EP2686406A1 - Moving bed reactor - Google Patents

Moving bed reactor

Info

Publication number
EP2686406A1
EP2686406A1 EP12713874.1A EP12713874A EP2686406A1 EP 2686406 A1 EP2686406 A1 EP 2686406A1 EP 12713874 A EP12713874 A EP 12713874A EP 2686406 A1 EP2686406 A1 EP 2686406A1
Authority
EP
European Patent Office
Prior art keywords
bulk material
reactor
moving bed
column
bed reactor
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Withdrawn
Application number
EP12713874.1A
Other languages
German (de)
French (fr)
Inventor
Thomas Stump
Leonhard Baumann
Roland Möller
Gunter Ulbrich
Thomas Von Beoeczy
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.)
Ecoloop GmbH
Original Assignee
Ecoloop 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
Application filed by Ecoloop GmbH filed Critical Ecoloop GmbH
Publication of EP2686406A1 publication Critical patent/EP2686406A1/en
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/002—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor with a moving instrument
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0035—Periodical feeding or evacuation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0045—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a rotary device in the flow channel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00539—Pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/0061—Controlling the level
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00761—Discharging
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00769—Details of feeding or discharging
    • B01J2208/00778—Kinetic energy reducing devices in the flow channel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime

Definitions

  • the present invention is concerned with a device for the thermal decomposition of carbon-rich substances in a moving through a bulk material from top to bottom moving bed reactor wherein a vertical bulk material column is provided for the supply of material streams.
  • Such a device is for example from the
  • the object of the present invention is to improve a device of the type described above in such a way that a safe operation with a reliably sealed inside of the reactor and setting Favor ter pressure conditions is possible.
  • this object is achieved in that egg egg ner device of the type mentioned also for the removal of material flows a vertical column of bulk material is seen, and the widths and heights of the bulk material columns and the nature of the bulk material are selected such that the bulk solids columns on the one hand her inner Pressure loss cause a seal of the interior of the reactor from the atmosphere, and on the other hand allow a continuous or batchwise bulk flow, wherein in the upper reactor region, a first cavity and in the lower reactor region, a second cavity is provided, between which a pressure difference ⁇ of at least 50 mbar is provided by the pressure loss over the bed is stabilized.
  • the system has a high availability and manages without disruptive fittings in the supply and discharge.
  • the plant is particularly suitable for the production of synthesis gas, which can be collected in the upper cavity of the reactor and discharged by suitable devices.
  • the vertical bulk solids columns allow, in conjunction with the vertical moving bed, a bulk material movement solely on the basis of its own gravity of the bulk material, without the moving elements must be provided to ensure the bulk material flow.
  • the device is designed such that the vertical bulk material column for the supply of the material streams is communicatively connected to the bulk material column of the moving bed reactor.
  • This embodiment is particularly preferred in continu ⁇ ous material flows, as are avoided by the bulk handling without chutes into the reactor chamber discontinuous movement.
  • a further preferred embodiment of the invention provides that the vertical bulk material column for the removal of the material streams is separated by the cavity formed in the lower part of the reactor in front of the bulk material moving bed of the reactor itself. Such a design has proved to be advantageous in order to avoid blockages of the reactor and thus an interruption of the material flows by juxtaposed bulk material parts.
  • the formation of the cavity in the lower part of the reactor can be carried out, for example, by a bulk material metering device which meters the bulk material from the moving bed reactor continuously or batchwise into the formed cavity.
  • a bulk material metering device which meters the bulk material from the moving bed reactor continuously or batchwise into the formed cavity.
  • turntable or sliding table devices can be used, for example, which are known, for example, from the calcining shaft furnace construction.
  • the bulk material below the cavity in the lower part of the reactor communicating with the vertical bulk material column for the removal of material flows is connected.
  • a mixing device is provided which mixes the bulk material with the carbon-rich substances, so that it
  • Transport medium for the carbon-rich substances in the moving bed reactor is used. In this way, by selective adjustment of the carbon content under favorable conditions operation of the reactor without additional fuel supply can be achieved.
  • a cooling device which cools the pipe jacket of the vertical bulk material column for the supply completely or partially indirectly with a cooling medium.
  • This cooling medium may be water in the simplest case, although embodiments are conceivable in which the water is not conducted in a circuit, but then flows into the interior of the reactor.
  • the cooling of the tubular jacket prevents easily melting in the bulk material column due to possibly higher temperatures prevailing in this area.
  • the tube jacket of the bulk material column for the feed can also be wholly or partially immersed in the upper part of the moving bed of the reactor and thereby form the upper cavity in the upper part of the moving bed reactor.
  • the mean operating pressure in the moving bed reactor is preferably below 3 bar (g), preferably below 1 bar (g) and more preferably in an area below
  • the bulk vertical feed column is a quotient of its bulk height (in meters) divided by the maximum pressure differential (in bar) in the reactor head to the prevailing atmospheric pressure (in bar) of> 10 and the vertical bulk material column for discharge has a quotient of its bulk material height (in m) divided by the maximum pressure difference of the operating pressure (in bar) at the reactor bottom to the prevailing atmospheric pressure (in bar) of> 5.
  • the different quotients result from the fact that the nature of the bulk material changes due to the oxidized carbon constituents.
  • the initially set pressure difference of at least 50 mbar is preferably below 1 bar, since higher pressure differences are generally not expedient for safe operation.
  • constituents of calcium oxide, carbonate and / or hydroxide as constituents, especially as they have halogen-containing plastics which have positive properties to bind the halogens and to withdraw from the process.
  • halogen-containing plastics which have positive properties to bind the halogens and to withdraw from the process.
  • catalytic effect of calcium compounds, in particular of calcium oxide in the thermal cleavage is particularly advantageous.
  • the method can be coupled with the production of quicklime, so that the device can be operated economically.
  • the embodiment shows a calcining shaft furnace, as used industrially in, for example, firing or sintering processes, in a modified embodiment, which is used as a moving bed reactor 1.
