EP0090148B1 - Procédé et appareil pour la destruction thermique des substances organiques et minérales - Google Patents

Procédé et appareil pour la destruction thermique des substances organiques et minérales Download PDF

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Publication number
EP0090148B1
EP0090148B1 EP83101052A EP83101052A EP0090148B1 EP 0090148 B1 EP0090148 B1 EP 0090148B1 EP 83101052 A EP83101052 A EP 83101052A EP 83101052 A EP83101052 A EP 83101052A EP 0090148 B1 EP0090148 B1 EP 0090148B1
Authority
EP
European Patent Office
Prior art keywords
reactor
filling material
helices
wall
angle
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.)
Expired
Application number
EP83101052A
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German (de)
English (en)
Other versions
EP0090148A2 (fr
EP0090148A3 (en
Inventor
Heinrich Dipl.-Ing. Bastian
Hans Dr. Dipl. Chem. Huschka
Gerhard Dr. Dipl. Chem. Kemmler
Elmar Dr. Dipl.-Ing. Schlich
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.)
Nukem GmbH
Original Assignee
Nukem 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 Nukem GmbH filed Critical Nukem GmbH
Publication of EP0090148A2 publication Critical patent/EP0090148A2/fr
Publication of EP0090148A3 publication Critical patent/EP0090148A3/de
Application granted granted Critical
Publication of EP0090148B1 publication Critical patent/EP0090148B1/fr
Expired legal-status Critical Current

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Classifications

    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/04—Treating liquids
    • G21F9/06—Processing
    • G21F9/14—Processing by incineration; by calcination, e.g. desiccation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/11—Stirrers characterised by the configuration of the stirrers
    • B01F27/114—Helically shaped stirrers, i.e. stirrers comprising a helically shaped band or helically shaped band sections
    • B01F27/1142—Helically shaped stirrers, i.e. stirrers comprising a helically shaped band or helically shaped band sections of the corkscrew type
    • G—PHYSICS
    • G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
    • G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
    • G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
    • G21F9/28—Treating solids
    • G21F9/30—Processing
    • G21F9/32—Processing by incineration

