachten Umweltbelastungen als natürlich ange¬ sehen werden.REPLACEMENT LEAF that the environmental pollution caused by it due to increased energy requirements and increased emissions is regarded as natural.
Bei der energetischen Nutzung von Rohbraunkohle haben sich insbesondere im Kraftwerken Mahltrocknungsanlagen durchge¬ setzt, die einen Teil des im Kesselfeuerraumes erzeugten Feuergases als Wärmeenergieträger für die Mahltrocknung zurücksaugen, so daß 'durch Wärmeübertragung von 800 bis 1000'C heißen Feuergases an die Rohbraunkohle im Rauchgas- ström, vor oder während der Mahlung der Kohle zu Brennstaub, das Kohlewasser verdunstet. Im Buch Effenberger, H. "Dampf¬ erzeuger" VEB Verlag für Grundstoffindustrie, 1. Auflage, 1987, wird der Stand der Technik dazu ausführlich beschrie¬ ben. Bezogen auf die im Feuerraum des Dampfkessels freige¬ setzte Wärmeenergie verursacht diese Art der Trocknung mehr als das 1,5 fache des naturgesetzlich erforderlichen Mini¬ mums der Rauchgasemission bedingt durch den hohen Brenn¬ stoffeigenbedarf der Trocknung und dem Wasserdampfanteil im Rauchgas.In the energetic use of raw lignite, in particular in the power plants, mill drying systems have prevailed, which suck back part of the fire gas generated in the boiler furnace as a heat energy source for the mill drying, so that ' by means of heat transfer from 800 to 1000'C hot fire gas to the raw lignite in the flue gas flows, before or during the grinding of the coal into fuel dust, the coal water evaporates. In the book Effenberger, H. "Dampf¬ producers" VEB Verlag für Grundstoffindustrie, 1st edition, 1987, the state of the art is described in detail. In relation to the heat energy released in the combustion chamber of the steam boiler, this type of drying causes more than 1.5 times the minimum amount of flue gas emission required by natural law due to the high fuel consumption of drying and the water vapor content in the flue gas.
Bei der Braunkohlenveredelung werden vorrangig mit Dampf indirekt beheizte Teller- und Röhrentrockner, also Kon¬ takttrockner, verwendet, wie sie von Krug und Nauendorf im Buch "Braunkohlenbrikettierung" Band 1, Betriebsabschnitt Trocknung, VEB Deutscher Verlag für Grundstoffindustrie, Leipzig, 1984, 1. Auflage, ausführlich beschrieben wurden.In lignite refinement, plate and tube dryers, i.e. contact dryers, are used which are indirectly heated with steam, as described by Krug and Nauendorf in the book "Lignite Briquetting" Volume 1, Drying Section, VEB German Publishing House for the Raw Material Industry, Leipzig, 1984, 1. Edition, have been described in detail.
Durch die Verwendung von Turbinenentnahme- oder Gegendruck- dampf als Wärmeenergieträger für die Trocknung, der durch Kondensation seine latente Wärmeenergie indirekt an die Kohle überträgt, nachdem er z.B. durch Einspritzung von Kon¬ densat zu Sattdampf umgewandelt wurde, wird das bekannte Prinzip der "Kraft-Wärme-Kopplung" genutzt und eine Senkung des der Trocknung zuzurechnenden Brennstoffbedarfes erreicht. Gegenüber der in den Braunkohle -Kraftwerken übli¬ chen Mahltrocknung könnte deshalb die vergleichbare Summe der während der einzelnen Veredelungs- und Nutzungsab¬ schnitte anfallenden Rauchgasen-!ssion auf annähernd das 1,3- fache des naturgesetzlich erforderlichen Minimums sinken. Da in den meisten Fällen aber "Schleppluft" eingesetzt wird, werden diese Vorteile nicht wirksam.The use of turbine extraction or counterpressure steam as a heat energy carrier for drying, which indirectly transfers its latent heat energy to the coal through condensation after it has been converted to saturated steam, for example, by injecting condensate, the known principle of "power Heat coupling "and a lowering of the fuel requirement attributable to drying. Compared to the grinding drying that is common in lignite-fired power plants, the comparable sum of the flue gas emissions occurring during the individual refining and utilization sections could therefore fall to approximately 1.3 times the minimum required by natural law. However, since "drag air" is used in most cases, these advantages are not effective.
Die Einführung von indirekt beheizten Teller- und Röhren- trocknem und damit die Erschließung der Kraft-Wärme-Kopp¬ lung, z.B. in Braunkohlen- und Torfkraftwerken, ist bisher gescheitert, da die erforderlichen Brennstoffmassenströme unc das begrenzte Leistungsvermögen solcher Trockner zuein¬ ander im Widerspruch stehen und keine wirtschaftliche Lösung der Aufgabe ermöglichten.The introduction of indirectly heated plate and tube dryers and thus the development of cogeneration, e.g. in lignite and peat power plants has so far failed because the required fuel mass flows and the limited performance of such dryers contradict each other and did not allow an economical solution to the task.
Durch die DD-PS 67 770 sind ein Verfahren und eine Einrich¬ tung zur Vortrocknung wasserhaltiger fester Brennstoffe, insbesondere von Weichbraunkohle bekannt, bei welchen die Trocknung von Braunkohle vor ihrer Verbrennung in einem Dampfkessel in einem mit Dampf direkt beheizten Wirbe - schichttrockner vorgenommen wird. Wie bei den Teller- und Röhrentrocknern sollte hier Turbinenentnahme- oder Gegen¬ druckdampf verwendet und damit das Prinzip der Kraft-Wärme- Kopplung" genutzt werden.DD-PS 67 770 discloses a method and a device for predrying water-containing solid fuels, in particular soft lignite, in which the lignite is dried in a steam boiler in a fluidized bed dryer heated directly with steam before it is burned. As in the case of plate and tube dryers, turbine extraction steam or counterpressure steam should be used and the principle of cogeneration should therefore be used.
In der DD-PS 67770 wird davon ausgegangen, daß jedes geeignete Wirbelmedium, also auch Dampf, zur Auf irbelung der Braunkohle über dem Wirbelboden im Wirbelschichttrockner verwendet werden kann.In DD-PS 67770 it is assumed that any suitable fluidizing medium, including steam, can be used to stir up the lignite above the fluidized bed in the fluidized bed dryer.
ERSATZBLATT In der US-PS 38 00 427 ist ein indirekt beheiztes Wirbel¬ schichttrocknungsverfahren beschrieben, bei dem die Braun¬ kohle mit Wasserdampf aufgewirbelt wird, so daß die Trock¬ nung in einer Wasserdampfatmosphäre abläuft. Die Erfindung geht jedoch davon aus, daß in der Dampfatmosphäre die Braun¬ kohle soweit erhitzt wird, daß sich Schwefelverbindungen ab¬ spalten, die sich an gegebenenfalls gleichzeitig im Wirbel- schichtbett befindlichen Additiven anlagern.REPLACEMENT LEAF US Pat. No. 3,800,427 describes an indirectly heated fluidized bed drying process in which the lignite is whirled up with water vapor, so that the drying takes place in a water vapor atmosphere. However, the invention is based on the fact that the lignite is heated in the steam atmosphere to such an extent that sulfur compounds split off, which accumulate on additives which may be present in the fluidized bed at the same time.
Die DE-PS 29 01 723 erweitert die Verwendung eines mit Dampf indirekt beheizten und mit Dampf fluidisierten Wirbel- schichtbettes allgemein auf die Trocknung von Feststoffmate- rialien, die weniger als 95 Masse-% eines verdampfungsfähi¬ gen Materials enthalten. Wobei das verdampfungsfähige Mate¬ rial außer Wasser auch andere Materialien, wie Lösungsmit¬ tel, sein können, die in ihrer Dampfform als Wirbelmedium und in ihrer Sattdampfform unter Nutzung unterschiedlicher Partialdrücke auch Wärmeenergieträger zur indirekten Behei¬ zung des Wirbelbettes sind.DE-PS 29 01 723 extends the use of a fluidized bed, which is indirectly heated with steam and fluidized with steam, to dry solid materials which contain less than 95% by mass of a vaporizable material. In addition to water, the vaporizable material can also be other materials, such as solvents, which, in their vapor form as a fluidizing medium and in their saturated vapor form using different partial pressures, are also heat energy sources for the indirect heating of the fluidized bed.
Die DE-PS 29 01 723 schränkt gegenüber der US-PS 38 00 427 die zulässige Temperatur des Wirbelschichtbettes ein und legt fest, daß diese im wesentlichen unterhalb der Zerset¬ zungstemperatur des Feststoffmateriε.ls liegt, so daß der aus dem Wirbelschichttrockner abgeführte Dampf im wesentlichen ohne Verunreinigung durch andere gasförmige Stoffe aus dem verdampfungsfähigen Material bestehen soll.DE-PS 29 01 723 restricts the permissible temperature of the fluidized bed in comparison to US-PS 38 00 427 and specifies that this is substantially below the decomposition temperature of the solid matter, so that the steam discharged from the fluidized bed dryer in the should consist essentially of the vaporizable material without contamination by other gaseous substances.
Mehrjährige Forschungs- und Entwicklungsarbeiten haben erge¬ ben, daß das durch die DE-PS 29 01 723 bekannte Verfahren in der beschriebenen Form technisch nicht realisierbar ist. Es zeigte sich insbesondere, daß die Temperatur des Wirbel- schichtbettes nicht frei wählbar ist, und daß die gasförmi¬ gen Verunreinigungen des verdampfungsfähigen Materials prak-Research and development work lasting several years has shown that the method known from DE-PS 29 01 723 in the form described cannot be implemented technically. It was shown in particular that the temperature of the fluidized bed cannot be freely selected and that the gaseous contaminants of the vaporizable material are practically
