EP1015527A1 - Method for thermal treatment of material containing volatile, combustible constituents - Google Patents

Method for thermal treatment of material containing volatile, combustible constituents

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Publication number
EP1015527A1
EP1015527A1 EP98945153A EP98945153A EP1015527A1 EP 1015527 A1 EP1015527 A1 EP 1015527A1 EP 98945153 A EP98945153 A EP 98945153A EP 98945153 A EP98945153 A EP 98945153A EP 1015527 A1 EP1015527 A1 EP 1015527A1
Authority
EP
European Patent Office
Prior art keywords
reactor
pyrolysis reactor
solids
hot
trickle zone
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
EP98945153A
Other languages
German (de)
French (fr)
Other versions
EP1015527B1 (en
Inventor
Hans-Jürgen WEISS
Udo Zentner
Jörg SCHMALFELD
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MG Technologies AG
Original Assignee
Metallgesellschaft AG
MG Technologies AG
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Publication of EP1015527A1 publication Critical patent/EP1015527A1/en
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Publication of EP1015527B1 publication Critical patent/EP1015527B1/en
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Classifications

    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form

Definitions

  • the invention relates to a method for the thermal treatment of volatile, combustible feed material with a water content of up to 20 wt .-%, wherein the feed material is mixed with hot granular solids coming from a collection bunker in a pyrolysis reactor , withdrawing gases and vapors from the reactor and generating a solid mixture in the reactor which is removed from the reactor, at least a portion of which is heated outside the reactor and returned to the pyrolysis reactor via the collection bunker.
  • a method of this type is known from US Pat. No. 3,703,442, which is used for the thermal depolymerization of bituminous materials and in particular oil shale.
  • the oil shale is mixed with granular hot solids of around 630 ° C, resulting in a mixing temperature of around 530 ° C.
  • the invention has for its object to obtain a gas with the highest possible heating value from the feed material, which is completely or largely tar-free and thus has only a low content of condensable organic constituents. According to the invention, this is achieved in the process mentioned at the outset by passing the hot granular solids at temperatures in the range from 700 to 1100 ° C.
  • Moving bed or fluidized bed with temperatures in the range of 650 to 1000 ° C has that the hot granular solids and the feed material at least partially together down through the trickle zone to the moving bed or fluidized bed and that gases and vapors from the moving bed or fluidized bed upwards countercurrent to the hot solids through the trickle zone before being withdrawn from the top of the reactor.
  • the hot granular solids are also referred to below as heat transfer solids.
  • G amount of gas generated (Nm 3 / h) /
  • M amount of feed material (kg / h)
  • a lower calorific value of the gas produced (MJ / Nm 3 )
  • b lower calorific value of the feed material (MJ / kg).
  • Thermally dried sewage sludge, biomass, waste plastics or other materials containing various organic residues with a high proportion of volatile constituents can be used as the material to be fed into the pyrolysis reactor.
  • the feed material is passed simultaneously through one or more feed points into the trickle zone of the pyrolysis reactor. If there are several feed points, the feed material is pre-distributed. Usually, the moist material will be passed through 1 to 6 feed points into the reactor.
  • the feed points can open in the upper, middle or lower area of the trickle zone.
  • the pyrolysis reactor and in particular also its trickle zone are expediently free of rotating mixing devices in order to rule out wear problems as far as possible.
  • fixed roof-like fixtures can be used to divide and redirect the trickling streams of solids several times so that they can be mixed quickly.
  • a height of 1 to 10 m is recommended for the trickle zone, the height being determined in individual cases depending on the material used and the temperatures, in particular in the trickle zone.
  • the speed of the cracking reactions increases with increasing temperature, so that shorter residence times can be used at high temperatures.
  • the collection bunker may also be advisable to use the collection bunker to further increase the temperature of the heat transfer solids before they are fed into the pyrolysis reactor.
  • a gas containing 0 2 e.g. air
  • combustion can be provided there, which increases the temperatures in the desired manner.
  • Fig. 1 is a flow diagram of the method
  • Fig. 2 shows a variant of the pyrolysis reactor in longitudinal section.
  • the line (2) branches before entering the reactor (1) to several feed points (2a) and (2b).
  • the trickle zone (la) In the upper area of the reactor (1) is the trickle zone (la), below which the solid mixture (4) forms a moving bed or fluidized bed. If you have a reactor gas, e.g. B. nitrogen or steam, through the dashed line (5) supplies, you can
  • the solid mixture (4) forms a bed, which slowly moves downwards as a moving bed, because solids are continuously drawn off through the line (6).
