EP0549577B1 - Verfahren und vorrichtung zum trocknen von feststoffmaterialien in einem indirekt beheizten wirbelschichtbett - Google Patents

Verfahren und vorrichtung zum trocknen von feststoffmaterialien in einem indirekt beheizten wirbelschichtbett Download PDF

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Publication number
EP0549577B1
EP0549577B1 EP90916213A EP90916213A EP0549577B1 EP 0549577 B1 EP0549577 B1 EP 0549577B1 EP 90916213 A EP90916213 A EP 90916213A EP 90916213 A EP90916213 A EP 90916213A EP 0549577 B1 EP0549577 B1 EP 0549577B1
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EP
European Patent Office
Prior art keywords
fluidised bed
solid material
vapour
fluidized bed
solid
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.)
Expired - Lifetime
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EP90916213A
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German (de)
English (en)
French (fr)
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EP0549577A1 (de
Inventor
Bodo Wolf
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UET UMWELT- UND ENERGIETECHNIK FREIBERG GMBH
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UET Umwelt- und Energietechnik Freiberg GmbH
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    • 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 an apparatus for drying solid materials, e.g. Lignite, peat, sand, filter cakes from mechanical separation processes and sludges containing less than 98% by mass of an evaporable material, e.g. Contain 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 evaporable 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 can be used for cleaning, cooling, material use and / or heat energy recovery and is suitable for use in industry, construction, agriculture and municipal disposal.
  • an evaporable material e.g. Contain water
  • Drying processes especially those that separate water as an evaporable component from solid materials, are of great economic and social importance for industrial production, construction, energy conversion and the disposal of municipalities and businesses. Drying is sometimes as self-evident or integrated into the process as is the case with the combustion of water-based fuels, e.g. lignite and sludge, that the environmental pollution caused by increased energy requirements and increased emissions is considered natural.
  • water-based fuels e.g. lignite and sludge
  • plate and tube dryers ie contact dryers
  • ie 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 Basic Industry, Leipzig, 1984, 1st edition, have been described in detail.
  • turbine extraction steam 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 "combined heat and power" used and a lowering of the fuel requirement attributable to drying.
  • the comparable sum of the flue gas emissions occurring during the individual upgrading and usage sections could therefore fall to almost 1.3 times the minimum required by natural law.
  • 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 before it is burned in a steam boiler in a fluidized bed dryer which is heated directly with steam.
  • turbine extraction or counterpressure steam should be used and the principle of "combined heat and power" should be used.
  • DD-PS 67770 assumes that any suitable fluidizing medium, including steam, can be used to fluidize the lignite above the fluidized bed in the fluidized bed dryer.
  • US Pat. No. 3,800,427 describes an indirectly heated fluidized-bed drying process in which the lignite is whirled up with steam, so that the drying takes place in a steam 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-A-29 01 723 extends the use of a indirectly heated with steam and fluidized fluidized bed with steam generally to dry solid materials containing less than 95% by mass of an evaporable material.
  • the vaporizable material can also be other materials besides water, 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 indirect heating of the fluidized bed.
  • DE-A-29 01 723 restricts the permissible temperature of the fluidized bed in relation to US Pat. No. 38 00 427 and specifies that this is substantially below the decomposition temperature of the solid material, so that the vapor discharged from the fluidized bed dryer is essentially without contamination by other gaseous substances from the evaporable material.
  • the device for performing the method according to DE-PS 29 01 723 consists of a fluidized bed dryer with a feed for the solid material. Radiators are provided within the fluidized bed dryer for indirect heating of the fluidized bed formed in the dryer. The discharge for the dried solid material lies in the lower area, the evaporation material is removed at the upper end of the dryer. At least the fluidized bed dryer and a first downstream separating device are located in a common, heat-insulated housing. Additional heating elements which can be heated with steam can be present in the casing forming the thermal insulation, and the separation of particulate matter takes place via cyclones.
  • 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 feasible and reworkable principles of drying technology, a method and the device required for implementing the method for drying solid materials in a fluidized bed dryer, the indirectly heated fluidized bed of which is preferably formed by the dried solid material itself and by the vaporizable material is whirled up in vapor form is to create, which achieve the aim of the invention in practical operation.
  • the decisive factor for the solution of the task is the knowledge 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 one that characterizes the solid material, i.e. substance-specific, in an isobaric process sequence Boiling curve 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 evaporable material in the solid material discharged from the fluidized bed by supplying solid material with a higher mass fraction of evaporable material to and removing dried solid material from the fluidized bed in such a way that it adjusts the boiling curve of the material to be evaporated corresponds to the fluidized bed removed from the fluidized bed, so that the vapor discharged from the fluidized bed dryer also 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, but only the components of the solid components of the solid material which are volatile below this boiling temperature or the Contains sludge.
  • 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 of the evaporable material contained in the steam, other gaseous impurities and decomposition products of the solid fraction, which are not condensable at ambient temperature and are 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 cleaning.