ERSATZBLATT tisch unabhängig von der Wirbelschichtbettemperatur voll¬ ständig im aus dem Wirbelschichttrockner a- stretenden Dampf des verdampfungsfähigen Materials enthalten sind.REPLACEMENT LEAF regardless of the fluidized bed temperature, the table completely contains the vapor of the evaporable material emerging from the fluidized bed dryer.
Das Ziel der Erfindung besteht in der Rückgewinnung des überwiegenden Anteiles der für die Trocknung aufgewendeten Wärmeenergie und in der Reduzierung der bei der Trocknung durch Verdunstung, Verdampfung, Pyrolyse, Ent- und Vergasung entstehenden Emissionen, insbesondere der bei Umge¬ bungstemperatur nicht kondensierbaren.The aim of the invention is to recover the predominant portion of the thermal energy used for drying and to reduce the emissions resulting from drying by evaporation, evaporation, pyrolysis, degassing and gasification, in particular those which cannot be condensed at ambient temperature.
Der Erfindung liegt die Aufgabe zugrunde, unter Beachtung der technisch realisierbaren und nacharbeitbaren Grundsätze der Trocknungstechnik ein Verfahren und die für die Reali¬ sierung des Verfahrens erforderliche Vorrichtung zum Trock¬ nen von Feststoffmaterialien in einem Wirbelschicht, „ckner, dessen indirekt beheiztes Wirbelschichtbett vorzugsweise vom getrockneten Feststoffmaterial selbst gebildet wird i-fd das durch das verdampfungsfähige Material in Damp form aufgewir¬ belt wird, zu schaffen, die das Ziel der Erfindung im prak¬ tischen Betrieb erreichen.The invention is based on the object, taking into account the technically realizable and reworkable principles of drying technology, a process and the device required for realizing the process for drying solid materials in a fluidized bed, the bed whose indirectly heated fluidized bed is preferably dried Solid material itself is formed, which is whirled up by the vaporizable material in vapor form, to achieve the goal of the invention in practical operation.
Entscheidend für die Lösung der Aufgabe ist die gewonnene Erkenntnis, daß die Überführung des verdampfungsfähigen Anteiles eines Feststoffmaterials oder Schlammes in seine Dampfform in einer Gasphase, die vom verdampfungsfähigen Anteil des Feststoffmaterials gebildet wird bei isobarem Prozeßablauf abhängig ist von einer das Feststoffmaterial charakterisierenden, also stoffspezifischen Siedekurve des zu verdampfenden Materials, die die notwendige Temperatur des Feststoffmaterials in Abhängigkeit vom Anteil des ver¬ dampfungsfähigen Materials im Feststoff aterial fixiert.The decisive factor for the solution of the task is the knowledge gained that the conversion of the vaporizable portion of a solid material or sludge into its vapor form in a gas phase, which is formed by the vaporizable portion of the solid material, is dependent on an isobaric process sequence on a substance-specific boiling curve that characterizes the solid material of the material to be evaporated, which fixes the necessary temperature of the solid material depending on the proportion of the evaporable material in the solid material.
ERSATZBLATT Erfindungsgemäß wird deshalb die Temperatur des Wirbel- schichtbettes in Abhängigkeit vom gewünschten Masseanteil an verdampfungsfähigem Material im aus dem Wirbelschichtbett ausgetragenen Feststoffmaterial durch Zuführung von Fest¬ stoffmaterial mit höherem Masseanteil an verdampfungsfähigem Material zum und Abführung von getrocknetem Feststoffmate¬ rial aus dem Wirbelschichtbett so eingestellt, daß sie der stoffspezifischen Siedetemperatur des verdampfungsfähigen Materials im aus dem Wirbelschichtbett abgeführten Fest¬ stoffmaterial entspricht, so daß der aus dem Wirbel- schichttrockner abgeführte Dampf auch die gasförmigen Stoffe des verdampfungsfähigen Materials sowie andere gasförmige Verunreinigungen, die z.B. mit dem Feststoffmaterial dem Wirbelschichttrockner zugeführt werden, jedoch nur die unterhalb dieser Siedetemperatur flüchtigen Bestandteile der Feststoffanteile des Feststoffmaterials oder der Schlämme enthält.REPLACEMENT LEAF According to the invention, the temperature of the fluidized bed is therefore set as a function of the desired mass fraction of evaporable material in the solid material discharged from the fluidized bed by supplying solid material with a higher mass fraction of evaporable material for the removal and removal of dried solid material from the fluidized bed so that it corresponds to the substance-specific boiling temperature of the vaporizable material in the solid material discharged from the fluidized bed, so that the vapor discharged from the fluidized bed dryer also includes the gaseous substances of the vaporizable material and other gaseous impurities which are fed to the fluidized bed dryer, for example with the solid material contains only the volatile constituents of the solid fractions of the solid material or the sludge below this boiling temperature.
Es ist weiterhin erfindungsgemäß, daß der aus dem Wirbel- schichttrockner abgeführte Dampf indirekt gekühlt wird, so daß er unter Abgabe seiner latenten Wärmeenergie kondensiert und die im Dampf enthaltenen gasförmigen Stoffe des verdamp¬ fungsfähigen Materials, andere gasförmige Verunreinigungen und Zersetzungsprodukte des Feststoffanteiles, die bei Umge¬ bungstemperatur nicht kondensierbar und im Kondensat des verdampfungsfähigen Materials nicht löslich sind, aus dem Dampf separiert und danach an die Umgebung oder eine Depo¬ nierung und/oder andere Gasreinigung abgegeben werden.It is furthermore according to the invention that the steam discharged from the fluidized bed dryer is cooled indirectly, so that it condenses while releasing its latent heat energy and the gaseous substances contained in the steam of the vaporizable material, other gaseous impurities and decomposition products of the solids content, which at Ambient temperature is not condensable and is not soluble in the condensate of the vaporizable material, separated from the steam and then released into the environment or a landfill and / or other gas purification.
Das erfindungsgemäße Verfahren erfordert im Normalfall die Bereitstellung des zu trocknenden Feststoffmaterials teil- chenförmig, vorzugsweise mit einer Körnung von 0 bis 10 mm, also als wirbelfähiges Schüttgut.The method according to the invention normally requires the provision of the solid material to be dried in particulate form, preferably with a grain size of 0 to 10 mm, that is to say as a swirlable bulk material.
ERSATZBLATT Feststoffmaterial, insbesondere Schlammprodukte, die direkt nicht geeignet sind zur Herstellung eines wirbelfähigen Schüttgutes, können durch Zumischung von bereits getrockne¬ tem Feststoffmaterial in eine solche Konsistenz überführt werden, die die Herstellung eines den Anforderungen des Ver¬ fahrens entsprechenden Eintragsgutes gestattet. Ein anderer Weg zu trocknendes Feststoffmaterial in eine dem Verfahren entsprechende Form zu überführen besteht darin, es mit Kon¬ densat des verdampfungsfähigen Materials in eine pump- und versprühfähige Schlammform umzuwandeln. Ist es erforderlich, die Großstuckigkeit des zu trocknenden Feststoffmaterials zu erhalten, dann kann das Verfahren erfolgreich realisiert werden, wenn das Wirbelbett nicht vom Feststoffraaterial £ jlbst, sondern von einem kleinerkörnigen Feststoff aterial, das d-.rch eine gegenüber dem zu trocknenden Material 1,2 bis 5,0 fache Dichte gekennzeichnet ist, gebildet v.rd.REPLACEMENT LEAF Solid material, in particular sludge products, which are not directly suitable for producing a swirlable bulk material, can be converted into a consistency by admixing already dried solid material, which permits the production of an entry material corresponding to the requirements of the process. Another way of converting solid material to be dried into a form corresponding to the method is to convert it into a pumpable and sprayable sludge form with condensate of the evaporable material. If it is necessary to maintain the bulk of the solid material to be dried, the process can be successfully implemented if the fluidized bed is not from the solid material itself, but from a smaller-sized solid material, which is different from the material to be dried 1. 2 to 5.0 times the density is marked, formed v.rd.
In diesem Falle muß davon ausgegangen werden, daß mit dem getrockneten Feststoffmaterial Bettmaterial aus dem Wirbel- schichtbett ausgetragen wird. Das erfordert eine Abtrennung des Bettmaterials vom getrockneten grobstückigen Feststoff- material und eine Rückführung des Bettmaterials in das Wir¬ belschichtbett. Insbesondere während instationärer Betriebs- phasen beim Betrieb des erfindungsgemäßen Verfahrens kann es erforderlich sein, alternativ zur Rückführung des verdamp¬ fungsfähigen Materials in Dampfform oder zusätzlich Wirbel- medium von außen, z.B. aus einem separaten System, dem Wir¬ belschichttrockner zuzuführen.In this case it must be assumed that bed material is discharged from the fluidized bed with the dried solid material. This requires the bed material to be separated from the dried, coarse solid material and the bed material to be returned to the fluidized bed. In particular, during unsteady operating phases in the operation of the method according to the invention, it may be necessary, as an alternative to recycling the vaporizable material in vapor form or additionally from the outside, e.g. from a separate system, the fluidized bed dryer.
