AT390018B - METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES - Google Patents
METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES Download PDFInfo
- Publication number
- AT390018B AT390018B AT0117188A AT117188A AT390018B AT 390018 B AT390018 B AT 390018B AT 0117188 A AT0117188 A AT 0117188A AT 117188 A AT117188 A AT 117188A AT 390018 B AT390018 B AT 390018B
- Authority
- AT
- Austria
- Prior art keywords
- reactor
- medium
- recuperator
- thermal treatment
- condenser
- Prior art date
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
- C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- 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
- F26B21/06—Controlling, e.g. regulating, parameters of gas supply
- F26B21/08—Humidity
- F26B21/086—Humidity by condensing the moisture in the drying medium, which may be recycled, e.g. using a heat pump cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B23/00—Heating arrangements
- F26B23/001—Heating arrangements using waste heat
- F26B23/002—Heating arrangements using waste heat recovered from dryer exhaust gases
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Dispersion Chemistry (AREA)
- Microbiology (AREA)
- Sustainable Development (AREA)
- Drying Of Solid Materials (AREA)
Description
Nr. 390018No. 390018
Die Erfindung betrifft ein Verfahren zur thermischen Behandlung wie z. B. Trocknung, Verschwelung, Vergasung pastöser oder schlammartiger Substanzen in einem beheizten Reaktor wie z. B. Wirbelbett, dessen abströmendes Medium nach Abscheidung von staubförmigen und Auskondensierung von dampfförmigen Verunreinigungen bzw. Überschußmengen zumindest teilweise dem Reaktor wieder zugeführt wird, und eine 5 Regenerationseinrichtung für ein im Kreislauf geführtes Medium, insbesondere Gas-Dampf-Gemisch, zur Durchführung des Verfahrens.The invention relates to a method for thermal treatment such. B. drying, carbonization, gasification of pasty or sludge-like substances in a heated reactor such. B. fluidized bed, the outflowing medium after separation of dust-like and condensation of vaporous impurities or excess amounts is at least partially fed back to the reactor, and a regeneration device for a circulated medium, in particular gas-steam mixture, for carrying out the process.
Bei den bekannten Anlagen (EU-A2-203.059, DE-OS 27 34 198 und DE-OS 31 18 931) erfolgt die Abscheidung in einem Nebenkreis, wobei das Nichtkondensierbare abgeführt werden muß, wodurch es zu Wärmeverlusten kommt. Es ist auch bekannt, dieses Verfahren im direkten Kreis durchzuführen, wobei aber das 10 gesättigte Medium mit mehr oder weniger großen Tropfen durch das Gebläse wieder in den Reaktor eingeblasen wird. Bei der letzteren Konstruktion treten im Gebläse Erosionen und im Reaktor Unterkühlungen auf, die letzten Endes durch verstärkte Beheizung behoben werden müssen.In the known systems (EU-A2-203.059, DE-OS 27 34 198 and DE-OS 31 18 931), the separation takes place in a secondary circuit, the non-condensable must be removed, which leads to heat losses. It is also known to carry out this process in a direct circuit, but the saturated medium is blown back into the reactor with more or less large drops through the fan. In the latter design, erosions occur in the fan and subcooling occurs in the reactor, which ultimately has to be remedied by increased heating.