  • the moving bed reactor 1 is continuously charged with a mixture of carbon-rich substances 2 and refractory bulk material 3.
  • the feed takes place via a conveying device 4 and a vertical bulk material column 5, the bed of which is communicatively connected to the bed 6 in the moving bed reactor.
  • the flow of the bulk material 6 in the moving bed reactor 1 is carried out by gravity from top to bottom by the bulk material metering 7, the bed of the moving bed reactor 1 continuously or batchwise passes into a cavity 8, which is arranged at the lower end of the moving bed reactor 1.
  • the bed slips continuously downward, as a result of which mixtures of carbon-rich substances 2 and refractory bulk material 3 can also slip over the bulk material column 5 into the moving bed reactor.
  • the moving bed reactor is operated as a so-called countercurrent gasifier, in which oxygen-containing gas 9 is introduced at the bottom of the reactor bottom.
  • At least the following three process zones are formed by the gasification process: in the upper part of the bed 6, a pyrolysis zone A in which the carbonaceous substances already partially react or cooke, later on a hotter burning zone B, in which the remaining carbon compounds in Synthesis gases are converted and in the lower part of a cooling zone C.
  • the originating in the process zones A and B The synthesis gas leaving the moving bed reactor at the head at 10.
  • the bulk material column 5 for the supply of bulk material is formed in the example as a dip tube, which dips into the upper part of the moving bed reactor.
  • the immersion depth of the dip tube can be targeted to the height of the bulk material 6 in the reactor and in particular to the volume of the resulting gas space 11 influence.
  • the area of the tubular jacket of the bulk material column immersed in the reactor is cooled by means of water via a double wall 12 or a cooling coil system. This makes it possible, even at low temperatures melting carbon-rich substances such. As plastics, easy to process in the system without it could lead to sticking.
  • the use of expensive fittings or lock systems for the supply to the moving bed reactor 1 can be omitted.
  • the bulk material column 13 is at the lower outlet directly communicating on a discharge device 14, which consists for example of a vibrating trough or a discharge belt. With this discharge device 14, the bulk material Good column 13 withdrawn continuously or batchwise from the reactor system.
  • a discharge device 14 which consists for example of a vibrating trough or a discharge belt.
  • the control of the reactor is carried out by the rate of oxidizable mixture and the proportion of carbon-rich substances. This control can be done on the one hand in the mixing device 4, but on the other hand alone by the throughput of the metering device 7 above the cavity 8, which controls the flow rate of the bulk material in the reactor.
  • a secure sealing of the interior of the reactor from the atmosphere must also be guaranteed at all times. This is necessary, on the one hand, in order to prevent the escape of synthesis gas and, on the other hand, in order to exclude the penetration of atmospheric oxygen and the formation of an explosive mixture in the interior of the reactor in the event of a negative pressure. This sealing takes place via the pressure loss of the two bulk material columns for the supply and discharge.
  • the bulk material column 5 for the material supply is therefore equipped with a level measuring device 15, which acts as a control variable on the speed of the conveyor 4 for the material supply to the bulk material column 5 and always ensures a minimum level.
  • the guarantee of a minimum fill level in the bulk material column 13 for the removal of material also takes place via a fill level measuring device 16.
  • This can optionally be controlled by a control 17 as a control variable D to the discharge speed of the metering device 7 or alternatively as a control device.
  • large E act on the speed of the discharge device 14.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

The apparatus serves to thermally separate carbon-rich substances in a moving bed reactor (1) through which a bulk material (6) passes. A vertical bulk material column (5) for supplying the material is supplemented by a bulk material column for removing material, wherein the widths and heights of the bulk material columns (5, 13) and the composition of the bulk material (6) are selected in such a manner that sealing of the interior of the reactor is brought about by an internal pressure loss in the columns (5, 13). At the same time, a stream of bulk material is made possible, wherein a first cavity (11) is provided in the upper reactor region and a second cavity (9) is provided in the lower reactor region, between which cavities a differential pressure Δρ of at least 50 mbar is provided, said differential pressure being stabilized by the pressure loss via the fill.

Description

Wanderbettreaktor  Moving bed reactor
Die vorliegende Erfindung befasst sich mit einer Vorrichtung zur thermischen Spaltung von kohlenstoffreichen Substanzen in einem mit einem Schüttgut von oben nach unten durchströmten Wanderbettreaktor wobei für die Zufuhr von Materialströmen eine vertikale Schüttgutsäule vorgesehen ist. The present invention is concerned with a device for the thermal decomposition of carbon-rich substances in a moving through a bulk material from top to bottom moving bed reactor wherein a vertical bulk material column is provided for the supply of material streams.
Eine derartige Vorrichtung ist beispielsweise aus der Such a device is for example from the
DE 10 2007 062 414 AI bekannt. Schwierigkeiten können beim Betreiben einer solchen Vorrichtung entstehen, wenn bestimmte Druckverhältnisse im Inneren des Reaktors eingestellt werden müssen, um einerseits stabile chemische Reaktionen zu bewirken ggf. andererseits den Gegenstrom an Gasen im Reaktor zu fördern . DE 10 2007 062 414 AI known. Difficulties can arise when operating such a device when certain pressure conditions must be set inside the reactor, on the one hand to cause stable chemical reactions, on the other hand, to promote the countercurrent of gases in the reactor.
Die thermische Verwertung von kohlenstoffreichen Substanzen, insbesondere die Vergasung von kunststoffhaltigen Abfällen, kontaminierten Kohlenstoffträgern oder auch Biomassen ist seit vielen Jahren von großem Interesse. Insbesondere für die Realisierung der Vergasung von kunststoffhaltigeri Abfällen wurden in der Vergangenheit große Anstrengungen unternommen. Zahlreiche Verfahren wurden in den großtechnischen Maßstab überführt, wobei unterschiedliche Reaktortypen zum Einsatz gekommen waren, wie beispielsweise Drehrohrreaktoren, Wirbelschichtreaktoren oder auch Wanderbettreaktoren. The thermal utilization of carbon-rich substances, in particular the gasification of waste containing plastic, contaminated carbon carriers or biomass has been of great interest for many years. In particular, great efforts have been made in the past to realize the gasification of plastic-containing wastes. Numerous processes have been commercialized using different types of reactors, such as rotary tube reactors, fluidized bed reactors or moving bed reactors.