Entscheidend für die Leistung des Verfahrens ist die Tempe¬ raturdifferenz zwischen erforderlicher Temperatur des Wir¬ belschichtbettes und Kondensationstemperatur des zur indi¬ rekten Wärmeübertragung verwendeten Heizdampfes, die erfin¬ dungsgemäß zwischen 10 und 150 K betragen soll. Bei einemDecisive for the performance of the process is the temperature difference between the required temperature of the fluidized bed and the condensation temperature of the heating steam used for indirect heat transfer, which according to the invention should be between 10 and 150 K. At a
ERSATZBLATT Druck im Wirbelschichttrockner, der annähernd dem Umgebungs¬ druck der Atmosphäre entspricht, erfordert das Heizdampf¬ drücke von 0,2 bis 4,0 MPa, was bei Verwendung von Wasser¬ dampf als Heizmedium, bei leicht überhitztem Zustand des Heizdampfes Dampf emperaturen von 125 bis 225*C zur Folge hat. Während hohe Heizdampfdrücke den Bau kleiner Trockner ermöglichen, sichern niedrige Heizdampfdrücke und damit niedrige Temperaturdifferenzen zwischen kondensierendem Dampf und Wirbelschichtbett eine gute Nutzung der Vorteile der Kraft-Wärme-Kopplung.REPLACEMENT LEAF Pressure in the fluidized bed dryer, which corresponds approximately to the ambient pressure of the atmosphere, requires the heating steam pressure of 0.2 to 4.0 MPa, which when using steam as heating medium, with slightly overheated heating steam, steam temperatures from 125 to 225 * C results. While high heating steam pressures enable the construction of small dryers, low heating steam pressures and thus low temperature differences between the condensing steam and the fluidized bed ensure good use of the advantages of combined heat and power.
Die dem Ziel der Erfindung entsprechende Rückgewinnung des überwiegenden Anteiles der für die Trocknung aufgewendeten Wärmeenergie und die Separation der gasförmigen, nicht kon¬ densierbaren und im Kondensat nicht löslichen Verunreinigun¬ gen erfordert erfindungsgemäß die Kondensation des verdampf¬ ten Anteils des Feststoffmaterials. Arbeitet der Wirbel- schichttrockner unter Dampfdrücken, die dem Druck der umge¬ benden Atmosphäre entsprechen, dann bestimmt die stoffabhän¬ gige Kondensationstemperatur das Temperaturniveau der dabei zurückgewinnbaren Wärmeenergie. Ist das zu verdampfende Material Wasser, dann kann die unter den erfindungsgemäßen Bedingungen zurückgewonnene Wärmeenergie eine Temperatur von über 90'C erreichen, geeignet für die Erfüllung von Aufgaben der Heizwärmeversorgung und der Vorwärmung in industriellen Prozessen. Gibt es bei diesem Temperaturniveau keinen Wärme- energiebedarf, dann kann der Dampf unter Abgabe von techni¬ scher Arbeit nach entsprechender Reinigung von Staub soweit expandiert werden, daß eine Kondensation bei Umgebungstempe¬ ratur noch möglich ist.The recovery of the predominant portion of the thermal energy used for drying and the separation of the gaseous, non-condensable and insoluble in the condensate contaminants, according to the invention, requires the condensation of the evaporated portion of the solid material. If the fluidized bed dryer operates under steam pressures which correspond to the pressure of the surrounding atmosphere, the substance-dependent condensation temperature determines the temperature level of the heat energy which can be recovered in the process. If the material to be evaporated is water, then the thermal energy recovered under the conditions according to the invention can reach a temperature of over 90'C, suitable for the fulfillment of heating heating and preheating tasks in industrial processes. If there is no need for thermal energy at this temperature level, the steam can be expanded with the release of technical work after appropriate cleaning of dust to such an extent that condensation at ambient temperature is still possible.
ERSATZBLATT Eine weitere Möglichkeit besteht darin, den Dampf aus dem Wirbelschichttrockner, ebenfalls nach entsprechender Reini¬ gung von Staub, vor seiner Kondensation durch Kompression soweit im Druck zu erhöhen, daß die Kondensationswärme bei einem Temperaturniveau anfällt, das zur Erfüllung der vorge¬ sehenen Wärmeübertragung, z.B. zur Auf eizung des Wirbel- schichtbettes des erfindungsgemäßen Verfahrens, ausreicht.REPLACEMENT LEAF A further possibility is to increase the steam from the fluidized bed dryer, also after appropriate cleaning of dust, before its condensation by compression so far that the heat of condensation arises at a temperature level which is sufficient to fulfill the intended heat transfer, for example for heating the fluidized bed of the process according to the invention is sufficient.
Zur Realisierung des erfindungsgemäßen Verfahrens ist des¬ halb eine von der Wirbelschichtbettemperatur in ihrer Lei¬ stung geregelte Zuführung für das zu trocknende Feststoffma¬ terial zum Wirbelschichttrockner mit einer Vorrichtung zum Eintragen des Feststoffmaterials in den Wirbelschichttrock¬ ner vorgesehen, die bezogen auf die einzutragende Masse des Feststoffmaterials mindestens eine 1,5 fache Leistung hat und die im Falle des Eintragens von teilchenförmigen, wir¬ belfähigen oder aufgeschlämmten Feststoffmaterial mindestens 25 % und bei Eintrag von klumpenförmigem, schwer oder nicht wirbelfähigen Feststoffmaterial mindestens 75 % der Oberflä¬ che des Wirbelschichtbettes annähernd gleichmäßig mit dem eingetragenen Feststoff aterial beaufschlagt.In order to implement the method according to the invention, a feed for the solid material to be dried to the fluidized bed dryer, with a device for introducing the solid material into the fluidized bed dryer, is provided which is controlled by the fluidized bed temperature in terms of its output and which is based on the mass of the Solid material has at least 1.5 times the performance and, in the case of the introduction of particulate, vortex-capable or slurried solid material, at least 25% and, if lumpy, difficult or non-vortexable solid material is introduced, at least 75% of the surface of the fluidized bed is approximately uniform the entered solid aterial.
Das Wirbelschichtbett überdeckt im Wirbelschichttrockner an¬ geordnete Heizkörper um mindestens 250 bis 1000 mm. Weitere Bestandteile der Vorrichtung sind eine durch die vorgegebene Höhe des Wirbelschichtbettes in ihrer Leistung gesteuerte Austragsvorrichtung für das getrocknete Feststoffmaterial und eine mechanische Staubabscheidung zur Senkung des Antei¬ les der Körnung kleiner 0,5 mm an mit dem Dampf des verdamp¬ fungsfähigen Materials über den Austrag ausgetragenen Staub des Feststoffmaterials unter 10 Masse-%.The fluidized bed covers radiators arranged in the fluidized bed dryer by at least 250 to 1000 mm. Further components of the device are a discharge device for the dried solid material which is controlled in terms of its performance by the predetermined height of the fluidized bed and a mechanical dust separation for lowering the proportion of the grain size less than 0.5 mm with the vapor of the vaporizable material via the discharge discharged dust of the solid material below 10% by mass.
ERSATZBLATT In einer Entstaubungsanlage wird der Staubanteil im aus dem Wirbelschichttrockner abgeführten Dampf unter 50 mg/kg Dampf gesenkt. Ferner gehören zur erfindungsgemäßen Vorrichtung eine Dampfrückführung mit einem Verdichter, der den Druck des Dampfes soweit erhöht, daß durch die Vorrichtung minde¬ stens die doppelte Menge an Dampf reduziert, die für den Übergang des Feststoffes auf dem Wirbelboden vom Festbett zum Wirbelschichtbett erforderlich ist, sowie ein Kondensa¬ tor, der durch Kondensation des im Wirbelschichtbett ver¬ dampften Materials die gasförmigen Verunreinigungen aus dem Dampf separiert und diese gegebenenfalls mit Hilfe einer Ab¬ saugung der Umwelt oder Deodorierung und/oder anderer Gas- reinigung und das Kondensat über eine Pumpe dem Kondensator und einer weitergehenden Aufbereitung und Nutzung zuführt.REPLACEMENT LEAF In a dedusting system, the proportion of dust in the steam discharged from the fluidized bed dryer is reduced to below 50 mg / kg steam. Furthermore, the device according to the invention includes a steam return with a compressor which increases the pressure of the steam to such an extent that the device reduces at least twice the amount of steam which is required for the transfer of the solid on the fluidized bed from the fixed bed to the fluidized bed, and a condenser which separates the gaseous impurities from the vapor by condensation of the material evaporated in the fluidized bed and, if appropriate, with the aid of suction of the environment or deodorization and / or other gas cleaning and the condensate via a pump to the condenser and for further processing and use.