Die Erfindung hat es sich zur Aufgabe gestellt, diesem Nachteil zu begegnen und praktisch mit einem trockenen Gas in den Reaktor einzutreten, so daß eine Anfeuchtung des zu trocknenden Gutes bzw. eine 15 übermäßige Wärmeaufnahme durch das eingeblasene Medium vermieden werden kann, wodurch einerseits der Dampfverbrauch für die Beheizung des Reaktors erniedrigt und andererseits auch die Instandhaltungskosten vermindert werden, da das Kreislaufgebläse mit trockenem Medium gefahren wird. Darüber hinaus läßt sich Heißwasser gewinnen, welches nicht bei atmosphärischen Bedingungen ausdampft, so daß Schwadenbildungen, insbesondere auf der Seite des Schmutzkondensates, nicht auftreten. 20 Die Erfindung ist dadurch gekennzeichnet, daß das vom Reaktor abströmende Medium über einen als Rekuperator geschalteten Enthitzer geführt und insbesondere auf Sättigungstemperatur gekühlt wird und daß das vom Rekuperator abströmende gekühlte Medium nach der in einer oder mehreren Stufen erfolgten Auskondensation wieder dem Rekuperator zur Wiedererhitzung bzw. Trocknung und schließlich über der Sättigungstemperatur wieder dem Reaktor zugeführt wird. Insbesondere weist das getrocknete Medium am 25 Reaktoreintritt weniger als 50 Vol. %, insbesondere 30 Vol. %, Dampfgehalt auf. Die erfindungsgemäße Regenerationseinrichtung zur Durchführung des Verfahrens ist dadurch gekennzeichnet, daß zwischen dem Reaktor und Kondensator sowie Kondensator und Kreislaufgebläse ein als Rekuperator geschalteter Gas-Gas-Wärmetauscher vorgesehen ist.The invention has set itself the task of addressing this disadvantage and practically enter the reactor with a dry gas, so that moistening of the material to be dried or excessive heat absorption by the blown-in medium can be avoided, thereby reducing steam consumption for heating the reactor and, on the other hand, the maintenance costs are also reduced, since the circulation fan is operated with dry medium. In addition, hot water can be obtained, which does not evaporate under atmospheric conditions, so that steam formation, especially on the side of the dirt condensate, does not occur. The invention is characterized in that the medium flowing out of the reactor is passed through a desuperheater connected as a recuperator and in particular is cooled to saturation temperature, and in that the cooled medium flowing out of the recuperator after the condensation has taken place in one or more stages, the recuperator for reheating or Drying and finally fed back to the reactor above the saturation temperature. In particular, the dried medium at the reactor inlet has a vapor content of less than 50% by volume, in particular 30% by volume. The regeneration device according to the invention for carrying out the method is characterized in that a gas-gas heat exchanger connected as a recuperator is provided between the reactor and the condenser as well as the condenser and circuit blower.
Die Erfindung ist in der angeschlossenen Figur beispielsweise und schematisch dargestellt. 30 Die Fig. zeigt einen beheizten Reaktor (1), der als Wirbelbettreaktor, beispielsweise zum Trocknen grubenfeuchter Kohle, ausgebildet ist. Dieser Reaktor wird durch Heizflächen (5) beheizt, die im Wirbelbett angeordnet sind und von einem kondensierenden Medium durchströmt werden. Durch den Wärmeeintrag dieser Heizflächen kommt es zu einem Trocknungseffekt, und es entstehen Brüden, die etwa mit Fließbett-Temperatur über die Leitung (6) abgesaugt werden. Der Brüden wird im Trockenentstauber (7) entstaubt und in einem als 35 Regenerator geschalteten Wärmetauscher (4) anschließend etwa auf Sättigungstemperatur abgekühlt. Im angeschlossenen Kondensator (2) werden mitgeführte Dämpfe kondensiert, wobei der Brüden noch weiter abgekühlt wird. Der kalte Brüden wird nun über die Leitung (6') wieder dem Wärmetauscher (4) zugeführt, wobei die ursprüngliche Temperatur fast wieder erreicht wird. Aber durch die Kondensatdurchströmung hat der Brüden sehr viel an Feuchtigkeit verloren, so daß die Dämpfe am Eintritt in das Gebläse quasi in überhitztem 40 Zustand vorliegen und so trocken in das Gebläse und auch wieder in den Reaktor (1) eingeblasen werden. Durch diese Maßnahme kann es auch zu keiner Tröpfchenbildung am Reaktor kommen, selbst wenn der rezirkulierte Brüden direkt mit der noch kalten Substanz bzw. Kohle im Bereich des Einlasses (8) in Kontakt kommt. Würde bei dem bis jetzt beschriebenen Verfahren die getrocknete Kohle mit etwa 100° ins Freie kommen, würde die Kohle unter atmosphärischen Bedingungen ausdampfen, bis es zu einem Gleichgewichtszustand mit der 45 Atmosphäre kommt. Es ist daher