  • the trickle zone already in the trickle zone (la), the hot solids brought in through line (3) at temperatures of 700 to 1100 ° C. are at least partially mixed with the feed material.
  • the trickle zone has stationary deflection devices in the form of several roof-like internals (8) on. A rotating mixing device is not used.
  • the hot heat transfer solids moving down through the trickle zone (la) come into intensive contact with the feed material, which also moves downwards, which is heated and subjected to degassing.
  • gases and vapors flow upwards through the trickle zone (la), which are formed during the heating.
  • the gases and vapors are passed through line (9) to a cyclone separator (10), where the entrained solids are largely separated.
  • the solids can at least partially be returned to the reactor (1) through line (11), and part can be removed from the process through line (12).
  • the gases and vapors leaving the cyclone separator (10) through line (15) are fed to a gas cleaning system (16) known per se, cooling also taking place. Purified gases and vapors are drawn for further use, e.g. B. as fuel gas in line (17).
  • the hot solid mixture drawn off from the reactor (1) in line (6) can be partially removed from the process through line (7).
  • the remaining solids are fed to the bottom of a pneumatic conveyor line (20), to which hot air is fed through line (21).
  • the hot air conveys the solids upwards, at the same time burning combustible substances, which leads to the heating of the solids.
  • the mixture of solids and gases reaches a collection bunker (22), gases are drawn off through line (23), passed through a cyclone separator (24) and fed to a waste gas cleaning system (not shown) in line (25). Secluded Solids can be removed in line (26) or fed back through line (26a) into the collection bunker (22).
  • the hot granular solids that collect in the lower area of the bunker (22) have temperatures of 700 to 1100 ° C. If these temperatures are not already reached in the pneumatic conveyor section (20), a gas containing 0 2 (e.g. air) can be supplied to the bunker (22) through the line (28) and the temperatures in the bunker increased by post-combustion .
  • the gas supply through line (28) can also be used to remove dust-fine solids by sifting these dusts through line (23) to separator (24) and through line (26) from the circuit away.
  • Fig. 2 shows a modified embodiment of the pyrolysis reactor (1) with countercurrent flow of the hot heat transfer solids and the gases and vapors formed above the mouths of the lines (2a) and (2b) through which the feed material is fed.
  • the heat transfer solids come from line (3); the other reference numerals have the meaning already explained together with FIG. 1.
  • a pyrolysis reactor (1) as shown in Fig. 2, 5 t of dried sewage sludge with a residual moisture content of 7 wt .-% are fed through line (2) per hour.
  • the sewage sludge consists of 63% by weight of volatile components, it has a lower calorific value of 17.0 MJ / kg.
  • the reactor (1) is carried out at 80 t / h hot heat transfer solids at 900 ° C the line (3). This produces 2920 Nm 3 / h, 850 ° C hot pyrolysis gas with a lower calorific value of 23.3 MJ / Nm 3 which is discharged through line (9), dedusted in the cyclone (10) and then fed to gas cleaning (16).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The feed material containing volatile, combustible constituents can have a water content of up to 20 wt. %. Said material is mixed with hot granulated solids in a pyrolysis reactor. The hot solids come from a collecting bin at temperatures ranging from 700-1100 DEG C and are conducted to the upper area of the pyrolysis reactor. The upper area of the reactor contains a flow zone. A moving bed or a fluidized bed with temperatures ranging from 650 DEG -1000 DEG C are arranged below the flow zone. The hot, granular solids and the feed material are jointly conducted at least in part through the flow area or fluidized bed in a downward direction. Gases and vapours are guided through the flow zone in an upward direction and removed from the upper area of the reactor. A solid mixture is removed from the lower area of the reactor and at least one part thereof is heated outside the reactor and is returned to the pyrolysis reactor via the collector bin.