Ist das Temperaturniveau der Kondensation des Dampfes des verdampfungsfähigen Materials nicht geeignet zur Erfüllung anstehender Wärmeversorgungsaufgaben, so kann die erfin¬ dungsgemäße Vorrichtung mit einem ein- und mehrstufigen Kom¬ pressor komplettiert werden, der den Druck des Dampfes soweit anhebt, daß die Kondensation des Dampfes beim zur Erfüllung der Wärmeversorgungsaufgabe erforderlichen Tempe¬ raturniveau durchgeführt werden kann, z.B. zur indirekten Beheizung des Wirbelschichtbettes. Ist auch diese Variante zur Nutzung der rückgewonnenen Wärmeenergie nicht zweck¬ mäßig, dann kann der Dampf des verdampfungsfähigen Materials aus dem Wirbelschichttrockner nach Verlassen der Entstau¬ bungsanlage einer Dampfturbinenanlage zugeführt werden, in der er unter Abgabe technischer Arbeit im Druck soweit redu¬ ziert wird, daß eine Kondensation bei Umgebungstemperatur, z.B. 30"C, noch möglich ist.If the temperature level of the condensation of the vapor of the vaporizable material is not suitable for fulfilling pending heat supply tasks, the device according to the invention can be completed with a single and multi-stage compressor which raises the pressure of the vapor to such an extent that the condensation of the vapor during the temperature level required to fulfill the heat supply task can be carried out, for example for indirect heating of the fluidized bed. If this variant for utilizing the recovered thermal energy is also not expedient, then the vapor of the evaporable material from the fluidized bed dryer can be fed to a steam turbine system after leaving the dedusting system, in which it is reduced to the extent that technical work is done in the pressure, that condensation at ambient temperature, e.g. 30 "C, is still possible.
ERSATZBLATT Aπg-FtihT-nngsbeispielREPLACEMENT LEAF Aπg-FtihT-nngsexample
Das erfindungsgemäße Verfahren und die erfindungsgemäße Vor¬ richtung werden mit Hilfe der beigefügten Zeichnung nachfol¬ gend beschrieben.The method according to the invention and the device according to the invention are described below with the aid of the attached drawing.
Die Aufgabe des Beispieles besteht darin, aus einer in einer üblichen Prallhammermühle auf eine Körnung von 0 bis 6 mm gebrochenen Rohbraunkohle mit einem Wassergehalt von 55 Masse-% eine Trockenbraunkohle mit einem Wassergehalt von 10 Masse-% herzustellen.The task of the example is to produce a dry lignite with a water content of 10 mass% from a raw lignite broken down in a conventional impact hammer mill to a grain size of 0 to 6 mm with a water content of 55% by mass.
Der Rohbraunkohlemassestrom beträgt 100 t/h, der der Trok- kenbraunkohle dementsprechend 50 t/h. Zu verdampfen sind also insgesamt 50 t Kohlewasser/h. Die Berechnung der Nach¬ verdampfung ergibt, daß sich der Wassergehalt nach Austrag aus dem Wirbelschichttrockner 2 um 1,5 Masse-% reduziert, so daß die getrocknete Kohle mit einem Wassergehalt von 11,5 Masse-% aus dem Wirbelschichttrockner 2 auszutragen ist und im Wirbelschichttrockner 249.152 kg Wasser/h zu verdampfen sind. Die je Stunde außerhalb des Wirbelschichttrockners 2 848 nachverdampfenden kg Wasser werden abgesaugt und als Brüden mit einem Luftanteil von 2 kg/kg Wasserdampf einer separaten Entstaubungsanlage 9 zugeführt.The raw lignite mass flow is 100 t / h, that of dry lignite correspondingly 50 t / h. A total of 50 t of coal water / h must be evaporated. The calculation of the post-evaporation shows that the water content after discharge from the fluidized bed dryer 2 is reduced by 1.5% by mass, so that the dried coal with a water content of 11.5% by mass is removed from the fluidized bed dryer 2 and in Fluid bed dryer 249.152 kg water / h are to be evaporated. The 2,848 kg of water evaporating per hour outside the fluidized bed dryer are suctioned off and fed as vapors with an air fraction of 2 kg / kg of water vapor to a separate dedusting system 9.
Mit der Kohle, die bei einem Schnittgewicht von 0,7 kp/Liter einem Volumen von 142,9 irr entspricht, werden entsprechend der für das Eintragsorgan getroffenen Festlegungen 200 irr Luft/h in den Wirbelschichttrockner 2 eingetragen. Das Koh¬ lewasser, im Beispiel das verdampfungsfähige Material, soll 20 m3 gelöste gasförmige Verunreinigungen, insbesondere Koh¬ lendioxid, enthalten, so daß der durch Trocknung in einerWith the coal, which corresponds to a volume of 142.9 irr at a cut weight of 0.7 kp / liter, 200 irr air / h are introduced into the fluidized bed dryer 2 in accordance with the stipulations made for the entry element. The coal water, in the example the vaporizable material, should contain 20 m 3 of dissolved gaseous impurities, in particular carbon dioxide, so that it is dried by drying in a
Stunde aus Kohlewasser erzeugte Dampf insgesamt 220 irr gas¬ förmige Verunreinigungen enthält, die entsprechend Sätti-Steam generated from coal water for an hour contains a total of 220 irr gaseous impurities, which
ERSATZBLATT gungstemperatur mit Wasserdampf beladen im Kondensator 18 separiert und an die Umgebung abgegeben werden.REPLACEMENT LEAF supply temperature with water vapor separated in the condenser 18 and released into the environment.
Bei einer Wärmedurchgangszahl vom kondensierenden Heizdampf an das Kohle-Wirbelschichtbett 2 k = 300 W/m2. K und einem Wärmebedarf von 800 W/kg zu verdampfendes Kohlewasser ergibt sich, daß im Wirbelschichttrockner 2, bei einer für die Wärmeübertragung wirksamen Temperaturdifferenz von 40 K, eine Heizfläche von 3277 irr installiert werden muß.With a heat transfer coefficient from the condensing heating steam to the coal fluidized bed 2 k = 300 W / m 2 . K and a heat requirement of 800 W / kg of coal water to be evaporated, it follows that in the fluidized bed dryer 2, with a temperature difference of 40 K effective for heat transfer, a heating surface of 3277 must be installed irr.
Bei einer Höhe der Heizkörper 7 von 2,00 m soll eine Heiz- flächendichte von 100 irr Wirbelboden 5 erreicht werden, d.h., der Wirbelschichttrockner 2 hat einen rund 32 m2 großen Wirbelboden 5, was bei einer Breite des Wirbelbo¬ dens 5 von 4 m eine Baulänge für den Wirbelboden 5 von 8 m ergibt. Erreicht das Feststoffmaterial auf dem Wirbelboden 5 bei Leerrohrgeschwindigkeit von 0,35 m/s seinen Lockerungs¬ punkt, dann müssen erfindungsgemäß 80670 irr Wasserdampf, das entspricht 53,8 t/h, rezierkuliert werden. Aus dem Wirbel- schichttrockner 2 müssen deshalb rund 103 t Wasserdampf/h, das entspricht annähernd einem Volumen von 150 000 πr/h, abgeführt und weitgehend entstaubt werden. Nur der durch Verdampfung von 49152 kg Kohlewassdr entstehende Dampf, der mit 220 irr nichtkondensierbaren gasförmigen Verunreinigungen belastet ist, wird dem Kondensator 18 zugeführt.At a height of the radiators 7 of 2.00 m, a heating surface density of 100 irr fluidized bed 5 is to be achieved, ie the fluidized bed dryer 2 has a fluidized bed 5 of approximately 32 m 2 , which with a width of the fluidized bed 5 of 4 m gives a length of 8 m for the fluidized bed 5. If the solid material on the fluidized bed 5 reaches its loosening point at an empty pipe speed of 0.35 m / s, then 80670 irr water vapor, which corresponds to 53.8 t / h, must be recirculated according to the invention. About 103 t of water vapor / h, which corresponds approximately to a volume of 150,000 πr / h, must therefore be removed from the fluidized bed dryer 2 and largely dedusted. Only the steam resulting from the evaporation of 49152 kg of coal water, which is contaminated with 220 non-condensable gaseous impurities, is fed to the condenser 18.
Der Wärmeenergiebedarf der erfindungsgemäßen Wirbel¬ schichttrocknungsanlage beträgt 39,3 MW/hth, wovon im Kon¬ densator 18 bei einem Temperaturniveau bis 95*C rund 30,8 MW/h^, das sind 78% der aufgewendeten Wärmeenergie, zurück¬ gewonnen werden können, womit diese Zielstellung der Erfin¬ dung erreicht wird. Werden die nichtkondensierbaren gasförmigen Verunreinigungen an die Umgebung mit einer Sättigungsteraperatur von 60'C abgegeben, dann werden rund 275 irr/h emitiert. Bezogen auf eine Röhrentrockneranlage mit vergleichbarer Leistung, die rund 170 000 irr Brüden/h emitiert, was bei einem Staubgehalt von 50 mg/m3 einer Belastung der Umwelt mit 8,5 kg Kohlen¬ staub/h entspricht, sind das 0,2% der üblichen Emissionen.The thermal energy requirement of the fluidized bed drying system according to the invention is 39.3 MW / h th , of which around 30.8 MW / h ^, which is 78% of the thermal energy expended, is recovered in the condenser 18 at a temperature level of up to 95 * C can, with which this objective of the invention is achieved. If the non-condensable gaseous impurities are released into the environment with a saturation temperature of 60'C, around 275 irr / h are emitted. Based on a tube dryer system with comparable performance, which emits around 170,000 irr vapors / h, which corresponds to a pollution of the environment with 8.5 kg coal dust / h at a dust content of 50 mg / m 3 , that is 0.2% the usual emissions.
Die stoffspezifische Siedekurve der im Beispiel zu trocknen¬ den Kohle erfordert eine Wirbelbettemperatur von 118'C. Zur Erzielung der angesetzten Temperaturdifferenz zwischen dem Wirbelschichtbett 6 und dem Heizkörper 7 von 40 K ist ein Heizdampf mit einem Mindestdruck von 0,59 MPa erforderlich.The substance-specific boiling curve of the coal to be dried in the example requires a fluidized bed temperature of 118 ° C. A heating steam with a minimum pressure of 0.59 MPa is required to achieve the temperature difference of 40 K between the fluidized bed 6 and the heating element 7.
Die Wirbelschichtbetthöhe muß durch den geregelten Austrag von getrockneter Kohle aufgrund der mit 2,0 m Höhe vorgege¬ benen Heizkörper 7 und einem zwischen dem Heizkörper 7 und dem Wirbelboden 5 vorhandenen Freiraum mit einer Höhe von 250 mm auf mindestens 2500 mm, aber maximal 3250 mm, einge¬ regelt werden.The fluidized bed height must be regulated by the controlled discharge of dried coal due to the predetermined heating element 7 with a height of 2.0 m and a space between the heating element 7 and the fluidized bed 5 with a height of 250 mm to at least 2500 mm, but a maximum of 3250 mm , are regulated.
ERSATZBLATT REPLACEMENT LEAF