ein weiterer Zweck der Erfindung, auch das Ausdampfen des heißen getrockneten Gutes zu verringern, indem für die fertig getrocknete Substanz eine Kühlung vorgesehen wird. Zu diesem Zweck zweigt von der Leitung (6') am Ausgang des Kondensators (2) eine Zweigleitung (9) ab, die eventuell zu einem Endkondensator (14) zur weiteren Entfeuchtung und einem Kondensatkühler (10) zur Trocknung des Brüden zugeführt wird, in welchem das wärmere Kondensat den gesättigten Brüden etwas erwärmt, 50 so daß er er im ungesättigten Zustand, also trocken, dem Gebläse (3') zugeführt wird und von diesem einem Fließbettkühler für die abströmende getrocknete Substanz eingeblasen wird und dort als Fluidisierungsmedium Wärme und Feuchte von der getrockneten Substanz aufnimmt und schließlich in den Reaktor (1) abströmt und sich dort mit dem über die Hauptleitung (6') strömenden Medium mischt. In dieser Zweigleitung (9) strömt etwa 5 bis 10 % der Menge, die durch die Leitung (6) strömt, so daß der Mischungsverlust bei etwaigem 55 Temperaturunterschied der beiden gasförmigen Medien in der Mischkammer (11) gering ist. Die getrocknete und gekühlte Substanz verläßt gemäß Pfeil (12) den Kühler (13), wobei durch die abgesenkte Temperatur der Substanz das Ausdampfen bedeutend vermindert wurde. Zur Verbesserung des Temperaturüberganges bzw. der Temperatur der einzelnen Dampfströme ist es von Vorteil, den Rekuperator als mehrstufigen Wärmetauscher (4) auszubilden, wobei es auch günstig ist, den Kondensator (2) mehrstufig auszubilden, so daß unter Umständen 60 Kondensate mit unterschiedlicher Zusammensetzung und unterschiedlicher Temperatur entstehen, die die Wirtschaftlichkeit der Anlagen noch weiter heben können. Genauso ist es möglich, noch weitere Kühleinrichtungen (13) vorzusehen, um den Ausdampfeffekt der getrockneten Substanz zm;Erreichung des -2-The invention is shown, for example and schematically in the attached figure. 30 The figure shows a heated reactor (1) which is designed as a fluidized bed reactor, for example for drying coal which is moist with mines. This reactor is heated by heating surfaces (5) which are arranged in the fluidized bed and through which a condensing medium flows. The heat input from these heating surfaces leads to a drying effect and vapors are formed which are sucked off via the line (6), for example at a fluid bed temperature. The vapors are dedusted in a dry deduster (7) and then cooled to about saturation temperature in a heat exchanger (4) connected as a regenerator. Any vapors entrained are condensed in the connected condenser (2), the vapor being cooled even further. The cold vapor is then fed back to the heat exchanger (4) via the line (6 '), the original temperature almost being reached again. But due to the flow of condensate, the vapors have lost a great deal of moisture, so that the vapors at the inlet to the blower are virtually overheated and are thus blown dry into the blower and also back into the reactor (1). This measure also prevents droplets from forming in the reactor, even if the recirculated vapor comes into direct contact with the still cold substance or coal in the area of the inlet (8). If the dried coal were released into the open at about 100 ° in the process described so far, the coal would evaporate under atmospheric conditions until a state of equilibrium with the 45 atmosphere occurs. It is therefore a further purpose of the invention to also reduce the evaporation of the hot dried material by providing cooling for the finished dried substance. For this purpose, a branch line (9) branches off from the line (6 ') at the outlet of the condenser (2), which may be fed to an end condenser (14) for further dehumidification and a condensate cooler (10) for drying the vapor which the warmer condensate warms the saturated vapors a little, 50 so that it is fed to the blower (3 ') in the unsaturated state, i.e. dry, and is blown into a blower bed cooler for the outflowing dried substance, where it acts as a fluidizing medium for heat and moisture absorbs the dried substance and finally flows out into the reactor (1), where it mixes with the medium flowing through the main line (6 '). In this branch line (9) flows about 5 to 10% of the amount that flows through the line (6), so that the mixture loss is small with any temperature difference between the two gaseous media in the mixing chamber (11). The dried and cooled substance leaves the cooler (13) according to arrow (12), the evaporation being significantly reduced by the reduced temperature of the substance. To improve the temperature transition or the temperature of the individual steam streams, it is advantageous to design the recuperator as a multi-stage heat exchanger (4), it also being favorable to design the condenser (2) in multiple stages, so that under certain circumstances 60 condensates with different compositions and different temperatures arise, which can further increase the efficiency of the systems. It is also possible to provide further cooling devices (13) in order to increase the evaporation effect of the dried substance;