Die bekannten Vorrichtungen und Verfahren besaßen erhebliche Nachteile, die in nahezu allen Fällen wieder zur Einstellung dieser Großprojekte führten. Insbesondere handelte es sich um Probleme im Bereich der KunststoffZuführung in den Reaktor The known devices and methods had considerable disadvantages, which led in almost all cases again to the setting of these major projects. In particular, these were problems in the field of plastic feed into the reactor
BESTÄTIGUNGSKOPIE sowie der Abführung der Reststoffe. Auch die Durchströmung des Reaktors sowie die Aufrechterhaltung eines kontinuierlichen Gegenstromes eines gasförmigen Mediums waren problematisch . CONFIRMATION COPY and the removal of the residues. The flow through the reactor and the maintenance of a continuous countercurrent of a gaseous medium were problematic.
Für die Zufuhr und Abfuhr der Ausgangs- und Reststoffe wurde zumeist aufwendige Schnecken-/ Schleusen- oder auch Stempelvorrichtungen eingesetzt, die üblicherweise komplexe konstruktive Merkmale, wie beispielsweise drehende Teile, Klapp mechanismen sowie statische oder dynamische Abdichtungssyste me aufwiesen. Insbesondere beim Einsatz von niedrig schmelzenden Materialien, wie beispielsweise Kunststoffen, traten bei diesen Vorrichtungen massive Probleme durch Anschmelzun- gen, Anbackungen und Verstopfungen auf. Dadurch kommt es zu Stillstandszeiten der Anlage, da die Zu- und Abführvorrichtungen häufig gereinigt werden mussten oder es zu Undichtigkeiten gegenüber dem Reaktorinneren kam. Die damit verbundenen Schwankungen der Druckverhältnisse oder gar der Austritt Undefinierter Gasgemische sind besonders nachteilig. For the supply and removal of the starting materials and residues mostly complicated screw / lock or punch devices was used, which usually had complex design features, such as rotating parts, folding mechanisms and static or dynamic Abdichtungssyste me. In particular, when using low-melting materials, such as plastics, occurred in these devices massive problems by Anschmelzun- gene, caking and clogging. This leads to downtimes of the plant, since the supply and discharge devices had to be cleaned frequently or there were leaks in relation to the interior of the reactor. The associated fluctuations in the pressure conditions or even the discharge of undefined gas mixtures are particularly disadvantageous.
Die Aufgabe der vorliegenden Erfindung besteht darin, eine Vorrichtung der eingangs beschriebenen Art dahingehend zu verbessern, dass ein sicherer Betriebsablauf mit einem zuver lässig abgedichteten Reaktorinneren und Einstellung bevorzug ter Druckverhältnisse möglich ist. The object of the present invention is to improve a device of the type described above in such a way that a safe operation with a reliably sealed inside of the reactor and setting Favor ter pressure conditions is possible.
Erfindungsgemäß wird die Aufgabe dadurch gelöst, dass bei ei ner Vorrichtung der eingangs genannten Art auch für die Abfuhr von Materialströmen eine vertikale Schüttgutsäule vorge sehen ist, und die Breiten und Höhen der Schüttgutsäulen sowie die Beschaffenheit des Schüttgutes derart gewählt sind, dass die Schüttgutsäulen einerseits durch ihren inneren Druckverlust eine Abdichtung des Reaktorinneren von der Atmosphäre bewirken, und andererseits einen kontinuierlichen oder batchweisen Schüttgutstrom ermöglichen, wobei im oberen Reaktorbereich ein erster Hohlraum und im unteren Reaktorbereich ein zweiter Hohlraum vorgesehen ist, zwischen denen eine Druckdifferenz Δρ von wenigstens 50 mbar vorgesehen ist, die durch den Druckverlust über die Schüttung stabilisiert ist. According to the invention this object is achieved in that egg egg ner device of the type mentioned also for the removal of material flows a vertical column of bulk material is seen, and the widths and heights of the bulk material columns and the nature of the bulk material are selected such that the bulk solids columns on the one hand her inner Pressure loss cause a seal of the interior of the reactor from the atmosphere, and on the other hand allow a continuous or batchwise bulk flow, wherein in the upper reactor region, a first cavity and in the lower reactor region, a second cavity is provided, between which a pressure difference Δρ of at least 50 mbar is provided by the pressure loss over the bed is stabilized.
Es hat sich gezeigt, dass mit einer solchen Vorrichtung koh- lenstoffreiche Substanzen thermisch verwertet werden können, wobei die Anlage eine hohe Verfügbarkeit besitzt und ohne störungsfällig Armaturen im Zuführ- und Abführbereich auskommt. Die Anlage eignet sich insbesondere für die Herstellung von Synthesegas, wobei dieses im oberen Hohlraum des Reaktors gesammelt und durch geeignete Vorrichtungen abgeführt werden kann. It has been found that with such a device carbon-rich substances can be thermally utilized, the system has a high availability and manages without disruptive fittings in the supply and discharge. The plant is particularly suitable for the production of synthesis gas, which can be collected in the upper cavity of the reactor and discharged by suitable devices.
Die vertikalen Schüttgutsäulen erlauben in Verbindung mit dem vertikalen Wanderbett eine Schüttgutbewegung ausschließlich auf Grund der eigenen Schwerkraft des Schüttgutes, ohne das bewegte Elemente vorgesehen sein müssen, um den Schüttgutstrom sicher zu stellen. The vertical bulk solids columns allow, in conjunction with the vertical moving bed, a bulk material movement solely on the basis of its own gravity of the bulk material, without the moving elements must be provided to ensure the bulk material flow.
