EP0379657A1 - Procédé de séchage de boues - Google Patents

Procédé de séchage de boues Download PDF

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Publication number
EP0379657A1
EP0379657A1 EP89120565A EP89120565A EP0379657A1 EP 0379657 A1 EP0379657 A1 EP 0379657A1 EP 89120565 A EP89120565 A EP 89120565A EP 89120565 A EP89120565 A EP 89120565A EP 0379657 A1 EP0379657 A1 EP 0379657A1
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EP
European Patent Office
Prior art keywords
sludge
layer
dryer
gas stream
sand
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
EP89120565A
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German (de)
English (en)
Other versions
EP0379657B1 (fr
Inventor
Karl Dipl.-Ing. Keller
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.)
Sulzer Escher Wyss GmbH
Original Assignee
Sulzer Escher Wyss GmbH
Escher Wyss GmbH
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
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Application filed by Sulzer Escher Wyss GmbH, Escher Wyss GmbH filed Critical Sulzer Escher Wyss GmbH
Priority to AT89120565T priority Critical patent/ATE67299T1/de
Publication of EP0379657A1 publication Critical patent/EP0379657A1/fr
Application granted granted Critical
Publication of EP0379657B1 publication Critical patent/EP0379657B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F26B21/02—Circulating air or gases in closed cycles, e.g. wholly within the drying enclosure
    • F26B21/04—Circulating air or gases in closed cycles, e.g. wholly within the drying enclosure partly outside the drying enclosure
    • 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
    • F26B3/088—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 using inert thermally-stabilised particles

