EP1965162A2 - Method and apparatus for drying crystalline carboxylic acids - Google Patents
Method and apparatus for drying crystalline carboxylic acids Download PDFInfo
- Publication number
- EP1965162A2 EP1965162A2 EP08003477A EP08003477A EP1965162A2 EP 1965162 A2 EP1965162 A2 EP 1965162A2 EP 08003477 A EP08003477 A EP 08003477A EP 08003477 A EP08003477 A EP 08003477A EP 1965162 A2 EP1965162 A2 EP 1965162A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- drying
- dryer
- ppm
- product
- carboxylic acids
- 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.)
- Withdrawn
Links
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
- F26B25/005—Treatment of dryer exhaust gases
-
- 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
Definitions
- the invention relates to a process for the drying of crystalline carboxylic acids, for example terephthalic acid, and to an apparatus for carrying out the process.
- crystalline carboxylic acids for example terephthalic acid
- rotary kiln dryers or steam tube dryers are mainly used, which operate because of dust explosion danger under inert or (solvent) steam atmosphere and have the type-specific disadvantages, such as difficult sealing, poor mass transfer, long residence times or caking.
- a modified steam tube dryer is proposed in which, in contrast to the conventional design, the heating medium flows around the tube (s) and the crystal slurry is conveyed through the tube.
- the parameters are set in such a way that the moisture (water or acetic acid) completely evaporates and thus a fluidization of the crystals and thus an automatic transport through the tube (s) is achieved.
- this dryer is only suitable for relatively high input moisture, otherwise it clogged.
- the drying of crystalline carboxylic acids, for example terephthalic acid is usually carried out at temperatures of at least 100 °, typically from 115 ° to 180 ° C, while residual moisture levels of 350-1250 ppm are typically achieved by 700 ppm, see, eg EP973716 . GB2024810 or US 5679848 , As a result of the high temperatures it comes in the storage silos or subsequent transport of the hot acid to lumps and caking to complete block formation.
- the EP0973716 therefore proposes, after drying, to provide cooling which cools the crystals, which generally have a humidity of between 600 and 1200 ppm, below 100 and preferably to 80 ° C. before they are stored or transported away. This can be done in a separate apparatus or during the pneumatic conveying.
- the aim of the invention is to prevent the problems of storage or transport of the hot acid without using additional steps or apparatus for cooling.
- the invention relates to a method and some advantageous embodiments of apparatus for carrying out the same, which avoid the disadvantages of the previously used methods.
- the invention is therefore characterized in that the drying takes place in a fluidized bed, the drying temperature of the product does not exceed 100 ° C and the product moisture content is less than 1200 ppm.
- the principle of the invention is based on that the drying at low
- Temperature level is performed so that the product does not need to be cooled afterwards. This is made possible because a fluidized bed apparatus is used for the drying, which, because of its good heat and mass transfer properties, despite the low temperature provides an equally good or better drying result than other dryers in the prior art.
- the drying temperature of the product does not exceed 90 ° C., advantageously 80 ° C., and the product final moisture content is less than 700 ppm, advantageously less than 350 ppm. As a result, sufficient security can be ensured that lumping and caking are prevented.
- An advantageous development is characterized in that the dust formed during drying is separated and returned to the dryer. Alternatively, it can be returned directly to the dryer or mixed with the moist input product and returned to the dryer. As a result of this recycling, the yield of the carboxylic acid, for example terephthalic acid, is substantially increased.
- drying gas If the drying gas is circulated, an economically favorable operation is possible.
- Nitrogen as a drying gas thus prevents a costly ongoing procurement of new gas.
- drying gas consists predominantly of the vapor of the moisture to be removed, whereby the excess vapor formed during the drying can be removed from the cycle in vapor or alternatively condensed form.
- the invention also relates to a device for drying crystalline carboxylic acids, for example terephthalic acid.
- a fluidized-bed dryer is provided and heat exchangers are installed in the fluidized-bed layer.