Claims

P a t e n t a n s p r ü c h e P a t e n t a n s r u c h e
Verfahren zum Trocknen von Feststoffmaterialien, wie Braunkohle, Torf, Filterkuchen aus mechanischen Trenn¬ verfahren, und von Schlämmen, die weniger als 98 Mas- se-% eines verdampfungsfähigen Materials, insbesondere Wasser, enthalten, die einem Wirbelschichttrockner zu¬ geführt werden, indem ein indirekt beheiztes Wirbel- schichtbett gebildet wird, das das durch ein Wirbelme¬ dium aufgewirbelte Feststoffmaterial enthält, wobei das Wirbelmedium das verdampfungsfähige Material in Dampf- form ist und bei dem das aus dem Wirbelschichttrockner ausgetragene getrocknete Material, gegebenenfalls nach Kühlung, einer weiteren Verarbeitung, Nutzung oder Deponie, das verdampfte Material jedoch einer Reini¬ gung, Kühlung und/oder Kondensation zugeführt werden, dadurch gekennzeichnet, daß die Temperatur des Wirbel- schichtbettes in Abhängigkeit vom gewünschten Massean¬ teil an verdampfungsfähigem Material im aus dem Wirbel- schichtbett ausgetragenen Feststoffmaterial, durch Zu¬ führung von Feststoffmaterial mit höherem Masseanteil an verdampfungsfähigem Material zum und Abführung von getrocknetem Feststoffmaterial aus dem Wirbelschicht¬ bett, so eingestellt wird, daß sie der Stoffspezifi¬ schen Siedetemperatur des verdampfungsfähigen Materials im aus dem Wirbelschichtbett abgeführten Feststoffmate¬ rial entspricht, der aus dem Wirbelschichttrockner abgeführte Dampf die gasförmigen Stoffe des verdamp¬ fungsfähigen Materials sowie andere gasförmige Verun¬ reinigungen, die z.B. mit dem Feststoffmaterial demProcess for drying solid materials, such as lignite, peat, filter cakes from mechanical separation processes, and sludges which contain less than 98% by mass of an evaporable material, in particular water, which are fed to a fluidized bed dryer by a indirectly heated fluidized bed is formed which contains the solid material whirled up by a fluidized medium, the fluidized medium being the vaporizable material in vapor form and in which the dried material discharged from the fluidized bed dryer, optionally after cooling, further processing, use or landfill, but the evaporated material is fed to cleaning, cooling and / or condensation, characterized in that the temperature of the fluidized bed depends on the desired mass fraction of evaporable material in the solid material discharged from the fluidized bed Zu¬ f Feeding of solid material with a higher mass fraction of evaporable material to and removal of dried solid material from the fluidized bed is adjusted so that it corresponds to the substance-specific boiling temperature of the evaporable material in the solid material discharged from the fluidized bed, which is discharged from the fluidized bed dryer Steam the gaseous substances of the vaporizable material as well as other gaseous impurities which, for example with the solid material
ERSATZBLATT Wirbelschichttrockner zugeführt werden, jedoch nur die unterhalb dieser Siedetemperatur flüchtigen Bestand¬ teile der Feststoffanteile des Feststoffmaterials oder der Schlämme enthält, deren nichtkondensierbaren und i Kondensat des verdampfungsfähigen Materials nicht lös¬ lichen Anteile durch Kühlung und Kondensation des Dampfes des verdampfungsfähigen Materials separiert und danach an die Umgebung oder einer Deodorierung und/oder anderen Gasreinigung zugeführt werden.REPLACEMENT LEAF Fluid bed dryers are supplied, however, only contain those components of the solid components of the solid material or the sludge which are volatile below this boiling temperature, their non-condensable and non-condensable components of the evaporable material separated by cooling and condensation of the vapor of the evaporable material and then to the Environment or a deodorization and / or other gas cleaning.
Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Feststoffmaterial als w rbelfähiges, teilchenförmi- ges Schüttgut in den Wirbelschichttrockner eingetragen wird und dort selbst das Wirbelschichtbett bildet.A method according to claim 1, characterized in that the solid material is introduced into the fluidized bed dryer as a swellable, particulate bulk material and forms the fluidized bed there itself.
Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das dem Wirbelschichtbett zugeführte Feststoffmaterial eine Mischung aus aus dem Wirbelschichttrockner ausge¬ tragenem, getrocknetem und frischem, ungetrocknetem Feststoffmaterial ist.A method according to claim 1, characterized in that the solid material fed to the fluidized bed is a mixture of dried and fresh, undried solid material discharged from the fluidized bed dryer.
Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das dem Wirbelschichttrockner zugeführte Feststoffmate¬ rial mit Kondensat des verdampfungsfähigen Materials als pumpfähiger Schlamm über dem Wirbelschichtbett im Wirbelschichttrockner versprüht wird und das Feststoff- material selbst das Wirbelschichtbett bildet.A method according to claim 1, characterized in that the solid material supplied to the fluidized bed dryer is sprayed with condensate of the vaporizable material as pumpable sludge over the fluidized bed in the fluidized bed dryer and the solid material itself forms the fluidized bed.
ERSATZBLATT Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Feststoffmaterial grobstückig oder klumpenförmig, d.h. schwer oder nicht wirbelfähig, in das Wirbel- schichtbett, das aus wirbelfähigem, teilchenförraigem Material mit einer Dichte, die 1,2- bis 5,0-fach höher ist als die des klumpenförmigen Materials, gebildet wird, eingetragen wird.REPLACEMENT LEAF A method according to claim 1, characterized in that the solid material is coarse or lump-shaped, ie difficult or not swirlable, in the fluidized bed, which is made of swirlable, particulate material with a density that is 1.2 to 5.0 times higher than that of the lumpy material being formed is registered.
Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß das getrocknete Feststoffmaterial in Verbindung mit einem Teil des teilchenförmigen, wirbelfähigen Materi¬ als aus dem Wirbelschichtbett ausgetragen, grobstücki¬ ges und wirbelfähiges Material getrennt und das Wirbel- fähige Material in das Wirbelschichtbett rückgeführt wird.A method according to claim 5, characterized in that the dried solid material in connection with a part of the particulate, fluidizable material is discharged from the fluidized bed, coarse and fluid material is separated and the fluidized material is returned to the fluidized bed.
Verfahren nach den Ansprüchen 1 und 5, dadurch gekenn¬ zeichnet, daß das Wirbelmedium dem Prozeß von außen zugeführt wird.Method according to claims 1 and 5, characterized gekenn¬ characterized in that the fluidizing medium is fed to the process from the outside.
Verfahren nach den Ansprüchen 1 und 5, dadurch gekenn¬ zeichnet, daß der für die indirekte Beheizung des Wir¬ belschichtbettes verwendete Dampf in seinen Parametern Druck im Bereich von 0,2 bis 4,0 MPa und Temperatur im Bereich von 125 bis 225*C so eingestellt wird, daß die mittlere Temperaturdifferenz zwischen kondensierendem Dampf und Wirbelschichtbett 10 bis 150 K beträgt.Process according to claims 1 and 5, characterized gekenn¬ characterized in that the steam used for the indirect heating of the fluidized bed in its parameters pressure in the range of 0.2 to 4.0 MPa and temperature in the range of 125 to 225 * C. is set so that the average temperature difference between condensing steam and fluidized bed is 10 to 150 K.