Definitions

  • the invention relates to a method for drying a sludge of the type specified in the preamble of claim 1.
  • All suspensions, sludges, pastes and filter cakes from various dewatering machines can be used for drying.
  • This also includes sewage sludge from municipal or industrial wastewater that comes from sewage treatment plants that are fed with it.
  • sludges are mechanically dewatered. Their further processing, recycling or disposal requires thermal drying. Depending on the degree of dewatering, the pasty sludges contain 40 to 60% water, which affects the handling and the processes for recycling or disposal of the sludge. Thermal drying improves or extends the possibilities for recycling these sludges and / or reduces the amount to be disposed of.
  • a known method uses a direct drum dryer. Depending on the consistency and after pretreatment, the sludge is placed in a rotating drum inclined towards the discharge and migrates to the discharge end by constant rolling in the rotating drum. At the same time, hot air or hot flue gas flows through the drum in countercurrent or cocurrent and absorbs the moisture of the sludge.
  • the system is mechanically and energetically complex, and the moist and polluted exhaust air from the drum dryer requires complex cleaning to limit emissions.
  • Hot air or hot flue gases flow through a layer of sand from the bottom up, which is a Forces fluidization of this sand filling.
  • An inflow floor ensures an even distribution of the inflowing hot gases.
  • Several pumps push the sludge through nozzles directly into the fluidized sand layer. The nozzles are located just above the inflow floor, i.e. in the lower quarter of the sand layer. The sludge releases its moisture to the hot gas flowing through, which has to be cleaned after it has left the dryer.
  • Indirect contact dryers are also known.
  • the sludge is heated indirectly via heating surfaces.
  • these heating surfaces take the form of disks, paddles, rollers, etc.
  • the steam or oil-heated heating surfaces heat the sludge until its moisture evaporates, a ventilator sucks off the vapors and presses them to condense.
  • the sludge is either applied thinly to the heating surfaces and scraped off again, or the heating surfaces are moved or stirred in the product to be dried.
  • the applicant offers a method with an indirect fluidized bed dryer. Overheated vapors flow through a sludge granulate in a circuit from bottom to top in a fluidized bed and thereby fluidize it. An inflow floor with nozzles distributes the gas evenly over the entire dryer surface and ensures balanced fluidization of the granules.
  • Heating surfaces for example heat exchangers, are arranged in this fluidized layer and indirectly transfer the energy required for drying to the granulate.
  • the heating surfaces have different shapes, such as smooth tubes, finned tubes, plates, etc., which are heated with steam or other heat carriers.
  • a granulator creates moist, stable granules by mixing dewatered sludge and part of the already dried sludge.
  • This moist granulate is introduced into the fluidized bed, where its moisture is absorbed by the flowing, overheated vapors.
  • the dried granulate leaves the fluidized bed dryer via an overflow weir or a discharge device. Part of the dried granulate goes back to the granulator, where dewatered sludge is added to the wet granulate.
  • the vapors emerging from the fluidized bed dryer also take fine-grained product particles and dust, which are separated in a cyclone or filter and fed into the granulator. The amount of water evaporated during drying is drawn off as vapors from the circulatory system and condensed or treated thermally.
  • the invention was based on the object of proposing a method of the initially specified type which is more economical than the previously known.
  • a pretreatment of the sludge before drying should not be necessary.
  • the discharge of the dry material from the dryer should be simplified.
  • the energy consumption of the process is to be reduced.
  • the equipment used should be simpler and cheaper, and at the same time largely trouble-free and low-maintenance.
  • the process should be continuously executable.
  • the product should have a high dry matter content and should be easy to manipulate. Environmental pollution should be largely avoided. The environmental impact should be as low as possible.
  • the resulting sludge 1 is a suspension containing organic substances, which is still pumpable with about 40% water and is kept in stock in a silo 12.
  • the drive motor 14 of which can be speed-regulated with a control device 15 the sludge is pumped into a fluidized bed dryer 2 through a line 16, in which a heated sand layer 3 fluidized by means of a gas stream is built up during operation becomes.
  • the sand layer 3 fluidized with a gas stream is heated indirectly by means of stationary heat exchange bodies 5 immersed in the sand layer 3.
  • the pumpable sludge 1 to be dried is introduced under pressure from the pump 13 into the dryer 2 from above onto the sand layer 3 in countercurrent to the fluidizing gas stream.
  • the feed points are provided in the uppermost area of the dryer 2.
  • the fluidized sand entrains the sludge immediately after it emerges from the mouthpieces of a distribution device. During this process, the sludge coagulates and sludge bulbs form which, owing to the fluidization, are distributed in the sand layer 3 and move in floating manner in this.
  • the hot sand and the hot fluidizing gas gradually release the thermal energy to the moist mud tubers, which leads to a steady heating, with water evaporation of the mud tubers, successively layer by layer from the surface to the core.
  • the water vapor is taken up by the gas stream and discharged from the dryer 2 with the exhaust gas stream 6.
  • the fluidized sand constantly rubs against the already dried-up layer of the mud tubers and grinds off the dry mud, its dry substance, as fine dust.
  • This pulverization of the sludge takes place at each sludge tuber until it has completely dried and been ground down to the respective core, until the remaining sludge dry matter has gradually been crushed and has been pulverized in this way.
  • the rising fluidizing gas stream also entrains the pulverized sludge dry matter and the product dust in addition to the water vapor and thus continuously carries the product 4 with the exhaust gas stream 6 out of the dryer 2 as a function of the gas stream speed.
  • the pulverized dry substance 4, ie the sludge dry matter, is continuously separated as a product from the exhaust gas stream 6 in a separation stage, the cyclone 7.