- the built-in fluidized layer heat exchanger is a particularly uniform heat transfer and a compact design with low drying gas required and / or the use of a low energy source at a low temperature level, which can be done at low temperatures, the required gentle drying of the crystals.
- a favorable development of the invention is characterized in that the heat exchangers consist of vertically erected, plate-shaped elements. This makes it possible to achieve a good heat transfer with little influence on the flow of the particles.
- a cyclone is provided for dust separation, wherein the solids outlet of the cyclone can be connected directly to the dryer or, alternatively, to the supply unit of the dryer.
- Fig. 1 the inventive method for a gas side open circuit
- Fig. 2 represents a variant of the method according to the invention with closed drying gas cycle.
- the crystal pulp A is mechanically dehydrated in a dewatering apparatus 1 (eg centrifuge, belt filter, vacuum filter) and passes via a screw conveyor 2 in the fluidized bed dryer 3. There it mixes with the fluidized and already largely dry fluidized bed content and is also dried.
- the energy required for the drying is supplied to the drying gas via a heat exchanger 4 installed in the fluidized bed (in the fluidized layer).
- This heat exchanger 4 advantageously consists of vertical, plate-shaped elements.
- the built-in fluidized layer heat exchanger is a particularly uniform heat transfer and a compact design with low drying gas required and / or the use of a low-cost energy source at a low temperature level possible.
- the executed with the fluidizing gas Fines are separated in the cyclone 7 and fed back into the fluidized bed for subsequent drying.
- the finished product leaves the dryer 3 automatically through an overflow opening and is promoted by a pneumatic system 9 for further use or storage.
- the fluidizing gas D is sucked by the fan 5, heated by a heating coil 6 and fed to the dryer. It leaves the dryer and is cleaned in the cyclone 7 and scrubber 8 before leaving the process as exhaust E.
- the gas is fed directly to the blower 5 via the exhaust pipe 10 after the scrubber 8.
- a cooler is installed in the washing liquid circuit, which makes it possible to cool the hot drying gas by injection cooling so far that the scrubber 8 acts as a condenser in which the evaporated liquid condenses out and then discharged (F)
- Other methods of gas purification and condensation can be used, e.g. Filter and surface capacitor.
- Water-moist terephthalic acid is introduced via a conveyor screw into the fluid bed dryer.
- the dryer has an inflow area of 0.6 m 2 and is provided with steam-heated plates, which dip into the fluidized layer.
- the dryer is flowed through with 430 kg / h of nitrogen at 100 ° C.
- the plates have a temperature of 118 ° C.
- the incoming product stream of 498 kg / h with 13% moisture is dried to 300 ppm residual moisture and leaves the dryer uncooled at 73 ° C.
- water-moist terephthalic acid is introduced via a screw conveyor into the fluid bed dryer.
- the dryer is passed through with 389 kg / h of nitrogen at 111 ° C.
- the plates have a temperature of 114 ° C.
- the incoming product flow of 395 kg / h with 13% Moisture is dried to 200 ppm residual moisture and leaves the dryer uncooled at 78 ° C.
- water-moist terephthalic acid is introduced via a screw conveyor into the fluid bed dryer.
- the dryer is flowed through with 735 kg / h of nitrogen at 103 ° C.
- the plates have a temperature of 139 ° C.
- the incoming product stream of 1080 kg / h with 13% moisture is dried to 350 ppm residual moisture and leaves the dryer uncooled at 93 ° C.
- water-moist terephthalic acid is introduced into the fluid bed dryer.
- the dryer is flowed through with 1770 m 3 / h of air of 144 ° C.
- the tube bundle heat exchanger immersed in the fluidized layer has a temperature of 146 ° C.
- the incoming product flow of 800 kg / h with 12.6% moisture is dried to 1080 ppm residual moisture and leaves the dryer uncooled at 93 ° C.