Description

Verfahren zum thermischen Behandeln von flüchtige, brennbare Bestandteile enthaltendem Material Process for the thermal treatment of volatile material containing combustible components
Beschreibungdescription
Die Erfindung betrifft ein Verfahren zum thermischen Behandeln von flüchtige, brennbare Bestandteile enthaltendem Einsatz-Material mit einem Wassergehalt von bis zu 20 Gew.-%, wobei man das Einsatz-Material mit heißen körnigen Feststoffen, die aus einem Sammelbunker kommen, in einem Pyrolysereaktor mischt, aus dem Reaktor Gase und Dämpfe abzieht und im Reaktor ein Feststoffgemisch erzeugt, welches man aus dem Reaktor abführt, wobei man mindestens einen Teil davon außerhalb des Reaktors erhitzt und über den Sammelbunker in den Pyrolysereaktor zurückführt .The invention relates to a method for the thermal treatment of volatile, combustible feed material with a water content of up to 20 wt .-%, wherein the feed material is mixed with hot granular solids coming from a collection bunker in a pyrolysis reactor , withdrawing gases and vapors from the reactor and generating a solid mixture in the reactor which is removed from the reactor, at least a portion of which is heated outside the reactor and returned to the pyrolysis reactor via the collection bunker.
Aus dem US-Patent 3 703 442 ist ein Verfahren dieser Art bekannt, welches der thermischen Depolymerisation bituminöser Materialien und insbesondere Ölschiefer dient. Der Ölschiefer wird hierbei mit körnigen heißen Feststoffen von etwa 630°C gemischt, wobei sich eine Mischungstemperatur von etwa 530°C einstellt. Man arbeitet bei relativ niedrigen Temperaturen, um Crackprozesse in der Gasphase zu vermeiden.A method of this type is known from US Pat. No. 3,703,442, which is used for the thermal depolymerization of bituminous materials and in particular oil shale. The oil shale is mixed with granular hot solids of around 630 ° C, resulting in a mixing temperature of around 530 ° C. One works at relatively low temperatures to avoid cracking processes in the gas phase.
Der Erfindung liegt die Aufgabe zugrunde, aus dem Einsatz-Material ein Gas mit möglichst hohem Heizwert zu gewinnen, das ganz oder weitgehend teerfrei ist und somit nur einen geringen Gehalt an kondensierbaren organischen Bestandteilen aufweist. Erfindungsgemäß wird dies beim eingangs genannten Verfahren dadurch erreicht, daß man die heißen körnigen Feststoffe mit Temperaturen im Bereich von 700 bis 1100°C aus dem Sammelbunker in den oberen Bereich des Pyrolysereaktors leitet, daß der Reaktor im oberen Bereich eine Rieselzone und unter der Rieselzone ein Wanderbett oder Wirbelbett mit Temperaturen im Bereich von 650 bis 1000°C aufweist, daß man die heißen körnigen Feststoffe und das Einsatz-Material zumindest teilweise gemeinsam abwärts durch die Rieselzone zum Wanderbett oder Wirbelbett leitet und daß man Gase und Dämpfe aus dem Wanderbett oder Wirbelbett aufwärts im Gegenstrom zu den heißen Feststoffen durch die Rieselzone führt, bevor man sie aus dem oberen Bereich des Reaktors abzieht. Die heißen körnigen Feststoffe werden nachfolgend auch als Wärmeträger-Feststoffe bezeichnet .The invention has for its object to obtain a gas with the highest possible heating value from the feed material, which is completely or largely tar-free and thus has only a low content of condensable organic constituents. According to the invention, this is achieved in the process mentioned at the outset by passing the hot granular solids at temperatures in the range from 700 to 1100 ° C. out of the collecting bunker into the upper region of the pyrolysis reactor by introducing a trickle zone in the upper region and below the trickle zone Moving bed or fluidized bed with temperatures in the range of 650 to 1000 ° C has that the hot granular solids and the feed material at least partially together down through the trickle zone to the moving bed or fluidized bed and that gases and vapors from the moving bed or fluidized bed upwards countercurrent to the hot solids through the trickle zone before being withdrawn from the top of the reactor. The hot granular solids are also referred to below as heat transfer solids.