Vorzugsweise ist die Vorrichtung derart ausgebildet, dass die vertikale Schüttgutsäule für die Zufuhr der Materialströme kommunizierend mit der Schüttgutsäule des Wanderbettreaktors verbunden ist. Diese Ausführungsform ist besonders bei konti¬ nuierlichen Materialströmen bevorzugt, da durch die Schüttgutförderung ohne Fallstrecken in den Reaktorraum diskontinuierliche Bewegungsabläufe vermieden werden. Eine weitere bevorzugte Ausführungsform der Erfindung sieht vor, dass die vertikale Schüttgutsäule für die Abfuhr der Materialströme durch den im unteren Teil des Reaktors ausgebildeten Hohlraum vor dem Schüttgutwanderbett des Reaktors selbst getrennt ist. Eine derartige Ausbildung hat sich als vorteilhaft erwiesen, um Verstopfungen des Reaktors und damit eine Unterbrechung der Materialströme durch aneinanderheftende Schüttgutteile zu vermeiden. Preferably, the device is designed such that the vertical bulk material column for the supply of the material streams is communicatively connected to the bulk material column of the moving bed reactor. This embodiment is particularly preferred in continu ¬ ous material flows, as are avoided by the bulk handling without chutes into the reactor chamber discontinuous movement. A further preferred embodiment of the invention provides that the vertical bulk material column for the removal of the material streams is separated by the cavity formed in the lower part of the reactor in front of the bulk material moving bed of the reactor itself. Such a design has proved to be advantageous in order to avoid blockages of the reactor and thus an interruption of the material flows by juxtaposed bulk material parts.
Die Ausbildung des Hohlraums im unteren Teil des Reaktors kann beispielsweise durch eine Schüttgutdosiereinrichtung erfolgen, die das Schüttgut aus dem Wanderbettreaktor kontinuierlich oder batchweise in den ausgebildeten Hohlraum dosiert. Als Schüttgutdosiereinrichtungen können beispielsweise Drehteller- oder Schubtischvorrichtungen eingesetzt werden, die beispielsweise aus dem Kalzinierschachtofenbau bekannt sind . The formation of the cavity in the lower part of the reactor can be carried out, for example, by a bulk material metering device which meters the bulk material from the moving bed reactor continuously or batchwise into the formed cavity. As bulk material metering devices, turntable or sliding table devices can be used, for example, which are known, for example, from the calcining shaft furnace construction.
In einer weiteren bevorzugten Ausführungsform der Erfindung ist vorgesehen, dass das Schüttgut unterhalb des Hohlraums im unteren Teil des Reaktors kommunizierend mit der vertikalen Schüttgutsäule für die Abfuhr der Materialströme verbunden ist . In a further preferred embodiment of the invention, it is provided that the bulk material below the cavity in the lower part of the reactor communicating with the vertical bulk material column for the removal of material flows is connected.
In einer noch weiter bevorzugten Ausführungsform ist vorgesehen, dass oberhalb des Eintrittes des Schüttgutes in die vertikale Schüttgutsäule für die Zufuhr der Materialströme eine Mischvorrichtung vorgesehen ist, die das Schüttgut mit den kohlenstoffreichen Substanzen vermischt, so dass es als In a still further preferred embodiment it is provided that above the entrance of the bulk material in the vertical bulk material column for the supply of material flows, a mixing device is provided which mixes the bulk material with the carbon-rich substances, so that it
Transportmedium für die kohlenstoffreichen Substanzen in den Wanderbettreaktor dient. Auf diese Weise kann durch gezieltes Einstellen des Kohlenstoffanteils unter günstigen Bedingungen ein Betrieb des Reaktors ohne zusätzliche Brennstoffzufuhr erreicht werden. Transport medium for the carbon-rich substances in the moving bed reactor is used. In this way, by selective adjustment of the carbon content under favorable conditions operation of the reactor without additional fuel supply can be achieved.
In einer besonders bevorzugten Ausführungsform der Erfindung ist eine Kühlvorrichtung vorgesehen, die den Rohrmantel der vertikalen Schüttgutsäule für die Zufuhr ganz oder teilweise indirekt mit einem Kühlmedium kühlt. Dieses Kühlmedium kann im einfachsten Fall Wasser sein, wobei auch Ausführungsformen denkbar sind, bei welchen das Wasser nicht in einem Kreislauf geführt wird, sondern dann in das Reaktorinnere fließt. In a particularly preferred embodiment of the invention, a cooling device is provided which cools the pipe jacket of the vertical bulk material column for the supply completely or partially indirectly with a cooling medium. This cooling medium may be water in the simplest case, although embodiments are conceivable in which the water is not conducted in a circuit, but then flows into the interior of the reactor.
Die Kühlung des Rohrmantels verhindert, dass durch in diesem Bereich möglicherweise vorherrschende höhere Temperaturen leicht aufschmelzende Kunststoffe in der Schüttgutsäule miteinander verbacken können. The cooling of the tubular jacket prevents easily melting in the bulk material column due to possibly higher temperatures prevailing in this area.
Der Rohrmantel der Schüttgutsäule für die Zufuhr kann auch ganz oder teilweise in den oberen Teil des Wanderbettes des Reaktors eintauchen und dadurch den oberen Hohlraum im oberen Teil des Wanderbettreaktors ausbilden. The tube jacket of the bulk material column for the feed can also be wholly or partially immersed in the upper part of the moving bed of the reactor and thereby form the upper cavity in the upper part of the moving bed reactor.
Der mittlere Betriebsdruck im Wanderbettreaktor liegt vorzugsweise unterhalb 3 bar (ü) vorzugsweise unterhalb 1 bar (ü) und besonders bevorzugt in einem Bereich unterhalb The mean operating pressure in the moving bed reactor is preferably below 3 bar (g), preferably below 1 bar (g) and more preferably in an area below
0, 1 bar (ü) . 0, 1 bar (g).