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Drying Of Solid Materials (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Die Erfindung betrifft ein Verfahren zur Trocknung von kristallinen Carbonsäuren, beispielsweise Terephthalsäure, sowie eine Vorrichtung zur Durchführung des Verfahrens.The invention relates to a process for the drying of crystalline carboxylic acids, for example terephthalic acid, and to an apparatus for carrying out the process.
Die Trocknung von kristallinen Carbonsäuren, beispielsweise Terephthalsäure, erfolgt am Ende des Herstellprozesses und zum Teil auch als Zwischenschritt. Dazu werden überwiegend Drehrohrtrockner oder Dampfröhrentrockner eingesetzt, die wegen Staubexplosionsgefahr unter inerter bzw. (Lösemittel-) Dampfatmosphäre arbeiten und die typspezifischen Nachteile aufweisen, wie z.B. schwierige Abdichtung, schlechter Stoffaustausch, lange Verweilzeiten oder Anbackungen. In der
Ziel der Erfindung ist es, die Probleme der Lagerung bzw. des Transportes der heißen Säure zu verhindern ohne zusätzliche Schritte bzw. Apparate zur Kühlung einzusetzen.The aim of the invention is to prevent the problems of storage or transport of the hot acid without using additional steps or apparatus for cooling.
Gegenstand der Erfindung sind ein Verfahren und einige vorteilhafte Ausführungsformen von Apparaten zur Durchführung desselben, die die Nachteile der bisher angewandten Verfahren vermeiden.The invention relates to a method and some advantageous embodiments of apparatus for carrying out the same, which avoid the disadvantages of the previously used methods.
Die Erfindung ist daher dadurch gekennzeichnet, dass die Trocknung in einer Wirbelschicht erfolgt, die Trocknungstemperatur des Produktes 100°C nicht übersteigt und die Produktendfeuchte geringer ist als 1200 ppm. Das Prinzip der Erfindung beruht darauf, dass die Trocknung auf niedrigemThe invention is therefore characterized in that the drying takes place in a fluidized bed, the drying temperature of the product does not exceed 100 ° C and the product moisture content is less than 1200 ppm. The principle of the invention is based on that the drying at low
Temperaturniveau durchgeführt wird, damit das Produkt hinterher nicht mehr gekühlt werden muss. Dies wird ermöglicht da für die Trocknung ein Wirbelschichtapparat eingesetzt wird, der wegen seiner guten Wärme- und Stoffaustauscheigenschaften trotz der niedrigen Temperatur ein gleich gutes oder besseres Trocknungsergebnis als andere Trockner im Stand der Technik liefert.Temperature level is performed so that the product does not need to be cooled afterwards. This is made possible because a fluidized bed apparatus is used for the drying, which, because of its good heat and mass transfer properties, despite the low temperature provides an equally good or better drying result than other dryers in the prior art.
Besonders günstig ist es, wenn die Trocknungstemperatur des Produktes 90°C, vorteilhafterweise 80°C nicht übersteigt und die Produktendfeuchte geringer ist als 700 ppm, vorteilhafterweise geringer als 350 ppm. Dadurch kann eine ausreichende Sicherheit gewährleistet werden, dass Klumpenbildungen und Anbackungen verhindert werden.It is particularly favorable if the drying temperature of the product does not exceed 90 ° C., advantageously 80 ° C., and the product final moisture content is less than 700 ppm, advantageously less than 350 ppm. As a result, sufficient security can be ensured that lumping and caking are prevented.
Eine vorteilhafte Weiterbildung ist dadurch gekennzeichnet, dass der bei der Trocknung entstandene Staub abgeschieden und in den Trockner zurückgeführt wird. Er kann dabei alternativ direkt in den Trockner zurückgeführt oder mit dem feuchten Eingangsprodukt vermischt und in den Trockner zurückgeführt werden. Durch diese Rückführung wird die Ausbeute an der Carbonsäure, beispielsweise Terephthalsäure, wesentlich erhöht.An advantageous development is characterized in that the dust formed during drying is separated and returned to the dryer. Alternatively, it can be returned directly to the dryer or mixed with the moist input product and returned to the dryer. As a result of this recycling, the yield of the carboxylic acid, for example terephthalic acid, is substantially increased.