  • a fan 17, downstream of the cyclone 7, sucks off the exhaust gas stream 6 and thus prevents an increase in pressure due to water evaporation and other gas development during the drying process in the dryer 2.
  • the sand in the sand layer 3 and the fluidizing gas stream are heated by means of smooth heat exchange tubes 5, which are arranged horizontally in the provided area of the sand layer 3 in the fluidized state and through which a heat-carrying medium flows.
  • flue gases 8 are the heat-carrying medium, which are generated in a combustion chamber 9 when fossil fuels 10 are burned.
  • necessary air is led through a line 18.
  • At least some of the flue gases are sucked off by a fan 19 after flowing through the heat exchange tubes 5 and led into the combustion chamber 9 with recovery of their residual heat and thus recirculated.
  • the excess part of the flue gases is removed from the circuit via a line 20 and discharged through a silencer 21.
  • the exhaust gas stream 6, from which the product 4 has been separated, is continuously recirculated to fluidize the sand layer 3, the fluidized bed in the dryer 2.
  • the gas still contains all of the water vapor newly generated in the dryer and the other gases developed there. This additional volume of gas must be withdrawn from the gas cycle system in order to keep the pressure in the gas cycle system constant.
  • the gas volume reduced to the amount of gas required for the fluidization of the layer 3 in the fluidized bed dryer 2 is passed through a fan 22, distribution box 37 and inflow base 38 of the dryer 2, which closes the gas circuit.
  • the excess gas quantity is reduced by condensing the condensable excess gas, primarily the excess water vapor in a condenser 11, into which the entire exhaust gas flow is led through a line 23.
  • the condensation takes place by spraying the gas with cooling water, for which a line 24 is provided.
  • the water with the condensate is recirculated via a pump 25 and possibly a cooler 26, an excess being drawn off via a line 27. If there is still an excess volume after the condenser 11 in the circulatory system, a corresponding one becomes Gas amount withdrawn from the circulatory system by opening a valve 28 via a line 29. Water vapor and the gases released during drying remain in the circuit.
  • the gas circuit used for fluidization becomes ever poorer in free oxygen, so that finally the process in and after the dryer 2 takes place in a non-reactive atmosphere, thereby eliminating the risk of burning or explosion.
  • the product dust present in the cyclone 7 has about 90% TS.
  • the pulverized sludge dry mass 4 obtained after the discharge apparatus 30 is fed to a mixer 31, where part of the sludge 1 from the silo 12 is added to the product dust via a speed-controllable pump 32 and a line 33, whereby a desired final moisture content of the product is set becomes.
  • a line 34 leads from the mixer 31 to the cyclone 7, through which the gases produced in the mixer 31 are drawn off.
  • the mixer 31 is provided with a granulator, where the product having the desired moisture content is processed into granules.
  • the end product processed in this way is loaded by means of a transport device 35.
  • a line 36 is also connected to this and, if necessary, serves to empty the dryer 2.
  • the process is suitable for drying a wide variety of suspensions, slurries, pastes and filter cakes from a wide variety of dewatering devices.
  • the process for drying municipal and / or industrial sewage sludge was described here.
  • the sludges no longer have to be structured or granulated before being introduced into the fluidized bed. Since the sand grinds the dried sludge into dust and the dust is discharged with the exhaust gas stream, no complicated discharge mechanism from the dryer is necessary. The recirculation of product for granulation can also be omitted.
  • the fluid bed dryer works in a chemically non-reactive atmosphere, which consists of slightly overheated vapors and the gases contained in the sludge without free oxygen.
  • the sand fluidized in the dryer is an absolutely inert material in the drying process, which does not react chemically with the sludge, moisture or the recycle gas. This prevents inflammation due to overheating in the dryer.
  • the energy for drying the material is indirectly transferred to the material or to the fluidized sand.
  • the heating medium does not come into direct contact with the material or the sand.
  • the evaporated moisture accumulates as water vapor and can be disposed of as such by simple condensation using the waste heat.
  • the horizontal smooth-tube heat exchangers in the fluidized layer carry out an extremely intensive energy exchange with a high specific heat output.
  • An optimal grain distribution of the sand which is selected according to the material to be dried, allows a relatively lower gas velocity and higher heat output than in a fluid bed dryer with a product granulate layer. This reduces the electrical energy required to drive the fans.
  • the fluidized sand layer constantly cleans the immersed heating surfaces during operation, so that their loss of performance due to contamination is excluded.
  • the horizontal smooth tube heating surfaces are stationary and therefore static heat exchangers. They can not only be heated with steam or liquid heat carriers, but also allow heating with hot gases such as air or flue gases.
  • the hot flue gases can be generated as waste heat or from a combustion chamber with direct firing.
  • the dryer Due to the inert sand layer, the dryer remains absolutely insensitive to temperature fluctuations or overheating.
  • the layer of sand also allows rapid heating and enables the system to be started up immediately at nominal output. When the system is switched off, forced reheating for the inert sand filling is absolutely harmless.
  • the dust-like dust product can be adjusted to a desired moisture content of 50% to 90% DM according to a further use.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Drying Of Solid Materials (AREA)
  • Treatment Of Sludge (AREA)
  • Crystals, And After-Treatments Of Crystals (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Current-Collector Devices For Electrically Propelled Vehicles (AREA)
  • Variable-Direction Aerials And Aerial Arrays (AREA)
  • Burglar Alarm Systems (AREA)
EP89120565A 1989-01-27 1989-11-07 Procédé de séchage de boues Expired - Lifetime EP0379657B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT89120565T ATE67299T1 (de) 1989-01-27 1989-11-07 Verfahren zur trocknung eines schlammes.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3902446A DE3902446C1 (fr) 1989-01-27 1989-01-27
DE3902446 1989-01-27