Ein Beispiel für eine Geometrie der Schüttgutsäulen, die sich im Betrieb als wirkungsvoll erwiesen hat, sieht vor, dass die vertikale Schüttgutsäule für die Zufuhr einen Quotienten gebildet aus ihrer Schüttguthöhe (in m) geteilt durch die maximale Druckdifferenz des Betriebsdruckes (in bar) im Reaktorkopf zum herrschenden Atmosphärendruck (in bar) von >10 auf- weist und die vertikale Schüttgutsäule für die Abfuhr einen Quotienten gebildet aus ihrer Schüttguthöhe (in m) geteilt durch die maximale Druckdifferenz des Betriebsdrucks (in bar) am Reaktorboden zum herrschenden Atmosphärendruck (in bar) von >5 aufweist. Die unterschiedlichen Quotienten resultieren daraus, dass sich die Beschaffenheit des Schüttgutes durch die oxidierten Kohlenstoffbestandteile ändert. An example of geometry of bulk solids columns that has proven to be effective in operation provides that the bulk vertical feed column is a quotient of its bulk height (in meters) divided by the maximum pressure differential (in bar) in the reactor head to the prevailing atmospheric pressure (in bar) of> 10 and the vertical bulk material column for discharge has a quotient of its bulk material height (in m) divided by the maximum pressure difference of the operating pressure (in bar) at the reactor bottom to the prevailing atmospheric pressure (in bar) of> 5. The different quotients result from the fact that the nature of the bulk material changes due to the oxidized carbon constituents.
Die eingangs genannte eingestellte Druckdifferenz von wenigstens 50 mbar liegt vorzugsweise unterhalb 1 bar, da höhere Druckdifferenzen für einen sicheren Betriebsablauf in der Regel nicht zweckdienlich sind. The initially set pressure difference of at least 50 mbar is preferably below 1 bar, since higher pressure differences are generally not expedient for safe operation.
Vorteilhaft wird mit Schüttungen aus Kalziumoxid, -carbonat und/oder -hydroxid als Bestandteile gearbeitet, zumal diese bei halogenhaltigen Kunststoffen, die positive Eigenschaften haben, die Halogene zu binden und dem Prozess zu entziehen. Besonders vorteilhaft ist dabei die katalytische Wirkung der Kalziumverbindungen, insbesondere von Kalziumoxid bei der thermischen Spaltung. Das Verfahren kann mit der Herstellung von Branntkalk gekoppelt werden, so dass sich die Vorrichtung wirtschaftlich betreiben lässt. It is advantageous to work with constituents of calcium oxide, carbonate and / or hydroxide as constituents, especially as they have halogen-containing plastics which have positive properties to bind the halogens and to withdraw from the process. Particularly advantageous is the catalytic effect of calcium compounds, in particular of calcium oxide in the thermal cleavage. The method can be coupled with the production of quicklime, so that the device can be operated economically.
Hinsichtlich des Spaltungsvorganges selbst hat es sich als vorteilhaft erwiesen, wenn das Gesamt-Λ der Oxidationsprozes- se in dem Wanderbettreaktor über alle Stufen kleiner 0,5 ist. Insgesamt erfolgt also die Oxidation unter Sauerstoffmangel, wobei der Λ-Wert weiter abgesenkt werden kann und auch gute Ergebnisse in einem Bereich mit einem Λ von 0,3 erzielt worden sind. Eine Ausführungsform der vorliegenden Erfindung ist in der beigefügten Abbildung gezeigt. Die Ausführungsform zeigt einen Kalzinierschachtofen, wie er beispielsweise in Brennoder Sinterprozessen großtechnisch zum Einsatz kommt, in modifizierter Ausführungsform, der als Wanderbettreaktor 1 eingesetzt wird. Der Wanderbettreaktor 1 wird mit einem Gemisch aus kohlenstoffreichen Substanzen 2 und feuerfestem Schüttgut 3 kontinuierlich beschickt. Die Beschickung erfolgt über eine Fördervorrichtung 4 und eine vertikale Schüttgutsäule 5, deren Schüttung kommunizierend mit der Schüttung 6 in dem Wanderbettreaktor verbunden ist. Die Strömung des Schüttgutes 6 im Wanderbettreaktor 1 erfolgt durch Schwerkraftwirkung von oben nach unten, indem die Schüttgut-Dosiervorrichtung 7 die Schüttung aus dem Wanderbettreaktor 1 kontinuierlich oder batchweise in einen Hohlraum 8 weitergibt, der am unteren Ende des Wanderbettreaktors 1 angeordnet ist. Durch diese Entnahme rutscht die Schüttung kontinuierlich nach unten, wodurch auch Gemische aus kohlenstoffreichen Substanzen 2 und feuerfestem Schüttgut 3 über die Schüttgutsäule 5 in den Wanderbettreaktor nachrutschen kann. With regard to the cleavage process itself, it has proved to be advantageous if the total Λ of the oxidation processes in the moving bed reactor over all stages is less than 0.5. Overall, therefore, the oxidation takes place under oxygen deficiency, the Λ value can be further lowered and good results have been achieved in a range with a Λ of 0.3. An embodiment of the present invention is shown in the accompanying drawing. The embodiment shows a calcining shaft furnace, as used industrially in, for example, firing or sintering processes, in a modified embodiment, which is used as a moving bed reactor 1. The moving bed reactor 1 is continuously charged with a mixture of carbon-rich substances 2 and refractory bulk material 3. The feed takes place via a conveying device 4 and a vertical bulk material column 5, the bed of which is communicatively connected to the bed 6 in the moving bed reactor. The flow of the bulk material 6 in the moving bed reactor 1 is carried out by gravity from top to bottom by the bulk material metering 7, the bed of the moving bed reactor 1 continuously or batchwise passes into a cavity 8, which is arranged at the lower end of the moving bed reactor 1. As a result of this removal, the bed slips continuously downward, as a result of which mixtures of carbon-rich substances 2 and refractory bulk material 3 can also slip over the bulk material column 5 into the moving bed reactor.