Wird das Trocknungsgas im Kreislauf geführt, ist ein wirtschaftlich günstiger Betrieb möglich. Bei Verwendung von z.B. Stickstoff als Trocknungsgas wird so auch eine kostenintensive laufende Neubeschaffung des Gases verhindert.If the drying gas is circulated, an economically favorable operation is possible. When using e.g. Nitrogen as a drying gas thus prevents a costly ongoing procurement of new gas.
Besonders günstig ist es, wenn das Trocknungsgas überwiegend aus dem Dampf der zu entfernenden Feuchtigkeit besteht, wobei der bei der Trocknung entstandene Überschussbrüden dampfförmig oder alternativ kondensiert aus dem Kreislauf ausgeschleust werden kann.It is particularly favorable if the drying gas consists predominantly of the vapor of the moisture to be removed, whereby the excess vapor formed during the drying can be removed from the cycle in vapor or alternatively condensed form.
Die Erfindung betrifft auch eine Vorrichtung zur Trocknung von kristallinen Carbonsäuren, beispielsweise Terephthalsäure. Diese ist dadurch gekennzeichnet, dass ein Wirbelschichttrockner vorgesehen ist und in die fluidisierte Schicht Wärmetauscher eingebaut sind. Durch die in die fluidisierte Schicht eingebauten Wärmetauscher wird eine besonders gleichmäßige Wärmeübertragung und eine kompakte Bauweise mit niedrigem Trocknungsgasbedarf und/oder die Verwendung eines günstigen Energieträgers auf niedrigem Temperaturniveau ermöglicht, wodurch auch bei niedrigen Temperaturen die erforderliche schonende Trocknung der Kristalle erfolgen kann.The invention also relates to a device for drying crystalline carboxylic acids, for example terephthalic acid. This is characterized a fluidized-bed dryer is provided and heat exchangers are installed in the fluidized-bed layer. The built-in fluidized layer heat exchanger is a particularly uniform heat transfer and a compact design with low drying gas required and / or the use of a low energy source at a low temperature level, which can be done at low temperatures, the required gentle drying of the crystals.
Eine günstige Weiterbildung der Erfindung ist dadurch gekennzeichnet, dass die Wärmetauscher aus vertikal aufgestellten, plattenförmigen Elementen bestehen. Damit lässt sich ein guter Wärmeübergang bei einer geringen Beeinflussung der Strömung der Teilchen erzielen.A favorable development of the invention is characterized in that the heat exchangers consist of vertically erected, plate-shaped elements. This makes it possible to achieve a good heat transfer with little influence on the flow of the particles.
Besonders günstig ist es, wenn nach dem Trockner ein Zyklon zur Staubabscheidung vorgesehen ist, wobei der Feststoffauslass des Zyklons direkt mit dem Trockner oder alternativ mit dem Zuführaggregat des Trockners verbunden sein kann.It is particularly favorable if, after the dryer, a cyclone is provided for dust separation, wherein the solids outlet of the cyclone can be connected directly to the dryer or, alternatively, to the supply unit of the dryer.