Publications (2)

Publication Number Publication Date
EP0379657A1 true EP0379657A1 (fr) 1990-08-01
EP0379657B1 EP0379657B1 (fr) 1991-09-11

Family

ID=6372936

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89120565A Expired - Lifetime EP0379657B1 (fr) 1989-01-27 1989-11-07 Procédé de séchage de boues

Country Status (10)

Country Link
US (1) US4970803A (fr)
EP (1) EP0379657B1 (fr)
JP (1) JPH02237700A (fr)
AT (1) ATE67299T1 (fr)
CA (1) CA2006507C (fr)
DE (1) DE3902446C1 (fr)
DK (1) DK21590A (fr)
ES (1) ES2024707B3 (fr)
FI (1) FI895755A0 (fr)
NO (1) NO894789L (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4028397C1 (fr) * 1990-09-07 1992-02-27 Deutsche Babcock Anlagen Ag, 4200 Oberhausen, De
EP0537637A1 (fr) * 1991-10-14 1993-04-21 Tsukishima Kikai Kabushiki Kaisha Système de séchage de boue humide
WO2008122137A1 (fr) * 2007-04-04 2008-10-16 Markus Lehmann Procédé pour sécher un matériau humide

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EP0393179B1 (fr) * 1988-10-18 1992-07-22 Saarberg-Interplan, Gesellschaft für Rohstoff-, Energie- und Ingenieurtechnik mbH Procede pour produire de l'energie electrique et/ou de la chaleur de chauffage et de la chaleur industrielle
DE4019242A1 (de) * 1990-06-15 1991-12-19 Petz Michael Dipl Ing Verfahren zur trocknung durch aenderung der beladungskapazitaet von luft o. dgl. (peflow-verfahren)
US5361708A (en) * 1993-02-09 1994-11-08 Barnes Alva D Apparatus and method for pasteurizing and drying sludge
DE19512563C2 (de) * 1995-04-04 1997-05-28 Deutag Ag Verfahren zur Verwertung von Schlämmen und wasserhaltigen Rückständen mit hohem Anteil organischer Substanzen
DE19522164A1 (de) * 1995-06-19 1997-01-02 Sep Tech Studien Verfahren und Vorrichtung zur kontinuierlichen Trocknung von Protein enthaltendem Schlamm
AT406671B (de) * 1996-11-22 2000-07-25 Andritz Patentverwaltung Verfahren zur trocknung von schlamm, insbesondere klärschlamm
AT406672B (de) * 1998-02-26 2000-07-25 Andritz Patentverwaltung Verfahren und anlage zur mechanischen und thermischen entwässerung von schlämmen
AU3338101A (en) * 2000-04-09 2001-10-11 Maschinenfabrik J. Dieffenbacher Gmbh & Co. Method and plant to reduce the water contents bound in the capillaries of fibrous cells
US6883444B2 (en) * 2001-04-23 2005-04-26 N-Viro International Corporation Processes and systems for using biomineral by-products as a fuel and for NOx removal at coal burning power plants
US6405664B1 (en) 2001-04-23 2002-06-18 N-Viro International Corporation Processes and systems for using biomineral by-products as a fuel and for NOx removal at coal burning power plants
US6752849B2 (en) 2001-08-08 2004-06-22 N-Viro International Corporation Method for disinfecting and stabilizing organic wastes with mineral by-products
US6752848B2 (en) 2001-08-08 2004-06-22 N-Viro International Corporation Method for disinfecting and stabilizing organic wastes with mineral by-products
ITRM20010625A1 (it) * 2001-10-19 2003-04-21 Francis Bacon S R L Processo per essiccare morchie.
US6666154B2 (en) * 2002-04-12 2003-12-23 N-Viro International Corporation Methods for controlling ignitability of organic waste with mineral by-products
DE10323774A1 (de) * 2003-05-26 2004-12-16 Khd Humboldt Wedag Ag Verfahren und Anlage zur thermischen Trocknung eines nass vermahlenen Zementrohmehls
US20060243648A1 (en) * 2005-04-27 2006-11-02 Shain Martin J Systems and Methods for Utilization of Waste Heat for Sludge Treatment and Energy Generation
US7513061B2 (en) * 2006-05-26 2009-04-07 Dai-Ichi High Frequency Co., Ltd. Sludge dehydrating processor for converting sludge including organic substance into resources of low water content
US7669348B2 (en) * 2006-10-10 2010-03-02 Rdp Company Apparatus, method and system for treating sewage sludge
AT504996B1 (de) * 2007-03-02 2009-03-15 Andritz Tech & Asset Man Gmbh Verfahren und vorrichtung zur trocknung von kristallinen carbonsäuren
US7637031B2 (en) * 2007-06-26 2009-12-29 Gm Global Technology Operations, Inc. Evaporator core drying system
JP4979538B2 (ja) * 2007-10-16 2012-07-18 株式会社神戸製鋼所 間接加熱乾燥装置、被乾燥物の間接加熱乾燥方法、ならびに固形燃料の製造方法および製造装置
IL204790A (en) * 2010-03-28 2014-07-31 Airgreen Ltd A method for processing and drying waste in a continuous circular process
CN102167488B (zh) * 2011-01-21 2012-11-21 上海伏波环保设备有限公司 非接触式烟气余热污泥干化系统
DE102011087264B4 (de) 2011-11-29 2023-01-19 Zf Friedrichshafen Ag Druckregelventilvorrichtung
JP6271274B2 (ja) * 2014-02-04 2018-01-31 株式会社大川原製作所 汚泥乾燥機における乾燥汚泥水分調整機構
CN112919772B (zh) * 2021-02-01 2022-10-21 武汉中科固废资源产业技术研究院有限公司 污泥热改性干化系统