Beim Verfahren der Erfindung gibt man dem Pyrolysereaktor hoch erhitzte Feststoffe zu, und man sorgt auch im Wanderbett oder Wirbelbett für relativ hohe Temperaturen. Dadurch werden in den Gasen und Dämpfen im Reaktor und insbesondere auch im Bereich der Rieselzone erwünschte Crackreaktionen hervorgerufen. Die aus dem Reaktor abgezogenen Gase und Dämpfe sind dadurch an Komponenten mit niederem Molgewicht angereichert, wodurch insbesondere der Anteil an Wasserstoff, Methan und kurzkettigen Olefinen hoch ist. Auf diese Weise ist es ohne weiteres möglich, ein Gas mit einem unteren Heizwert von 20 bis 25 MJ/Nm3 zu erzeugen. Gleichzeitig kann man einen Kaltgas-Wirkungsgrad von 75 bis 85 % erreichen, weil die Temperaturen im Pyrolysereaktor sehr hoch liegen. Der Kaltgas-Wirkungsgrad W errechnet sich ausIn the process of the invention, highly heated solids are added to the pyrolysis reactor, and relatively high temperatures are also ensured in the moving bed or fluidized bed. This causes the desired cracking reactions in the gases and vapors in the reactor and in particular in the trickle zone. The gases and vapors withdrawn from the reactor are thereby on Components with a low molecular weight are enriched, which means that the proportion of hydrogen, methane and short-chain olefins is particularly high. In this way it is easily possible to produce a gas with a lower calorific value of 20 to 25 MJ / Nm 3 . At the same time, a cold gas efficiency of 75 to 85% can be achieved because the temperatures in the pyrolysis reactor are very high. The cold gas efficiency W is calculated
W = (G • a) : (M • b)W = (G • a): (M • b)
dabei bedeutenmean
G = Menge des erzeugten Gases (Nm3/h) / G = amount of gas generated (Nm 3 / h) /
M = Menge des Einsatz-Materials (kg/h) , a = unterer Heizwert des erzeugten Gases (MJ/Nm3) , b = unterer Heizwert des Einsatz-Materials (MJ/kg) .M = amount of feed material (kg / h), a = lower calorific value of the gas produced (MJ / Nm 3 ), b = lower calorific value of the feed material (MJ / kg).
Als Material, das man dem Pyrolysereaktor aufgibt, kommen thermisch getrockneter Klärschlamm, Biomassen, Abfallkunststoffe oder andere organische Rückstände enthaltende Materialien verschiedenster Art mit hohem Anteil an flüchtigen Bestandteilen infrage .Thermally dried sewage sludge, biomass, waste plastics or other materials containing various organic residues with a high proportion of volatile constituents can be used as the material to be fed into the pyrolysis reactor.
Vorteilhafterweise wird das Einsatz-Material gleichzeitig durch eine oder mehrere Aufgabestellen in die Rieselzone des Pyrolysereaktors geleitet. Bei mehreren Aufgabestellen erreicht man eine Vorverteilung des eingespeisten Materials. Üblicherweise wird man das feuchte Material durch 1 bis 6 Aufgabestellen in den Reaktor leiten. Die Aufgabestellen können im oberen, mittleren oder unteren Bereich der Rieselzone münden. Zweckmäßigerweise ist der Pyrolysereaktor und insbesondere auch seine Rieselzone frei von rotierenden Mischeinrichtungen, um Verschleißprobleme möglichst auszuschließen. In der Rieselzone kann man durch ortsfeste dachartige Einbauten für ein Aufteilen und mehrfaches Umlenken der rieselnden Feststoffströme sorgen und so deren rasche Durchmischung herbeiführen.Advantageously, the feed material is passed simultaneously through one or more feed points into the trickle zone of the pyrolysis reactor. If there are several feed points, the feed material is pre-distributed. Usually, the moist material will be passed through 1 to 6 feed points into the reactor. The feed points can open in the upper, middle or lower area of the trickle zone. The pyrolysis reactor and in particular also its trickle zone are expediently free of rotating mixing devices in order to rule out wear problems as far as possible. In the trickle zone, fixed roof-like fixtures can be used to divide and redirect the trickling streams of solids several times so that they can be mixed quickly.
Für die Rieselzone empfiehlt sich eine Höhe von 1 bis 10 m, wobei man die Höhe im Einzelfall abhängig vom Einsatz-Material und den Temperaturen insbesondere in der Rieselzone festlegt. Auf diese Weise ergeben sich für die aus dem Wirbelbett oder Wanderbett aufsteigenden Gase und Dämpfe in der Rieselzone Verweilzeiten im Bereich von 0,5 bis 20 Sekunden und zumeist 1 bis 10 Sekunden. Mit steigender Temperatur nimmt die Geschwindigkeit der Crackreaktionen zu, so daß bei hohen Temperaturen mit kürzeren Verweilzeiten gearbeitet werden kann.A height of 1 to 10 m is recommended for the trickle zone, the height being determined in individual cases depending on the material used and the temperatures, in particular in the trickle zone. In this way, there are residence times in the range from 0.5 to 20 seconds and mostly 1 to 10 seconds for the gases and vapors rising from the fluidized bed or moving bed in the trickle zone. The speed of the cracking reactions increases with increasing temperature, so that shorter residence times can be used at high temperatures.