Die Erfindung wird nun beispielhaft anhand der Zeichnungen beschrieben, wobei
Im erfindungsgemäßen Verfahren gemäß
Sicherheitstechnische (Explosionsgefahr) oder wirtschaftliche Überlegungen (Lösemittelrückgewinnung) machen eine geschlossene Kreislaufführung des Trocknungsgases sinnvoll. Ein derartiger Prozess ist in
Dabei wird nach dem Wäscher 8 das Gas über die Abgasleitung 10 direkt dem Gebläse 5 zugeführt. Damit sich die verdampfte Feuchtigkeit nicht im Kreislauf anreichert, wird in den Waschflüssigkeitskreislauf ein Kühler eingebaut, der es ermöglicht, durch Einspritzkühlung das heiße Trocknungsgas soweit abzukühlen, dass der Wäscher 8 als Kondensator wirkt in dem die verdampfte Flüssigkeit auskondensiert und dann ausgeschleust (F) wird. Auch andere Verfahren der Gasreinigung und Kondensation lassen sich einsetzen, z.B. Filter und Oberflächenkondensator.In this case, the gas is fed directly to the blower 5 via the
In einem Aufbau ähnlich
In einem Aufbau ähnlich Beispiel 1 wird wasserfeuchte Terephthalsäure über eine Förderschnecke in den Fliessbetttrockner eingetragen. Der Trockner wird mit 389 kg/h Stickstoff von 111°C durchströmt. Die Platten haben eine Temperatur von 114°C. Der eintretende Produktstrom von 395 kg/h mit 13% Feuchte wird auf 200 ppm Restfeuchte getrocknet und verlässt den Trockner ungekühlt mit 78°C.In a structure similar to Example 1, water-moist terephthalic acid is introduced via a screw conveyor into the fluid bed dryer. The dryer is passed through with 389 kg / h of nitrogen at 111 ° C. The plates have a temperature of 114 ° C. The incoming product flow of 395 kg / h with 13% Moisture is dried to 200 ppm residual moisture and leaves the dryer uncooled at 78 ° C.
In einem Aufbau ähnlich Beispiel 1 wird wasserfeuchte Terephthalsäure über eine Förderschnecke in den Fliessbetttrockner eingetragen. Der Trockner wird mit 735 kg/h Stickstoff von 103°C durchströmt. Die Platten haben eine Temperatur von 139°C. Der eintretende Produktstrom von 1080 kg/h mit 13% Feuchte wird auf 350 ppm Restfeuchte getrocknet und verlässt den Trockner ungekühlt mit 93°C.In a structure similar to Example 1, water-moist terephthalic acid is introduced via a screw conveyor into the fluid bed dryer. The dryer is flowed through with 735 kg / h of nitrogen at 103 ° C. The plates have a temperature of 139 ° C. The incoming product stream of 1080 kg / h with 13% moisture is dried to 350 ppm residual moisture and leaves the dryer uncooled at 93 ° C.
In einem Aufbau ähnlich Beispiel 1, jedoch nicht in Gaskreislauffahrweise, wird wasserfeuchte Terephthalsäure in den Fliessbetttrockner eingetragen. Der Trockner wird mit 1770 m3/h Luft von 144°C durchströmt. Der Rohrbündelwärmetauscher, der in die fluidisierte Schicht eintaucht, hat eine Temperatur von 146°C. Der eintretende Produktstrom von 800 kg/h mit 12,6% Feuchte wird auf 1080 ppm Restfeuchte getrocknet und verlässt den Trockner ungekühlt mit 93°C.In a structure similar to Example 1, but not in gas cycle mode, water-moist terephthalic acid is introduced into the fluid bed dryer. The dryer is flowed through with 1770 m 3 / h of air of 144 ° C. The tube bundle heat exchanger immersed in the fluidized layer has a temperature of 146 ° C. The incoming product flow of 800 kg / h with 12.6% moisture is dried to 1080 ppm residual moisture and leaves the dryer uncooled at 93 ° C.