Der Wanderbettreaktor wird als sogenannter Gegenstromvergaser betrieben, in dem sauerstoffhaltiges Gas 9 unten am Reaktorboden aufgegeben wird. Durch den Vergasungsprozess bilden sich dabei mindestens die folgenden drei Prozesszonen aus: im oberen Teil der Schüttung 6 eine Pyrolysezone A, in welcher die kohlenstoffhaltigen Substanzen bereits teilweise reagieren oder verkoken, im weiteren Verlauf nach unten eine heißere Brennzone B, in welcher die restlichen KohlenstoffVerbindungen in Synthesegase umgewandelt werden, sowie im unteren Teil eine Kühlzone C. Das in den Prozesszonen A und B entste- hende Synthesegas verlässt den Wanderbettreaktor am Kopf bei 10. The moving bed reactor is operated as a so-called countercurrent gasifier, in which oxygen-containing gas 9 is introduced at the bottom of the reactor bottom. At least the following three process zones are formed by the gasification process: in the upper part of the bed 6, a pyrolysis zone A in which the carbonaceous substances already partially react or cooke, later on a hotter burning zone B, in which the remaining carbon compounds in Synthesis gases are converted and in the lower part of a cooling zone C. The originating in the process zones A and B The synthesis gas leaving the moving bed reactor at the head at 10.
Die Schüttgutsäule 5 für die Zufuhr von Schüttgut ist im Beispielsfall als Tauchrohr ausgebildet, das in den oberen Teil des Wanderbettreaktors eintaucht. Mit der Wahl der Eintauchtiefe des Tauchrohres kann gezielt auf die Höhe des Schüttgutes 6 im Reaktor und insbesondere auf das Volumen des dadurch entstehenden Gasraumes 11 Einfluss genommen werden. The bulk material column 5 for the supply of bulk material is formed in the example as a dip tube, which dips into the upper part of the moving bed reactor. With the choice of the immersion depth of the dip tube can be targeted to the height of the bulk material 6 in the reactor and in particular to the volume of the resulting gas space 11 influence.
Da sich im Gasraum 11 im oberen Bereich des Reaktors Temperaturen von oberhalb 300°C ausbilden können, ist bei dem gezeigten Ausführungsbeispiel der in den Reaktor eingetauchte Bereich des Rohrmantels der Schüttgutsäule 5 mittels Wasser über eine doppelt ausgeführte Wandung 12 oder ein Kühlschlangensystem gekühlt. Dadurch ist es möglich, auch bei niedrigen Temperaturen aufschmelzende kohlenstoffreiche Substanzen, wie z. B. Kunststoffe, problemlos in dem System zu verarbeiten, ohne dass es zu Verklebungen kommen könnte. Die Verwendung aufwendiger Armaturen oder Schleusensysteme für die Zufuhr zu dem Wanderbettreaktor 1 kann entfallen. Since temperatures of above 300 ° C. can form in the upper region of the reactor in the gas space 11, in the exemplary embodiment shown, the area of the tubular jacket of the bulk material column immersed in the reactor is cooled by means of water via a double wall 12 or a cooling coil system. This makes it possible, even at low temperatures melting carbon-rich substances such. As plastics, easy to process in the system without it could lead to sticking. The use of expensive fittings or lock systems for the supply to the moving bed reactor 1 can be omitted.
Das im Hohlraum 8 vorhandene Gemisch aus feuerfestem Schüttgut 3 und thermisch nicht verwertbaren Reststoffen, wie z. B. Asche, ist kommunizierend mit der Schüttgutsäule 13 für die Abfuhr des Materials aus dem Reaktorsystem verbunden. The present in the cavity 8 mixture of refractory bulk material 3 and thermally unusable residues such. As ash, is communicatively connected to the bulk material column 13 for the removal of the material from the reactor system.
Die Schüttgutsäule 13 steht am unteren Auslauf direkt kommunizierend auf einer Abfördervorrichtung 14, die beispielsweise aus einer Vibrationsrinne oder aus einem Abzugsband besteht. Mit dieser Abfördervorrichtung 14 wird die Schütt- gutsäule 13 kontinuierlich oder batchweise aus dem Reaktorsystem abgezogen. The bulk material column 13 is at the lower outlet directly communicating on a discharge device 14, which consists for example of a vibrating trough or a discharge belt. With this discharge device 14, the bulk material Good column 13 withdrawn continuously or batchwise from the reactor system.
Die Steuerung des Reaktors erfolgt durch den Durchsatz an oxidationsfähigem Gemisch und dem Anteil an kohlenstoffreichen Substanzen. Diese Steuerung kann zum einen im Bereich der Mischvorrichtung 4 vorgenommen werden, zum anderen aber auch alleine durch den Durchsatz der Dosiervorrichtung 7 oberhalb des Hohlraumes 8, die die Durchsatzgeschwindigkeit des Schüttgutes in dem Reaktor steuert. Um den Prozess der thermischen Verwertung sicher betreiben zu können, muss auch zu jedem Zeitpunkt eine sichere Abdichtung des Reaktorinnenraums gegenüber der Atmosphäre gewährleistet sein. Dies ist zum einen erforderlich, um das Austreten von Synthesegas zu verhindern, und zum anderen, um im Falle eines Unterdruckes das Eindringen von Luftsauerstoff und die Ausbildung eines explosionsfähigen Gemisches im Reaktorinnenraum auszuschließen. Diese Abdichtung erfolgt über den Druckverlust der beiden Schüttgutsäulen für die Zu- und Abführung. Daher ist sicherzustellen, dass beide Schüttgutsäulen zu jedem Zeitpunkt und in jedem Betriebszustand eine Mindestfüllhöhe aufweisen. Die Schüttgutsäule 5 für die Materialzufuhr ist daher mit einer Füllstandsmessvorrichtung 15 ausgestattet, die als Steuergröße auf die Drehzahl der Fördervorrichtung 4 für die Materialzufuhr in die Schüttgutsäule 5 wirkt und stets einen Mindestfüllstand sicherstellt. The control of the reactor is carried out by the rate of oxidizable mixture and the proportion of carbon-rich substances. This control can be done on the one hand in the mixing device 4, but on the other hand alone by the throughput of the metering device 7 above the cavity 8, which controls the flow rate of the bulk material in the reactor. In order to be able to operate the process of thermal utilization safely, a secure sealing of the interior of the reactor from the atmosphere must also be guaranteed at all times. This is necessary, on the one hand, in order to prevent the escape of synthesis gas and, on the other hand, in order to exclude the penetration of atmospheric oxygen and the formation of an explosive mixture in the interior of the reactor in the event of a negative pressure. This sealing takes place via the pressure loss of the two bulk material columns for the supply and discharge. It must therefore be ensured that both bulk material columns have a minimum filling level at all times and in every operating condition. The bulk material column 5 for the material supply is therefore equipped with a level measuring device 15, which acts as a control variable on the speed of the conveyor 4 for the material supply to the bulk material column 5 and always ensures a minimum level.