Es kann empfehlenswert sein, das Einsatz-Material von außen in den mittleren oder unteren Bereich der Rieselzone einzuspeisen, während man aber die heißen körnigen Feststoffe in den oberen Bereich der Rieselzone aufgibt. Dadurch kommen die aufsteigenden Gase und Dämpfe im oberen Bereich der Rieselzone nur mit den heißen Feststoffen in Kontakt. Bei vorgegebener Cracktemperatur kann so die nötige Verweilzeit der Gase und Dämpfe in der Rieselzone verringert werden oder aber kann die Temperatur der eingespeisten Feststoffe abgesenkt werden.It may be advisable to feed the feed material from the outside into the middle or lower area of the trickle zone, while the hot granular solids are fed into the upper area of the trickle zone. As a result, the rising gases and vapors in the upper area of the trickle zone only come into contact with the hot solids. At a given cracking temperature, the necessary residence time of the gases and vapors in the trickle zone can be reduced or the temperature of the solids fed in can be reduced.
Es kann ferner empfehlenswert sein, den Sammelbunker dafür zu nutzen, um die Temperatur der Wärmeträger-Feststoffe weiter zu erhöhen, bevor sie in den Pyrolysereaktor geleitet werden. Insbesondere durch Einleiten eines 02-haltigen Gases (z. B. Luft) in den Sammelbunker kann dort für eine Verbrennung gesorgt werden, welche die Temperaturen in erwünschter Weise erhöht.It may also be advisable to use the collection bunker to further increase the temperature of the heat transfer solids before they are fed into the pyrolysis reactor. In particular by introducing a gas containing 0 2 (e.g. air) In the collection bunker, combustion can be provided there, which increases the temperatures in the desired manner.
Ausgestaltungsmöglichkeiten des Verfahrens werden mit Hilfe der Zeichnung erläutert . Es zeigt :Design options of the method are explained with the aid of the drawing. It shows :
Fig. 1 ein Fließschema des Verfahrens undFig. 1 is a flow diagram of the method and
Fig. 2 eine Variante des Pyrolysereaktors im Längsschnitt.Fig. 2 shows a variant of the pyrolysis reactor in longitudinal section.
Gemäß Fig. 1 führt man dem Pyrolysereaktor (1) durch die Leitung1 leads the pyrolysis reactor (1) through the line
(2) das zu behandelnde Einsatz -Material und durch die Leitung(2) the insert material to be treated and through the line
(3) heiße körnige Feststoffe als Wärmeträger zu. Die Leitung (2) verzweigt sich vor Eintritt in den Reaktor (1) auf mehrere Aufgabestellen (2a) und (2b) . Im oberen Bereich des Reaktors (1) befindet sich die Rieselzone (la) , darunter bildet das Feststoffgemisch (4) ein Wanderbett oder Wirbelbett. Wenn man dem Reaktor (1) in den unteren Bereich ein Sichtungsgas, z. B. Stickstoff oder Wasserdampf, durch die gestrichelt eingezeichnete Leitung (5) zuführt, kann man die(3) hot granular solids as heat transfer medium. The line (2) branches before entering the reactor (1) to several feed points (2a) and (2b). In the upper area of the reactor (1) is the trickle zone (la), below which the solid mixture (4) forms a moving bed or fluidized bed. If you have a reactor gas, e.g. B. nitrogen or steam, through the dashed line (5) supplies, you can
Feststoffschüttung soweit auflockern, daß zumindest teilweise ein Wirbelbett gebildet wird. Ohne ein solches Sichtungsgas bildet das Feststoffgemisch (4) eine Schüttung, die sich als Wanderbett langsam nach unten bewegt, weil ständig Feststoffe durch die Leitung (6) abgezogen werden.Loosen the solid bed so far that a fluidized bed is at least partially formed. Without such a sighting gas, the solid mixture (4) forms a bed, which slowly moves downwards as a moving bed, because solids are continuously drawn off through the line (6).
Bereits in der Rieselzone (la) werden die mit Temperaturen von 700 bis 1100°C durch die Leitung (3) herangeführten heißen Feststoffe zumindest teilweise mit dem Einsatz-Material durchmischt. Zu diesem Zweck weist die Rieselzone ortsfeste Umlenkeinrichtungen in Form mehrerer dachartiger Einbauten (8) auf. Auf eine rotierende Mischvorrichtung wird hierbei verzichtet .Already in the trickle zone (la), the hot solids brought in through line (3) at temperatures of 700 to 1100 ° C. are at least partially mixed with the feed material. For this purpose, the trickle zone has stationary deflection devices in the form of several roof-like internals (8) on. A rotating mixing device is not used.