Claims (17)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT3372007A AT504996B1 (en) | 2007-03-02 | 2007-03-02 | METHOD AND DEVICE FOR DRYING CRYSTALLINE CARBOXYLIC ACIDS |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1965162A2 true EP1965162A2 (en) | 2008-09-03 |
EP1965162A3 EP1965162A3 (en) | 2014-02-26 |
Family
ID=39469503
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP08003477.0A Withdrawn EP1965162A3 (en) | 2007-03-02 | 2008-02-26 | Method and apparatus for drying crystalline carboxylic acids |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1965162A3 (en) |
CN (1) | CN101270044A (en) |
AT (1) | AT504996B1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106766680A (en) * | 2016-12-02 | 2017-05-31 | 安徽强旺生物工程有限公司 | Continuous fluidized bed drying system is used in Variety salt production |
CN108302923A (en) * | 2017-12-08 | 2018-07-20 | 安徽三兄弟薯业有限责任公司 | A kind of instant vermicelli drying unit |
CN110131966A (en) * | 2019-05-20 | 2019-08-16 | 天津科技大学 | Intermittent combustion internal heating type fluidized bed drying device |
CN111854333A (en) * | 2020-06-16 | 2020-10-30 | 安徽泰德康农业科技发展有限公司 | Energy-saving sesame drying fluidized bed drying system |
DE102021125452B4 (en) | 2021-09-30 | 2024-06-27 | Dr. Weigel Anlagenbau Gmbh | Drying device and method for operating a drying device |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2024810A (en) | 1978-06-08 | 1980-01-16 | Orient Chemical Ind | Method of obtaining dried terephthalic acid |
US5679848A (en) | 1995-01-24 | 1997-10-21 | Huels Aktiengesellschaft | Process for the preparation of terephthalic acid and its isomers |
EP0973716A1 (en) | 1997-04-10 | 2000-01-26 | E.I. Du Pont De Nemours And Company | Improved method for producing crystalline carboxylic acids and apparatus therefor |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4133857A (en) * | 1975-09-16 | 1979-01-09 | Chisso Corporation | Method for producing a granular sorbic acid |
CH644683A5 (en) * | 1979-05-28 | 1984-08-15 | Escher Wyss Ag | METHOD FOR THERMALLY TREATING A MATERIAL LAYER. |
DE3306250A1 (en) * | 1983-02-23 | 1984-08-23 | Basf Ag, 6700 Ludwigshafen | SPHERICAL SINGLE CRYSTALS FOR PHARMACEUTICAL PURPOSES |
DE3902446C1 (en) * | 1989-01-27 | 1990-07-05 | Sulzer-Escher Wyss Gmbh, 7980 Ravensburg, De | |
DE4206521A1 (en) * | 1992-03-02 | 1993-09-09 | Cognis Bio Umwelt | Drying wetting, washing and/or cleaning agent or component |
DE4316320A1 (en) * | 1993-05-15 | 1994-11-17 | Degussa | Process for the production of sodium perborate monohydrate |
DE19620047C2 (en) * | 1996-05-18 | 2002-06-27 | Rwe Rheinbraun Ag | Method and device for drying lignite |
US20050288527A1 (en) * | 2004-06-28 | 2005-12-29 | Cook William L | Method for preparing free-flowing crystalline material |
-
2007
- 2007-03-02 AT AT3372007A patent/AT504996B1/en not_active IP Right Cessation
-
2008
- 2008-02-26 EP EP08003477.0A patent/EP1965162A3/en not_active Withdrawn
- 2008-03-03 CN CN 200810080681 patent/CN101270044A/en active Pending
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2024810A (en) | 1978-06-08 | 1980-01-16 | Orient Chemical Ind | Method of obtaining dried terephthalic acid |
US5679848A (en) | 1995-01-24 | 1997-10-21 | Huels Aktiengesellschaft | Process for the preparation of terephthalic acid and its isomers |
EP0973716A1 (en) | 1997-04-10 | 2000-01-26 | E.I. Du Pont De Nemours And Company | Improved method for producing crystalline carboxylic acids and apparatus therefor |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106766680A (en) * | 2016-12-02 | 2017-05-31 | 安徽强旺生物工程有限公司 | Continuous fluidized bed drying system is used in Variety salt production |
CN108302923A (en) * | 2017-12-08 | 2018-07-20 | 安徽三兄弟薯业有限责任公司 | A kind of instant vermicelli drying unit |