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FR2458037A1 (fr) * 1979-05-28 1980-12-26 Escher Wyss Sa Procede de traitement thermique, destine plus particulierement au sechage et a la calcination
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FR2466439A1 (fr) * 1979-10-04 1981-04-10 Von Roll Ag Procede de sechage de boues, notamment de boues de stations d'epuration communales
GB2074299A (en) * 1980-03-17 1981-10-28 Salem Corp Method and Apparatus for Heating Particulate Material
FR2496085A1 (fr) * 1980-12-13 1982-06-18 Bergwerksverband Gmbh Procede et dispositif pour le sechage et la combustion des boues
WO1987004780A1 (fr) * 1986-01-31 1987-08-13 Valtion Teknillinen Tutkimuskeskus Procede de sechage d'un materiau pulverulent, granulaire ou en forme de copeaux ou d'un materiau analogue

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FR2252989A1 (fr) * 1973-12-04 1975-06-27 Hoechst Ag
FR2458037A1 (fr) * 1979-05-28 1980-12-26 Escher Wyss Sa Procede de traitement thermique, destine plus particulierement au sechage et a la calcination
GB2052708A (en) * 1979-05-28 1981-01-28 Escher Wyss Ltd Treating wet materials
DE2929486A1 (de) * 1979-07-20 1981-01-29 Hitachi Metals Ltd Verfahren zum dehydratisieren einer aufschlaemmung
FR2466439A1 (fr) * 1979-10-04 1981-04-10 Von Roll Ag Procede de sechage de boues, notamment de boues de stations d'epuration communales
GB2074299A (en) * 1980-03-17 1981-10-28 Salem Corp Method and Apparatus for Heating Particulate Material
FR2496085A1 (fr) * 1980-12-13 1982-06-18 Bergwerksverband Gmbh Procede et dispositif pour le sechage et la combustion des boues
WO1987004780A1 (fr) * 1986-01-31 1987-08-13 Valtion Teknillinen Tutkimuskeskus Procede de sechage d'un materiau pulverulent, granulaire ou en forme de copeaux ou d'un materiau analogue

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4028397C1 (fr) * 1990-09-07 1992-02-27 Deutsche Babcock Anlagen Ag, 4200 Oberhausen, De
EP0537637A1 (fr) * 1991-10-14 1993-04-21 Tsukishima Kikai Kabushiki Kaisha Système de séchage de boue humide
US5283959A (en) * 1991-10-14 1994-02-08 Tsukishima Kikai Kabushiki Kaisha System for drying moist sludge
WO2008122137A1 (fr) * 2007-04-04 2008-10-16 Markus Lehmann Procédé pour sécher un matériau humide
US8434241B2 (en) 2007-04-04 2013-05-07 Markus Lehmann Method for drying a wet material

Also Published As

Publication number Publication date
ES2024707B3 (es) 1992-03-01
DK21590A (da) 1990-07-30
DE3902446C1 (fr) 1990-07-05
US4970803A (en) 1990-11-20
FI895755A0 (fi) 1989-12-01
CA2006507C (fr) 1994-02-08
NO894789L (no) 1990-07-30
NO894789D0 (no) 1989-11-30
EP0379657B1 (fr) 1991-09-11
DK21590D0 (da) 1990-01-26
ATE67299T1 (de) 1991-09-15
CA2006507A1 (fr) 1990-07-27
JPH02237700A (ja) 1990-09-20

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