Die sich durch die Rieselzone (la) abwärts bewegenden heißen Wärmeträger-Feststoffe kommen intensiv in Kontakt mit dem sich ebenfalls abwärts bewegenden Einsatz-Material, das dabei erhitzt und einer Entgasung unterzogen wird. Gleichzeitig strömen Gase und Dämpfe aufwärts durch die Rieselzone (la) , die während der Erhitzung gebildet werden. Die Gase und Dämpfe werden durch die Leitung (9) zu einem Zyklonabscheider (10) geführt, wo man mitgeführte Feststoffe weitgehend abtrennt. Die Feststoffe können durch die Leitung (11) zumindest teilweise in den Reaktor (1) zurückgeführt werden, einen Teil kann man durch die Leitung (12) aus dem Verfahren entfernen. Die den Zyklonabscheider (10) durch die Leitung (15) verlassenden Gase und Dämpfe werden einer an sich bekannten Gasreinigung (16) aufgegeben, wobei auch eine Kühlung stattfindet. Gereinigte Gase und Dämpfe ziehen zur weiteren Verwendung, z. B. als Brenngas, in der Leitung (17) ab.The hot heat transfer solids moving down through the trickle zone (la) come into intensive contact with the feed material, which also moves downwards, which is heated and subjected to degassing. At the same time, gases and vapors flow upwards through the trickle zone (la), which are formed during the heating. The gases and vapors are passed through line (9) to a cyclone separator (10), where the entrained solids are largely separated. The solids can at least partially be returned to the reactor (1) through line (11), and part can be removed from the process through line (12). The gases and vapors leaving the cyclone separator (10) through line (15) are fed to a gas cleaning system (16) known per se, cooling also taking place. Purified gases and vapors are drawn for further use, e.g. B. as fuel gas in line (17).
Das in der Leitung (6) aus dem Reaktor (1) abgezogene heiße Feststoffgemisch kann teilweise durch die Leitung (7) aus dem Verfahren entfernt werden. Die übrigen Feststoffe werden zum Fuß einer pneumatischen Förderstrecke (20) geführt, der man durch die Leitung (21) Heißluft zuführt. Die Heißluft fördert die Feststoffe nach oben, wobei gleichzeitig brennbare Substanzen verbrannt werden, was zur Erhitzung der Feststoffe führt. Das Gemisch aus Feststoffen und Gasen gelangt in einen Sammelbunker (22), Gase werden durch die Leitung (23) abgezogen, durch einen Zyklonabscheider (24) geführt und in der Leitung (25) einer nicht dargestellten Abgasreinigung zugeführt. Abgeschiedene Feststoffe können in der Leitung (26) entfernt oder durch die Leitung (26a) zurück in den Sammelbunker (22) geführt werden.The hot solid mixture drawn off from the reactor (1) in line (6) can be partially removed from the process through line (7). The remaining solids are fed to the bottom of a pneumatic conveyor line (20), to which hot air is fed through line (21). The hot air conveys the solids upwards, at the same time burning combustible substances, which leads to the heating of the solids. The mixture of solids and gases reaches a collection bunker (22), gases are drawn off through line (23), passed through a cyclone separator (24) and fed to a waste gas cleaning system (not shown) in line (25). Secluded Solids can be removed in line (26) or fed back through line (26a) into the collection bunker (22).
Die sich im unteren Bereich des Bunkers (22) sammelnden heißen körnigen Feststoffe weisen Temperaturen von 700 bis 1100°C auf. Wenn diese Temperaturen nicht bereits in der pneumatischen Förderstrecke (20) erreicht werden, kann man durch die Leitung (28) dem Bunker (22) ein 02-haltiges Gas (z. B. Luft) zuführen und die Temperaturen im Bunker durch Nachverbrennung erhöhen. Die Gaszufuhr durch die Leitung (28) kann ferner auch dazu genutzt werden, um durch Sichten staubfeine Feststoffe zu entfernen, wobei man diese Stäube durch die Leitung (23) zum Abscheider (24) führt und sie durch die Leitung (26) aus dem Kreislauf entfernt.The hot granular solids that collect in the lower area of the bunker (22) have temperatures of 700 to 1100 ° C. If these temperatures are not already reached in the pneumatic conveyor section (20), a gas containing 0 2 (e.g. air) can be supplied to the bunker (22) through the line (28) and the temperatures in the bunker increased by post-combustion . The gas supply through line (28) can also be used to remove dust-fine solids by sifting these dusts through line (23) to separator (24) and through line (26) from the circuit away.