ERSATZBLATT Verfahren nach den Ansprüchen 1 und 5, dadurch gekenn¬ zeichnet, daß der Druck im Wirbelschichtbett etwa dem Umgebungsdruck der Atmosphäre entspricht.REPLACEMENT LEAF Process according to claims 1 and 5, characterized gekenn¬ characterized in that the pressure in the fluidized bed corresponds approximately to the ambient pressure of the atmosphere.
10. Verfahren nach den Ansprüchen 1 und 5, dadurch gekenn¬ zeichnet, daß der Druck des aus dem Wirbelschichttrock¬ ner abgeführten Dampfes des verdampfungsfähigen Mate¬ rials, nach entsprechender Reinigung von festen Bestandteilen in einer Vorrichtung des Standes der Technik, aber vor der indirekten Übertragung seiner latenten Wärmeenergie an einen anderen Wärmeenergieträ- σer durch Zuführung von mechanischer Energie erhöht oder durch Expansion unter Abgabe mechanischer Energie gesenkt wird.10. The method according to claims 1 and 5, characterized gekenn¬ characterized in that the pressure of the evaporated from the fluidized bed dryer vapor of the evaporable Mate¬ rials, after appropriate cleaning of solid components in a device of the prior art, but before the indirect Transfer of its latent heat energy to another heat energy carrier is increased by supplying mechanical energy or reduced by expansion while releasing mechanical energy.
11. Verfahren nach den Ansprüchen 1, 5 und 10, dadurch gekennzeichnet, daß der im Druck erhöhte Dampf des ver¬ dampfungsfähigen Materials zur indirekten Beheizung des Wirbelschichtbettes verwendet wird.11. The method according to claims 1, 5 and 10, characterized in that the vapor of the evaporable material, which is increased in pressure, is used for the indirect heating of the fluidized bed.
12. Vorrichtung zur Durchführung des Verfahrens nach den Ansprüchen 1 bis 11, gekennzeichnet durch die Kombina¬ tion folgender Merkmale:12. Device for performing the method according to claims 1 to 11, characterized by the combination of the following features:
a) eine von der Wirbelschichtbettemperatur in ihrera) one of the fluidized bed temperature in your
Lsistung stufenlos geregelte Zuführung (1) für das zu trocknende Feststoffmaterial zum Wirbel- schichttrockner (2) ,Solution infinitely controlled feed (1) for the solid material to be dried to the fluidized bed dryer (2),
ERSATZBLATT b) eine Einrichtung zum Eintragen (3) des Feststoff¬ materials in den Wirbelschichttrockner (2), die, bezogen auf die einzutragende Masse des Feststoff¬ materials, mindestens eine 1,5-fache Leistung hat und die im Falle des Eintragens von teilchenförmi- gem, wirbelfähigem oder aufgeschlämmtem Feststoff- material mindestens 25 % und bei Eintrag von klum- penförmigem, schwer oder nicht wirbelfähigem Fest¬ stoffmaterial mindestens 75 % der Oberfläche (12) eines Wirbelschichtbettes (6) annähernd gleich¬ mäßig mit dem eingetragenen Feststoffmaterial beaufschlagt,ERS A TZBLATT b) a device for introducing (3) the solid material into the fluidized bed dryer (2), which, based on the mass of the solid material to be introduced, has at least 1.5 times the output and which in the case of the entry of particulate at least 25% according to the whirlable or slurried solid material and, if lumpy, difficult or non-whirlable solid material is introduced, at least 75% of the surface (12) of a fluidized bed (6) is applied approximately uniformly to the solid material added,
c) einem Wirbelschichtbett (6), das einen Heizkör¬ per (7) mindestens 250 bis 1000 mm überdeckt,c) a fluidized bed (6) which covers a radiator (7) at least 250 to 1000 mm,
d) eine durch die vorgegebene Höhe des Wirbelschicht¬ bettes (6) in ihrer Leistung gesteuerte Austrags- vorrichtung (4) für getrocknetes Feststoffmate- rial,d) a discharge device (4), which is controlled in terms of its output by the predetermined height of the fluidized bed (6), for dried solid material,
e) eine mechanische Staubabscheidung (13) zur Senkung des Anteiles der Körnung kleiner 0,5 mm am mit dem Dampf des verdampfungsfähigen Materials über einen Austrag (8) ausgetragenen Staub des Feststoffmate¬ rial unter 10 Masse-%,e) a mechanical dust separator (13) for reducing the proportion of the grain size less than 0.5 mm in the dust of the solid matter material discharged with the vapor of the vaporizable material via a discharge (8) below 10% by mass,
f) eine Entstaubungsanlage (9) zur Senkung des Staub¬ anteiles im aus dem Wirbelschichttrockner (2) abgeführten Dampf unter 50 mg/kg Dampf,f) a dedusting system (9) for reducing the dust content in the steam discharged from the fluidized bed dryer (2) below 50 mg / kg steam,
g) eine Dampfrückführung (10) mit einem Verdich¬ ter (11), der den Druck des Dampfes soweit erhöht, daß durch die Vorrichtung mindestens die doppelte Menge an Dampf zirkuliert, die erforderlich ist für den Übergang des Feststoffes auf dem Wirbelbo-g) a steam return (10) with a compressor (11) which increases the pressure of the steam to such an extent that at least twice the amount of steam circulates through the device which is required for the transfer of the solid on the fluidized bed
ERSATZ LATT den (5) vom Festbett zum Wirbelschichtbett (6), undREPLACEMENT LATT den (5) from the fixed bed to the fluidized bed (6), and
h) ein indirekt gekühlter Kondensator (18), der durch Kondensation des verdampften Materials die gasför¬ migen Verunreinigungen aus dem Dampf separiert und über eine Absaugung (14) der Umwelt, einer Odorie¬ rung oder anderen Gasreinigung und das Kondensat über eine Pumpe (15) zum Teil dem Kondensator (18) zuführt, miteinander kombiniert werden.h) an indirectly cooled condenser (18), which separates the gaseous impurities from the steam by condensation of the evaporated material and via an extraction system (14) to the environment, odorization or other gas purification and the condensate via a pump (15 ) partially supplies the capacitor (18), can be combined with one another.
13. Vorrichtung nach Anspruch 12, dadurch gekennzeichnet, daß die Kombination nach Anspruch 12 mit einem ein- oder mehrstufigen Kompressor (16) komplettiert wird, der den Druck des nach der Entstaubungsanlage (9) vor¬ liegenden Dampfes soweit anhebt, daß es zu indirekten Beheizung des Wirbelschichtbettes (6) verwendet werden kann.13. The apparatus according to claim 12, characterized in that the combination according to claim 12 is completed with a one- or multi-stage compressor (16) which raises the pressure of the steam present after the dedusting system (9) to such an extent that it leads to indirect Heating the fluidized bed (6) can be used.
14. Vorrichtung nach Anspruch 12, dadurch gekennzeichnet, daß die Kombination nach Anspruch 12 mit einer Dampf- turbinenanlage (17), bestehend aus Entspannungsturbine, Generator zur Elektroenergieerzeugung und Kondensator ausgerüstet ist. Hierzu ein Blatt Zeichnung.14. The apparatus according to claim 12, characterized in that the combination according to claim 12 is equipped with a steam turbine system (17), consisting of expansion turbine, generator for generating electrical energy and a capacitor. A sheet of drawing.
ERSATZBLATT REPLACEMENT LEAF
EP90916213A 1990-09-18 1990-10-15 Process and device for drying solid materials in an indirectly heated fluidized bed Expired - Lifetime EP0549577B1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4029525 1990-09-18
DE4029525A DE4029525A1 (en) 1990-09-18 1990-09-18 METHOD AND DEVICE FOR DRYING SOLID MATERIALS IN AN INDIRECTLY HEATED FLUIDIZED BED
PCT/EP1990/001744 WO1992005393A1 (en) 1990-09-18 1990-10-15 Process and device for drying solid materials in an indirectly heated fluidized bed