Die Gewährleistung eines Mindestfüllstandes in der Schüttgutsäule 13 für die Materialabführung erfolgt ebenfalls über eine Füllstandsmessvorrichtung 16. Diese kann wahlweise über eine Regelung 17 als Steuergröße D auf die Austragsgeschwin- digkeit der Dosiervorrichtung 7 oder alternativ als Steuer- große E auf die Drehzahl der Abfördervorrichtung 14 wirken. Die getrennten Steuerkreise für die Schüttgutsäulen stellen sicher, dass auch bei Unstetigkeiten im Schüttgutstrom innerhalb des Reaktors immer eine ausreichende Schüttgutsäulenhöhe in der Zufuhr und in der Abfuhr erhalten bleibt. The guarantee of a minimum fill level in the bulk material column 13 for the removal of material also takes place via a fill level measuring device 16. This can optionally be controlled by a control 17 as a control variable D to the discharge speed of the metering device 7 or alternatively as a control device. large E act on the speed of the discharge device 14. The separate control circuits for the bulk material columns ensure that even with discontinuities in the bulk flow within the reactor, a sufficient bulk material column height is always maintained in the feed and in the discharge.

Claims

Patentansprüche claims
1. Vorrichtung zur thermischen Spaltung von kohlenstoffreichen Substanzen in einem mit einem Schüttgut von oben nach unten durchströmten Wanderbettreaktor (1), wobei für die Zufuhr von Materialströmen eine vertikale Schüttgutsäule (5) vorgesehen ist, dadurch gekennzeichnet, dass für die Abfuhr von Materialströmen aus dem Wanderbettreaktor (1) eine vertikale Schüttgutsäule (13) vorgesehen, und die Breiten und Höhen der Schüttgutsäulen (5, 13) sowie die Beschaffenheit des Schüttgutes derart gewählt sind, dass die Schüttgutsäulen (5, 13) einerseits durch ihren inneren Druckverlust eine Abdichtung des Reaktorinneren von der Atmosphäre bewirken und andererseits einen kontinuierlichen oder batchweisen Schüttgutstrom ermöglichen, wobei im oberen Reaktorbereich ein erster Hohlraum (11) und im unteren Reaktorbereich ein zweiter Hohlraum (9) vorgesehen ist, zwischen denen eine Druckdifferenz Δρ von wenigstens 50 mbar vorgesehen ist, die durch den Druckverlust über das Schüttgut (6) innerhalb des Wanderbettreaktors (1) stabilisiert ist. 1. Apparatus for the thermal cleavage of carbon-rich substances in a with a bulk material from top to bottom through the moving bed reactor (1), wherein for the supply of material flows a vertical bulk material column (5) is provided, characterized in that for the removal of material flows from the Wanderbettreaktor (1) provided a vertical bulk material column (13), and the widths and heights of the bulk material columns (5, 13) and the nature of the bulk material are chosen such that the bulk material columns (5, 13) on the one hand by their internal pressure loss sealing the interior of the reactor effect of the atmosphere and on the other hand allow a continuous or batchwise bulk flow, wherein in the upper reactor region, a first cavity (11) and in the lower reactor region, a second cavity (9) is provided, between which a pressure difference Δρ of at least 50 mbar is provided by the pressure loss over the Sch ttgut (6) is stabilized within the moving bed reactor (1).
2. Vorrichtung nach Anspruch 1, dadurch gekennzeichnet, dass die vertikale Schüttgutsäule (5) für die Zufuhr der Mate- rialströme kommunizierend mit der Schüttung (6) des Wanderbettreaktors (1) verbunden ist. 2. Apparatus according to claim 1, characterized in that the vertical bulk material column (5) for the supply of mate- rialströme communicating with the bed (6) of the moving bed reactor (1) is connected.
3. Vorrichtung nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass die vertikale Schüttgutsäule (13) für die Abfuhr der Materialströme durch den im unteren Teil des Reaktors ausgebildeten Hohlraum (9) von dem Schüttgut (6) des Wanderbetts des Wanderbettreaktors (1) selbst getrennt ist. 3. Apparatus according to claim 1 or 2, characterized in that the vertical bulk material column (13) for the removal of material flows through the formed in the lower part of the reactor cavity (9) of the bulk material (6) the moving bed of the moving bed reactor (1) itself is separated.
4. Vorrichtung nach Anspruch 3, dadurch gekennzeichnet, dass die Ausbildung des Hohlraums (9) im unteren Teil des Reaktors (1) durch eine Schüttgutdosiereinrichtung (7) erfolgt, die das Schüttgut (6) aus dem Wanderbettreaktor (1) kontinuierlich oder batchweise in den ausgebildeten Hohlraum dosiert. 4. The device according to claim 3, characterized in that the formation of the cavity (9) in the lower part of the reactor (1) by a bulk material metering device (7), the bulk material (6) from the moving bed reactor (1) continuously or batchwise in dosed the formed cavity.