Fig. 2 zeigt eine modifizierte Ausführungsform des Pyrolysereaktors (1) mit Gegenstromführung der heißen Wärmeträger-Feststoffe und der gebildeten Gase und Dämpfe oberhalb der Einmündungen der Leitungen (2a) und (2b) , durch die das Einsatz-Material zugeführt wird. Die Wärmeträger-Feststoffe kommen aus der Leitung (3) ; die übrigen Bezugsziffern haben die bereits zusammen mit der Fig. 1 erläuterte Bedeutung.Fig. 2 shows a modified embodiment of the pyrolysis reactor (1) with countercurrent flow of the hot heat transfer solids and the gases and vapors formed above the mouths of the lines (2a) and (2b) through which the feed material is fed. The heat transfer solids come from line (3); the other reference numerals have the meaning already explained together with FIG. 1.
Beispiel :For example:
Einem Pyrolysereaktor (1) , wie er in Fig. 2 dargestellt ist, werden pro Stunde 5 t getrockneter Klärschlamm mit einer Restfeuchte von 7 Gew.-% durch Leitung (2) zugeführt. Der Klärschlamm besteht zu 63 Gew.-% aus flüchtigen Bestandteilen, er hat einen unteren Heizwert von 17,0 MJ/kg. Dem Reaktor (1) führt man 80 t/h heiße Wärmeträger-Feststoffe mit 900 °C durch die Leitung (3) zu. Hierdurch entstehen 2920 Nm3/h, 850 °C heißes Pyrolysegas mit einem unteren Heizwert von 23,3 MJ/Nm3 welches durch Leitung (9) abgeführt, im Zyklon (10) entstaubt und dann der Gasreinigung (16) zugeführt wird. Aus dem Pyrolysereaktor zieht man 81 t/h auf 750°C gekühlte Feststoffe durch Leitung (6) ab. Nach Ausschleusung des überschüssigen Rückstandes (1 t/h) durch Leitung (7) wird der Wärmeträger-Feststoff in die pneumatische Förderstrecke (20) dosiert und dort mit vorgeheizter Verbrennungsluft durch Leitung (21) in den Sammelbunker (22) gefördert, wobei durch Abbrand von Restkoks aus dem Wärmeträger-Feststoff dieser auf 900°C rückerhitzt wird. Er wird dann bei dieser Temperatur im Sammelbunker (22) und Zyklon (24) von den Abgasen getrennt und dosiert dem Reaktor (1) wieder zugeführt. A pyrolysis reactor (1), as shown in Fig. 2, 5 t of dried sewage sludge with a residual moisture content of 7 wt .-% are fed through line (2) per hour. The sewage sludge consists of 63% by weight of volatile components, it has a lower calorific value of 17.0 MJ / kg. The reactor (1) is carried out at 80 t / h hot heat transfer solids at 900 ° C the line (3). This produces 2920 Nm 3 / h, 850 ° C hot pyrolysis gas with a lower calorific value of 23.3 MJ / Nm 3 which is discharged through line (9), dedusted in the cyclone (10) and then fed to gas cleaning (16). From the pyrolysis reactor, 81 t / h of solids cooled to 750 ° C. are drawn off through line (6). After the excess residue (1 t / h) has been discharged through line (7), the heat transfer solid is metered into the pneumatic conveying section (20) and is conveyed there with preheated combustion air through line (21) into the collecting bunker (22), with combustion of residual coke from the heat transfer solid which is reheated to 900 ° C. It is then separated from the exhaust gases at this temperature in the collecting bunker (22) and cyclone (24) and metered back to the reactor (1).