Claims (7)
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT0117188A AT390018B (en) | 1988-05-05 | 1988-05-05 | METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES |
DE3912586A DE3912586A1 (en) | 1988-05-05 | 1989-04-17 | Process and regeneration device for the thermal treatment, such as drying, low-temperature carbonisation or gasification, of pasty or sludge-like substances |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT0117188A AT390018B (en) | 1988-05-05 | 1988-05-05 | METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES |
Publications (2)
Publication Number | Publication Date |
---|---|
ATA117188A ATA117188A (en) | 1989-08-15 |
AT390018B true AT390018B (en) | 1990-03-12 |
Family
ID=3508145
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
AT0117188A AT390018B (en) | 1988-05-05 | 1988-05-05 | METHOD AND REGENERATION DEVICE FOR THERMAL TREATMENT, E.g. DRYING, SWELLING, GASIFICATION OF PASTOESER OR SLUDGEY SUBSTANCES |
Country Status (2)
Country | Link |
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AT (1) | AT390018B (en) |
DE (1) | DE3912586A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114835370A (en) * | 2022-04-28 | 2022-08-02 | 杭州真一环保科技有限公司 | Sludge low-temperature drying coupling pyrolysis device |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5092959A (en) * | 1990-04-27 | 1992-03-03 | Yamato Scientific Co., Ltd. | Organic solvent spray dryer device |
DE4029525A1 (en) * | 1990-09-18 | 1992-03-19 | Umwelt & Energietech | METHOD AND DEVICE FOR DRYING SOLID MATERIALS IN AN INDIRECTLY HEATED FLUIDIZED BED |
DE4319828A1 (en) * | 1993-06-16 | 1994-12-22 | Henkel Kgaa | Modified drying process using superheated steam in the drying medium and its application |
ATE203761T1 (en) * | 1996-04-30 | 2001-08-15 | Christian Eder | METHOD AND DEVICE FOR PROCESSING BIOLOGICAL RESIDUES, IN PARTICULAR SEWAGE SLUDGE |
CN102224389B (en) * | 2008-11-24 | 2013-10-02 | Rwe动力股份公司 | Method for generating process steam |
CN104857903B (en) * | 2014-02-21 | 2017-03-29 | 中国科学院工程热物理研究所 | A kind of chemical heat pump device containing reactive distillation and series connection exothermic reactor |
WO2020201277A1 (en) | 2019-04-02 | 2020-10-08 | Covestro Intellectual Property Gmbh & Co. Kg | Drying apparatus and use thereof and process for producing an isocyanate using the drying apparatus |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2734198A1 (en) * | 1977-07-29 | 1979-02-08 | Babcock Bsh Ag | Low energy hot gas double treatment dryer - has closed circuit plus branch with cooler and condenser |
DE3118931A1 (en) * | 1981-05-13 | 1982-12-02 | Krupp-Koppers Gmbh, 4300 Essen | METHOD AND DEVICE FOR OPERATING A COOKING PLANT |
EP0203059A2 (en) * | 1985-05-22 | 1986-11-26 | Waagner-Biro Aktiengesellschaft | Process for drying granular material, and a fluid bed dryer |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE927349C (en) * | 1953-09-19 | 1955-05-05 | Basf Ag | Process for the refining of mineral oils and tars and their distillation, cracking and hydrogenation products by catalytic pressure hydrogenation |
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1988
- 1988-05-05 AT AT0117188A patent/AT390018B/en not_active IP Right Cessation
-
1989
- 1989-04-17 DE DE3912586A patent/DE3912586A1/en not_active Withdrawn
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2734198A1 (en) * | 1977-07-29 | 1979-02-08 | Babcock Bsh Ag | Low energy hot gas double treatment dryer - has closed circuit plus branch with cooler and condenser |
DE3118931A1 (en) * | 1981-05-13 | 1982-12-02 | Krupp-Koppers Gmbh, 4300 Essen | METHOD AND DEVICE FOR OPERATING A COOKING PLANT |
EP0203059A2 (en) * | 1985-05-22 | 1986-11-26 | Waagner-Biro Aktiengesellschaft | Process for drying granular material, and a fluid bed dryer |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114835370A (en) * | 2022-04-28 | 2022-08-02 | 杭州真一环保科技有限公司 | Sludge low-temperature drying coupling pyrolysis device |
Also Published As
Publication number | Publication date |
---|---|
ATA117188A (en) | 1989-08-15 |
DE3912586A1 (en) | 1989-11-16 |
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