CN110131966A (en) * | 2019-05-20 | 2019-08-16 | 天津科技大学 | Intermittent combustion internal heating type fluidized bed drying device |
CN111854333A (en) * | 2020-06-16 | 2020-10-30 | 安徽泰德康农业科技发展有限公司 | Energy-saving sesame drying fluidized bed drying system |
DE102021125452B4 (en) | 2021-09-30 | 2024-06-27 | Dr. Weigel Anlagenbau Gmbh | Drying device and method for operating a drying device |
Also Published As
Publication number | Publication date |
---|---|
AT504996B1 (en) | 2009-03-15 |
CN101270044A (en) | 2008-09-24 |
AT504996A1 (en) | 2008-09-15 |
EP1965162A3 (en) | 2014-02-26 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0067299B1 (en) | Process and apparatus for operating a coke oven plant | |
DE112008002740B4 (en) | Indirect heat drying device, Indirect heat drying process for drying a substance to be dried | |
EP0379657B1 (en) | Sludge drying process | |
AT504996B1 (en) | METHOD AND DEVICE FOR DRYING CRYSTALLINE CARBOXYLIC ACIDS | |
DE2256385A1 (en) | PROCESS AND DEVICE FOR CONTINUOUS HEATING OF FINE-GRAIN MATERIALS, IN PARTICULAR COAL, TO AN EQUAL, EXACTLY CONTROLLED FINAL TEMPERATURE | |
EP0091566A1 (en) | Process and apparatus for the post condensation of polycondensates | |
DE2640508C2 (en) | Process for heating two-stage coal entrained flow dryers | |
EP2029267A1 (en) | Process and apparatus for continuous polymerization of polymer in solid phase | |
DE3613305A1 (en) | METHOD AND DEVICE FOR FLUIDIZED STEAM DRYING OF LOW-QUALITY COALS BY WET CLEANING | |
EP0716264B1 (en) | Method and installation for sludge combustion | |
EP2858802A1 (en) | Method and device for drying and crystallizing granulate | |
EP2994707B1 (en) | Method for producing salts with a reduced water of crystallisation content | |
DE2626653A1 (en) | METHOD AND DEVICE FOR PRE-HEATING COAL | |
DE19729302A1 (en) | Deodorising of freshly cut polypropylene chips | |
DE2415024B2 (en) | ||
US4514910A (en) | Dehydration of lignite or the like | |
DE3323770C2 (en) | ||
DE3912586A1 (en) | Process and regeneration device for the thermal treatment, such as drying, low-temperature carbonisation or gasification, of pasty or sludge-like substances | |
DE69204420T2 (en) | Process for removing pollutants from substrate drying gas. | |
US4979313A (en) | Process for cooling hygroscopic powder | |
DE4221573A1 (en) | Method and arrangement for drying tobacco | |
DE3305994A1 (en) | METHOD FOR DRY DISTILLING BITUMIOUS OR OIL-BASED SOLIDS | |
DE602004012765T2 (en) | COOLING PELLETS FROM A REACTOR FOR POST-POLYMERIZATION OF PET IN FIXED CONDITION WITH WATER | |
DE1729240C3 (en) | Method of drying sewage sludge | |
AT389466B (en) | Process and installation for the heat treatment of materials with a solids content |
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 |
|
AK | Designated contracting states |
Kind code of ref document: A2 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR |
|
AX | Request for extension of the european patent |
Extension state: AL BA MK RS |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: STANKE, KLAUS, DIPL.-ING. Inventor name: HOFMANN, PETER, DR. ING. Inventor name: JUNKER, KURT, DIPL.-ING. Inventor name: KROEHL PAUL, DR. ING. |
|
PUAL | Search report despatched |
Free format text: ORIGINAL CODE: 0009013 |
|
AK | Designated contracting states |
Kind code of ref document: A3 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR |
|
AX | Request for extension of the european patent |
Extension state: AL BA MK RS |
|
RIC1 | Information provided on ipc code assigned before grant |
Ipc: F26B 3/084 20060101AFI20140123BHEP Ipc: C07C 51/43 20060101ALN20140123BHEP Ipc: F26B 25/00 20060101ALN20140123BHEP |
|
AKY | No designation fees paid | ||
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R108 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R108 Effective date: 20141029 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20140827 |