Claims

Patentansprüche claims
1. Verfahren zum thermischen Behandeln von flüchtige, brennbare Bestandteile enthaltendem Einsatz-Material mit einem Wassergehalt von bis zu 20 Gew.-%, wobei man das Einsatz-Material mit heißen körnigen Feststoffen, die aus einem Sammelbunker kommen, in einem Pyrolysereaktor mischt, aus dem Reaktor Gase und Dämpfe abzieht und im Reaktor ein Feststoffgemisch erzeugt, welches man aus dem Reaktor abführt, wobei man mindestens einen Teil davon außerhalb des Reaktors erhitzt und über den Sammelbunker in den Pyrolysereaktor zurückführt, dadurch gekennzeichnet, daß man die heißen körnigen Feststoffe mit Temperaturen im Bereich von 700 bis 1100°C aus dem Sammelbunker in den oberen Bereich des Pyrolysereaktors leitet, daß der Reaktor im oberen Bereich eine Rieselzone und unter der Rieselzone ein Wanderbett oder Wirbelbett mit Temperaturen im Bereich von 650 bis 1000°C aufweist, daß man die heißen körnigen Feststoffe und das Einsatz-Material zumindest teilweise gemeinsam abwärts durch die Rieselzone zum Wanderbett oder Wirbelbett leitet und daß man Gase und Dämpfe aus dem Wanderbett oder Wirbelbett aufwärts im Gegenstrom zu den heißen Feststoffen durch die Rieselzone führt, bevor man sie aus dem oberen Bereich des Reaktors abzieht.1. A method for the thermal treatment of volatile, combustible feed material with a water content of up to 20% by weight, the feed material being mixed with hot granular solids coming from a collection bunker in a pyrolysis reactor withdrawing gases and vapors from the reactor and generating a solid mixture in the reactor which is removed from the reactor, at least a portion of which is heated outside the reactor and returned to the pyrolysis reactor via the collecting bunker, characterized in that the hot granular solids are at temperatures in the range of 700 to 1100 ° C from the collecting bunker in the upper area of the pyrolysis reactor that the reactor has a trickle zone in the upper area and a moving bed or fluidized bed with temperatures in the range of 650 to 1000 ° C under the trickle zone that the are called granular solids and the insert material at least partially together ts leads through the trickle zone to the moving bed or fluidized bed and that gases and vapors from the moving bed or fluidized bed are led upwards in countercurrent to the hot solids through the trickle zone before they are withdrawn from the upper region of the reactor.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Einsatz-Material Klärschlamm, Biomasse, Abfallkunststoffe oder andere organische Rückstände enthaltende Materialien in den Pyrolysereaktor geleitet werden. 2. The method according to claim 1, characterized in that sewage sludge, biomass, waste plastics or other materials containing organic residues are passed as feed material into the pyrolysis reactor.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Einsatz-Material gleichzeitig durch mehrere Aufgabestellen in die Rieselzone des Pyrolysereaktors geleitet wird.3. The method according to claim 1, characterized in that the feed material is passed simultaneously through several feed points into the trickle zone of the pyrolysis reactor.
4. Verfahren nach Anspruch 1 oder einem der folgenden, dadurch gekennzeichnet, daß die Rieselzone eine Höhe von 1 bis 10 m aufweist .4. The method according to claim 1 or one of the following, characterized in that the trickle zone has a height of 1 to 10 m.
5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß das Einsatz-Material zumindest teilweise in den unteren Bereich der Rieselzone eingeleitet wird.5. The method according to any one of claims 1 to 4, characterized in that the insert material is at least partially introduced into the lower region of the trickle zone.
6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die heißen Feststoffe im Sammelbunker durch Verbrennung nacherhitzt werden.6. The method according to any one of claims 1 to 5, characterized in that the hot solids in the collection bunker are reheated by combustion.
7. Verfahren nach Anspruch 1 oder einem der folgenden, dadurch gekennzeichnet, daß in den unteren Bereich des Pyrolysereaktors ein Sichtungs- oder Strippgas eingeleitet wird.7. The method according to claim 1 or one of the following, characterized in that a sighting or stripping gas is introduced into the lower region of the pyrolysis reactor.
8. Verfahren nach Anspruch 1 oder einem der folgenden, dadurch gekennzeichnet, daß der Pyrolysereaktor frei von rotierenden Mischeinrichtungen ist.8. The method according to claim 1 or one of the following, characterized in that the pyrolysis reactor is free of rotating mixing devices.
9. Verfahren nach Anspruch 1 oder einem der folgenden, dadurch gekennzeichnet, daß die Verweilzeit der Gase und Dämpfe im Pyrolysereaktor 0,5 bis 20 Sekunden beträgt. 9. The method according to claim 1 or one of the following, characterized in that the residence time of the gases and vapors in the pyrolysis reactor is 0.5 to 20 seconds.
EP98945153A 1997-09-01 1998-08-06 Method for thermal treatment of material containing volatile, combustible constituents Expired - Lifetime EP1015527B1 (en)

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PCT/EP1998/004889 WO1999011736A1 (en) 1997-09-01 1998-08-06 Method for thermal treatment of material containing volatile, combustible constituents

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