5. Vorrichtung nach Anspruch 4, dadurch gekennzeichnet, dass die Schüttgutdosiereinrichtung (7) als Drehteller- oder Schubtischvorrichtung ausgebildet ist. 5. Apparatus according to claim 4, characterized in that the bulk material metering device (7) is designed as a turntable or push table device.
6. Vorrichtung nach einem der Ansprüche 3 bis 5, dadurch gekennzeichnet, dass das Schüttgut unterhalb des Hohlraums (9) im unteren Teil des Reaktors (1) kommunizierend mit der vertikalen Schüttgutsäule (13) für die Abfuhr der Materialströme verbunden ist. 6. Device according to one of claims 3 to 5, characterized in that the bulk material below the cavity (9) in the lower part of the reactor (1) communicating with the vertical bulk material column (13) is connected for the removal of material flows.
7. Vorrichtung nach einem der vorhergehenden Ansprüche, 7. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass oberhalb des Eintrittes des Schüttgutes in die vertikale Schüttgutsäule (5) für die Zufuhr der Materialströme eine Fördervorrichtung (4) vorgesehen ist, die das Schüttgut mit den kohlenstoffreichen Substanzen vermischt, so dass es als Transportmedium für die kohlenstoffreichen Substanzen in den Wanderbettreaktor (1) dient.  characterized in that above the entrance of the bulk material in the vertical bulk material column (5) for the supply of material streams, a conveyor (4) is provided which mixes the bulk material with the carbon-rich substances, so that it as a transport medium for the carbon-rich substances in the moving bed reactor (1) serves.
8. Vorrichtung nach einem der vorhergehenden Ansprüche, 8. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass eine Kühlvorrichtung (12) vorgesehen ist, die einen Rohrmantel der vertikalen  characterized in that a cooling device (12) is provided which has a pipe jacket of the vertical
Schüttgutsäule (5) für die Zufuhr ganz oder teilweise indirekt mit einem Kühlmedium kühlt. Bulk column (5) for the supply cools all or part indirectly with a cooling medium.
9. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, dass der Rohrmantel der vertikalen Schüttgutsäule (5) für die Zufuhr ganz oder teilweise in den oberen Teil des Wanderbettreaktors (1) eintaucht und dadurch den oberen Hohlraum (11) im oberen Teil des Wanderbettreaktors (1) ausbildet . 9. Apparatus according to claim 8, characterized in that the tube jacket of the vertical bulk material column (5) for the supply completely or partially immersed in the upper part of the moving bed reactor (1) and thereby the upper cavity (11) in the upper part of the moving bed reactor (1 ) trains.
10. Vorrichtung nach einem der vorhergehenden Ansprüche, 10. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass der mittlere Betriebsdruck im Wanderbettreaktor unterhalb 3 bar (ü) , vorzugsweise unterhalb 1 bar (ü) und insbesondere bevorzugt in einem Bereich unterhalb 0,1 bar (ü) eingestellt ist.  characterized in that the average operating pressure in the moving bed reactor below 3 bar (ü), preferably below 1 bar (ü) and more preferably in a range below 0.1 bar (ü) is set.
11. Vorrichtung nach einem der vorhergehenden Ansprüche, 11. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass die vertikale Schüttgutsäule characterized in that the vertical column of bulk material
(5) für die Zufuhr einen Quotienten gebildet aus ihrer Schüttguthöhe (in Metern) geteilt durch die maximale Druckdifferenz des Betriebsdruckes (in Bar) im Reaktorkopf zum herrschenden Atmosphärendruck (in Bar) von >10 aufweist und die vertikale Schüttgutsäule (13) für die Abfuhr einen Quotienten gebildet aus ihrer Schüttguthöhe(5) for the feed a quotient formed from its bulk height (in meters) divided by the maximum pressure difference of the operating pressure (in bar) in the reactor head to the prevailing atmospheric pressure (in bar) of> 10 and the vertical bulk material column (13) for the discharge a quotient formed from their bulk height
(in Metern) geteilt durch die maximale Druckdifferenz des Betriebsdruckes (in Bar) am Reaktorboden zum herrschenden Atmosphärendruck (in Bar) von >5 aufweist. (in meters) divided by the maximum pressure difference of the operating pressure (in bar) at the reactor bottom to the prevailing atmospheric pressure (in bar) of> 5.
12. Vorrichtung nach einem der vorhergehenden Ansprüche, 12. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass Δρ maximal 1 bar beträgt.  characterized in that Δρ is at most 1 bar.
13. Vorrichtung nach einem der vorhergehenden Ansprüche, 13. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass die Schüttung Kalziumoxid, -carbonat und /oder -hydroxidanteile enthält.  characterized in that the bed contains calcium oxide, carbonate and / or hydroxide.
14. Vorrichtung nach einem der vorhergehenden Ansprüche, 14. Device according to one of the preceding claims,
dadurch gekennzeichnet, dass das Gesamt-Λ des Oxidations- Prozesses in dem Wanderbettreaktor (1) über alle Stufen kleiner 0,5 ist. characterized in that the total Λ of the oxidation Process in the moving bed reactor (1) over all stages is less than 0.5.
Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die Steuerung des thermischen Spaltvorganges durch die Variation des Durchsatzes an Schüttgut (6) und kohlenstoffreichen Substanzen und/oder der Mengenanteile an zugegebenen kohlenstoffrei chen Substanzen erfolgt. Device according to one of the preceding claims, characterized in that the control of the thermal splitting process by the variation of the throughput of bulk material (6) and carbon-rich substances and / or the proportions of added carbon-free chen substances takes place.
EP12713874.1A 2011-03-18 2012-03-16 Moving bed reactor Withdrawn EP2686406A1 (en)

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US20140127090A1 (en) 2014-05-08
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DE102011014349A1 (en) 2012-09-20
AU2012231048A1 (en) 2013-10-31
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CN103534339B (en) 2016-04-06
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AU2012231048B2 (en) 2015-09-03
CA2835611A1 (en) 2012-09-27

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