Publications (2)

Publication Number Publication Date
EP0549577A1 true EP0549577A1 (en) 1993-07-07
EP0549577B1 EP0549577B1 (en) 1994-06-22

Family

ID=6414459

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90916213A Expired - Lifetime EP0549577B1 (en) 1990-09-18 1990-10-15 Process and device for drying solid materials in an indirectly heated fluidized bed

Country Status (8)

Country Link
US (1) US5373648A (en)
EP (1) EP0549577B1 (en)
AU (1) AU6618690A (en)
DE (1) DE4029525A1 (en)
DK (1) DK0549577T3 (en)
ES (1) ES2057598T3 (en)
RU (1) RU2075708C1 (en)
WO (1) WO1992005393A1 (en)

Families Citing this family (41)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4220953A1 (en) * 1992-06-26 1994-01-05 Metallgesellschaft Ag Process for drying water-containing solids in a fluidized bed
DE4344593C1 (en) * 1993-12-24 1995-02-16 Somos Gmbh Apparatus for drying bulk material
DE4401623A1 (en) * 1994-01-20 1995-07-27 Waldner Gmbh & Co Hermann Sewage sludge or slurry dryer
DE4404813C1 (en) * 1994-02-16 1995-02-23 Kraftanlagen Ag Process for fluidised-bed drying of sludge and fluidised-bed dryer for carrying out the process
DE19602290A1 (en) * 1996-01-23 1997-07-24 Loedige Maschbau Gmbh Geb Process for drying sewage sludge or sludge of similar consistency
WO1999064801A1 (en) * 1998-06-11 1999-12-16 Universal Dynamics, Inc. Method and apparatus for drying granular solids with venturi powered gas circulation
JP3825587B2 (en) * 1999-08-18 2006-09-27 新日本製鐵株式会社 Coal drying method and drying apparatus
AU2003253682A1 (en) * 2002-06-24 2004-01-06 The Procter And Gamble Company Food package
US7275644B2 (en) 2004-10-12 2007-10-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US8062410B2 (en) 2004-10-12 2011-11-22 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
US7987613B2 (en) 2004-10-12 2011-08-02 Great River Energy Control system for particulate material drying apparatus and process
US7730633B2 (en) * 2004-10-12 2010-06-08 Pesco Inc. Agricultural-product production with heat and moisture recovery and control
US8579999B2 (en) 2004-10-12 2013-11-12 Great River Energy Method of enhancing the quality of high-moisture materials using system heat sources
US8523963B2 (en) 2004-10-12 2013-09-03 Great River Energy Apparatus for heat treatment of particulate materials
US7540384B2 (en) 2004-10-12 2009-06-02 Great River Energy Apparatus and method of separating and concentrating organic and/or non-organic material
US20100038288A1 (en) * 2008-08-12 2010-02-18 MR&E, Ltd. Refining coal-derived liquid from coal gasification, coking, and other coal processing operations
CN102177406B (en) * 2008-08-12 2013-11-06 施维英生物泥公司 Closed loop drying system and method
EP2196756A1 (en) 2008-12-15 2010-06-16 Siemens Aktiengesellschaft Device for drying fuel
WO2010135744A1 (en) * 2009-05-22 2010-11-25 The University Of Wyoming Research Corporation Efficient low rank coal gasification, combustion, and processing systems and methods
TR201112915T1 (en) * 2009-06-04 2012-09-21 Shan Dong Tian Li Drying Equipment Co. Ltd. Very effective brown coal pre-drying system using superheated steam and related process.
US8470134B2 (en) * 2009-07-14 2013-06-25 C2O Technologies, Llc Process for treating coal by removing volatile components
WO2011008832A2 (en) * 2009-07-14 2011-01-20 C20 Technologies, Llc Process for treating agglomerating or bituminous coal by removing volatile components
US8366882B2 (en) * 2009-07-14 2013-02-05 C20 Technologies, Llc Process for treating agglomerating coal by removing volatile components
FR2953005B1 (en) * 2009-11-23 2011-12-09 Degremont PROCESS AND INSTALLATION FOR DRYING PASTE MATERIALS, IN PARTICULAR SLUDGE OF PURIFICATION STATIONS
CN101922859B (en) * 2010-09-13 2011-09-28 山东天力干燥股份有限公司 Grading crushing dryer for upgrading lignite
CN103124782B (en) 2010-09-16 2015-08-26 C20技术发展公司 By the Coal dressing that the biomass of adding and volatile matter control
CN102183122A (en) * 2011-03-01 2011-09-14 中国中轻国际工程有限公司 Drying dehydration steam-recycle process and device for solid containing water
US8968520B2 (en) 2011-06-03 2015-03-03 National Institute Of Clean And Low-Carbon Energy (Nice) Coal processing to upgrade low rank coal having low oil content
US9005322B2 (en) 2011-07-12 2015-04-14 National Institute Of Clean And Low-Carbon Energy (Nice) Upgrading coal and other carbonaceous fuels using a lean fuel gas stream from a pyrolysis step
US9074138B2 (en) 2011-09-13 2015-07-07 C2O Technologies, Llc Process for treating coal using multiple dual zone steps
KR101216827B1 (en) * 2011-12-15 2012-12-28 한국서부발전 주식회사 System for drying coal using super-heated steam
JP5851883B2 (en) * 2012-02-28 2016-02-03 三菱日立パワーシステムズ株式会社 Non-condensable gas exhaust system and gasification combined power generation facility
WO2014110221A1 (en) 2013-01-09 2014-07-17 C2O Technologies, Llc Process for treating coal to improve recovery of condensable coal derived liquids
DE102013220501A1 (en) 2013-10-11 2015-04-16 Technische Universität Bergakademie Freiberg Process and apparatus for coal pyrolysis
DE102013221075A1 (en) 2013-10-17 2015-04-23 Technische Universität Bergakademie Freiberg Process for drying coal and pyrolysis
CN105021020A (en) * 2014-08-26 2015-11-04 呼伦贝尔东能化工有限公司 Dust removal and collection method for lignite drying system
US9327320B1 (en) 2015-01-29 2016-05-03 Green Search, LLC Apparatus and method for coal dedusting
AT517644B1 (en) * 2015-08-18 2018-08-15 Gaston Ing Glock Method and device for drying wood chips
US11215360B2 (en) * 2015-08-18 2022-01-04 Glock Ökoenergie Gmbh Method and device for drying wood chips
CN105222528B (en) * 2015-10-23 2017-06-06 天华化工机械及自动化研究设计院有限公司 A kind of fluidized bed coal is dried and water recovery method
CN106862077B (en) * 2017-01-21 2018-10-19 中国矿业大学 A kind of coupled system and method for wetted coal fines sorting and drying