  • 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 the production of 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 to dry solid material into a form corresponding to the process is to convert it with condensate of the evaporable material into a pumpable and sprayable sludge form. If it is necessary to maintain the bulk of the solid material to be dried, then the process can be successfully implemented if the fluidized bed is not from the solid material itself, but from a small-grain solid material, which is 1.2 to 5.0 compared to the material to be dried times the density is marked, is formed.
  • bed material is discharged from the fluidized bed with the dried solid material. This requires separating the bed material from the dried, coarse solid material and returning the bed material to the fluidized bed.
  • the decisive factor 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.
  • the heating steam pressure of 0.2 to 4.0 MPa is required, which results in steam temperatures of 125 to 225 ° C when using steam as the heating medium, with the heating steam in a slightly overheated state Has. 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 requires, according to the invention, the condensation of the evaporated portion of the solid material.
  • the fluid bed dryer works under steam pressures that correspond to the pressure of the surrounding atmosphere, the substance-dependent condensation temperature determines the temperature level of the heat energy that can be recovered. 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 tasks of heating heating and preheating in industrial processes. If there is no need for thermal energy at this temperature level, the steam can be expanded by handing in technical work after appropriate cleaning of dust to such an extent that condensation at ambient temperature is still possible.
  • Another possibility is to increase the steam from the fluidized bed dryer, also after appropriate cleaning of dust, before its condensation by compression to such an extent that the heat of condensation arises at a temperature level which is sufficient to fulfill the intended heat transfer, e.g. for heating the fluidized bed of the process according to the invention is sufficient.
  • a feeder controlled by the fluidized bed temperature for the solid material to be dried is provided to the fluidized bed dryer with a device for introducing the solid material into the fluidized bed dryer which, based on the mass of solid material to be introduced, has at least 1.5 times the output and has at least 25% in the case of the introduction of particulate, swirlable or slurried solid material and in the case of the introduction of lumpy, heavy or not vortex-capable solid material is applied to at least 75% of the surface of the fluidized bed approximately uniformly with the solid material introduced.
  • 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 by the predetermined height of the fluidized bed in its output and a mechanical dust separation to reduce the proportion of the grain size less than 0.5 mm of dust of the solid material discharged with the vapor of the evaporable material via the discharge below 10% by mass.
  • the device according to the invention includes a steam recirculation 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 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 steam by condensation of the material evaporated in the fluidized bed and, if necessary, supplies the condenser and further processing and use via a pump to the environment or deodorization and / or other gas cleaning and the condensate.
  • the device according to the invention can be completed with a single and multi-stage compressor which reduces the pressure of the vapor to the extent that the condensation of the steam can be carried out at the temperature level required to fulfill the heat supply task, for example for indirect heating of the fluidized bed.
  • the vapor of the vaporizable material from the fluidized bed dryer can be fed to a steam turbine system after leaving the dedusting system, in which it is reduced in pressure by submitting technical work so that condensation at ambient temperature, eg 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 the 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 weight is removed from the fluidized bed dryer 2 and in the fluidized bed dryer 249.152 kg of 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 water in the example the vaporizable material, should contain 20 m3 of dissolved gaseous impurities, in particular carbon dioxide, so that the steam generated from drying in one hour from coal water contains a total of 220 m3 of gaseous impurities which correspond to the saturation temperature loaded with water vapor in the condenser 18 separated and released into the environment.
  • a heating surface density of 100 m2 of fluidized bed 5 is to be achieved, that is, the fluidized bed dryer 2 has a 32 m2 large fluidized bed 5, which is a length for the width of the fluidized bed 5 of 4 m Vortex floor 5 of 8 m results. 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 m3 of water vapor, which corresponds to 53.8 t / h, must be recirculated.
  • the heat 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 th in the condenser 18 at a temperature level of up to 95 ° C., that is 78% of the thermal energy expended, making this objective Invention is achieved.
  • 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 height of the fluidized bed must be regulated by the regulated discharge of dried coal due to the heating element 7 specified 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 maximum 3250 mm will.

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
EP90916213A 1990-09-18 1990-10-15 Verfahren und vorrichtung zum trocknen von feststoffmaterialien in einem indirekt beheizten wirbelschichtbett Expired - Lifetime EP0549577B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4029525 1990-09-18
DE4029525A DE4029525A1 (de) 1990-09-18 1990-09-18 Verfahren und vorrichtung zum trocknen von feststoffmaterialien in einem indirekt beheizten wirbelschichtbett
PCT/EP1990/001744 WO1992005393A1 (de) 1990-09-18 1990-10-15 Verfahren und vorrichtung zum trocknen von feststoffmaterialien in einem indirekt beheizten wirbelschichtbett

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EP0549577A1 EP0549577A1 (de) 1993-07-07
EP0549577B1 true EP0549577B1 (de) 1994-06-22

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

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EP0549577A1 (de) 1993-07-07
ES2057598T3 (es) 1994-10-16
AU6618690A (en) 1992-04-15
RU2075708C1 (ru) 1997-03-20
WO1992005393A1 (de) 1992-04-02
DK0549577T3 (da) 1994-11-14
DE4029525A1 (de) 1992-03-19
US5373648A (en) 1994-12-20

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