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH544918A (en) * 1971-11-10 1973-11-30 Ciba Geigy Ag Drying process
US3790334A (en) * 1972-05-22 1974-02-05 Fuller Co Manufacture of lightweight aggregate
US3800427A (en) * 1973-01-18 1974-04-02 Waagner Biro American Method for drying coal
AU4296978A (en) * 1978-02-10 1979-08-16 Monash University Drying particulate materials
DD137005A1 (en) * 1978-06-16 1979-08-08 Horst Bergmann DEVICE FOR REGULATING THE DRYING PROCESS IN SWIVEL LAYER DRYERS
US4304049A (en) * 1979-05-28 1981-12-08 Escher Wyss Limited Process for thermal treatment, especially drying
EP0132493B1 (en) * 1980-12-16 1988-06-15 Cosworth Research And Development Limited Apparatus for and method of reclaiming used foundry sand
DD235387A3 (en) * 1983-09-26 1986-05-07 Guenter Voels METHOD FOR CONDITIONING CALCIUM SLUDGE
AT386071B (en) * 1985-05-22 1988-06-27 Waagner Biro Ag DRYING SYSTEM FOR GRAINY SOLIDS
AT390018B (en) * 1988-05-05 1990-03-12 Waagner Biro Ag METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES
DD282509A5 (en) * 1989-04-18 1990-09-12 Orgreb Inst Kraftwerke METHOD AND DEVICE FOR DRYING SOLIDS MATERIALS IN AN INDIRECTLY HEATED SWITCH BED

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9205393A1 *

Also Published As

Publication number Publication date
WO1992005393A1 (en) 1992-04-02
DK0549577T3 (en) 1994-11-14
EP0549577B1 (en) 1994-06-22
ES2057598T3 (en) 1994-10-16
DE4029525A1 (en) 1992-03-19
US5373648A (en) 1994-12-20
AU6618690A (en) 1992-04-15
RU2075708C1 (en) 1997-03-20

Similar Documents

Publication Publication Date Title
EP0549577A1 (en) Process and device for drying solid materials in an indirectly heated fluidized bed.
DE2901722C2 (en)
DE2901723C2 (en) Method and apparatus for drying a solid material
DE69912809T2 (en) WASTE COMBUSTION WITH CLOSED CIRCUIT
DE2609330B2 (en) Process for converting solid waste materials initially containing water into economically usable or environmentally harmless products and device for carrying out the process
US2102427A (en) Method of treating waste wet organic material
DE1943776A1 (en) Process and system for the destruction of solid waste
EP0465479B1 (en) A method of reprocessing sewage sludge
DE3613308A1 (en) METHOD AND DEVICE FOR FLUIDIZED STEAM DRYING OF LOW-QUALITY COALS
DE3613305A1 (en) METHOD AND DEVICE FOR FLUIDIZED STEAM DRYING OF LOW-QUALITY COALS BY WET CLEANING
EP0393179A1 (en) Process for generating electrical energy and/or drying and process heat.
DE3404915A1 (en) METHOD FOR BURNING WATER-BASED FUELS AND ARRANGEMENT FOR IMPLEMENTING THE METHOD
DE3417620A1 (en) Method and device for generating heat energy, which can be converted into mechanical energy, from the combustion of wet waste
DE3943366C2 (en) Method and device for drying solid materials in an indirectly heated fluidized bed
DE112012002496T5 (en) A method of drying material and dryer for use in the process
DD142085A5 (en) METHOD AND DEVICE FOR DRYING A SOLID MATERIAL
EP0031558A1 (en) Refuse incineration plant
DD262559A3 (en) METHOD AND DEVICE FOR DRYING AND COMBUSTION OF COMBUSTION AND WASTE MATERIALS, PARTICULARLY HUMIDIFIED RAW BROWN COAL
DE3103417A1 (en) Process and apparatus for the oxidation of solid substances and aqueous sludges
DE3103399A1 (en) Apparatus for producing and purifying gases and vapours
EP0080549A2 (en) Process for the production of pyrolysis gas from combustible materials, and installation for carrying out the process
DE19906061A1 (en) Apparatus for pollutant-deficient combustion of clarified sludge comprises a pulsation reactor, a hot gas cyclone, a high temperature heat exchanger and further heat exchangers
DD277735A1 (en) METHOD FOR GENERATING ELECTRICAL ENERGY AND / OR HEATING AND PROCESSING WASTE
DD274267A1 (en) POWER PLANT FOR USING BALLASTIC FOSSIL FUELS
DD239419A1 (en) INTEGRATED PYROLYSIS COMBUSTION PROCESS

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: 19930306

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DK ES FR IT SE

17Q First examination report despatched

Effective date: 19931112

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: UET UMWELT- UND ENERGIETECHNIK FREIBERG GMBH

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DK ES FR IT SE

ITF It: translation for a ep patent filed
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2057598

Country of ref document: ES

Kind code of ref document: T3

ET Fr: translation filed
REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

EAL Se: european patent in force in sweden

Ref document number: 90916213.3

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

Ref country code: FR

Payment date: 20031021

Year of fee payment: 14

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

Ref country code: SE

Payment date: 20031027

Year of fee payment: 14

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

Ref country code: ES

Payment date: 20031029

Year of fee payment: 14

Ref country code: DK

Payment date: 20031029

Year of fee payment: 14

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

Ref country code: SE

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

Effective date: 20041016

Ref country code: ES

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

Effective date: 20041016

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

Ref country code: DK

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

Effective date: 20041101

EUG Se: european patent has lapsed
REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

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

Ref country code: FR

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

Effective date: 20050630

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

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

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20051015

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20041016