Definitions

  • the invention relates to a method for the thermal decomposition and conversion of organic and inorganic substances in a bed consisting of mechanically moving packing elements, which is located in a heated, upright cylindrical reactor, and an apparatus for carrying out the method.
  • Nuclear technology produces a number of solid and liquid organic and inorganic wastes, which are mostly radioactive or otherwise highly toxic and must be disposed of safely. This is normally eliminated by incineration or pyrolytic decomposition, taking into account numerous safety requirements, such as exhaust gas treatment, ease of repair and operational safety of the systems used.
  • DE-A 26 41 264 describes a method and a device for the pyrohydrolytic decomposition of waste materials, the reaction taking place at temperatures between 600 and 1000 ° C.
  • this process has the disadvantage that the different decomposition processes of liquid and solid substances result in different thermal loads, which lead to different hot and cold spots in the reactor.
  • the decomposition reaction also takes place at different speeds, depending on the position in the reactor of the reaction mixture. Since the dwell time is determined by the metering capacity and the volume of the reactor, locally different decomposition efficiencies arise, which overall increase the proportion of higher hydrocarbons (tar, soot) in the exhaust gas.
  • the corrosion can only be controlled to a very limited extent, since the decomposition products can only be incompletely bound by admixed basic additives Ca (OH) 2 . This is mainly due to the fact that the quality of mixing of the liquid substance to be decomposed with the existing solid organic waste and the basic additive present in solid form is very low.
  • DE-A 30 28 193 describes a process for the pyrolytic decomposition of organic substances in a reactor, these substances mixed with basic compounds being introduced into a fixed-bed reactor, the spherical packing of which is mechanically moved. The reactor is heated from the outside.
  • the packing is moved by means of a stirrer so that it does not cake together due to the decomposition products deposited.
  • a stirrer so that it does not cake together due to the decomposition products deposited.
  • the integral thermal conductivity of the packed bed is generally no longer sufficient to prevent breakdown of undecomposed waste products in the middle of the furnace.
  • the packing is moved in a special circulation within the reactor by targeted stirring of the packed bed.
  • energy is transported uniformly inwards from the outer wall of the reactor and, on the other hand, a build-up of substances foreign to the filler on the filler and on the inside of the reactor is avoided.
  • a relatively coarse-grained dust is formed as a solid reaction product, which is discharged with the exhaust gas.
  • the exhaust gas is then dedusted in a known manner.
  • the process according to the invention prevents different thermal loads on the reactor as well as decomposition reactions taking place at different speeds.
  • the amount of exhaust gas is only determined by the minimum necessary purge gas flow, e.g. Nitrogen, enlarged.
  • the method according to the invention is largely insensitive to overdosing and underdosing. Temporary overdoses are no problem, stoichiometric mixtures of the substances to be decomposed with additives only have to be correct over longer periods of time.
  • a device consisting of a heated, upright cylindrical reactor with a bed of packing and a stirrer consisting of a stirrer shaft, support arms and one or more helices, the helix being between 10 and 45 °, which Form helices with the wall of the reactor at an angle ⁇ between 45 and 85 °, the support arms, as seen in the direction of rotation, are inclined forward and downward by an angle y between 5 and 45 ° and the width of the helixes and support arms is greater than the filler body diameter or hydraulic diameter of the packing.
  • the pitch of the spirals (2) is between 20 and 30 °
  • the spirals (2) form an angle y between 85 and 75 ° with the wall (7) of the reactor and the support arms (9) around one Angle y are inclined between 15 and 25 °.
  • the spirals (2) are at least single-thread, as well as if the distance between the outer edge (8) of the spirals (2) and the wall (7) is at most 75% of the diameter of the smallest packing. This also applies to the distance of the lowest support arm (9) from the bottom (10) of the reactor, which should be at most 75% of the diameter of the smallest packing.
  • the front edge (5) of the support arm (9) is designed in the shape of a scoop or wedge.
  • the device according to the invention works best when the packed bed (4) in the reactor has a height to width ratio of between 0.75 and 1.5, with a height to width ratio of the packed bed (4) for the Packing movement is particularly advantageous.
  • the stirrer is expediently made of a metallic material which is harder than the packing and is resistant to corrosion and high temperatures.
  • two or more helices (2) can also be arranged on the stirrer axis (8). Due to the defined pitch of the filaments (2) and the defined angle of attack of the filaments (2) and support arms (9), a directional packing movement is generated on the reactor wall (7) and inside the reactor. However, this also results in a directed flow from the outside in or vice versa in the upper and lower packing layers, which significantly increases the heat flow density from the outside heating to the inside of the reactor.
  • reaction processes and mass transport mechanisms are thereby accelerated, so that reactor diameters of 0.5 to 1.5 m can be used, which allow specific throughputs of 10 to 100 kg of waste substances per hour, without causing breakthroughs in the interior of the reactor.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • High Energy & Nuclear Physics (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
  • Processing Of Solid Wastes (AREA)

Claims (10)

1- Procédé pour la décomposition thermique et la transformation de substances organiques et minérales, dans un lit constitué de corps de garnissage déplacés mécaniquement, et placé dans un réacteur cylindrique vertical, chauffé, caractérisé en ce que les corps de garnissage (4) sont guidés le long de la paroi du réacteur (7) dans le sens axial, et sont ramenés en sens contraire dans le centre du réacteur.
2- Procédé pour la décomposition thermique suivant la revendication 1, caractérisé en ce que les corps de garnissage (4) sont guidés de bas en haut sur la paroi du réacteur (7).
3- Dispositif pour la décomposition thermique et la transformation de substances organiques et minérales, constitué d'un réacteur cylindrique, vertical, chauffé, contenant un lit de corps de garnissage et un agitateur monté sur un axe d'agitateur, des bras porteurs et une ou plusieurs spires hélicoïdales, caractérisé en ce que l'inclinaison des spires est comprise entre 10 et 45°, les spirales (2) forment avec la paroi (7) du réacteur un angle y compris entre 45 et 85 ° si l'on regarde dans la direction de la rotation, les parties avant des bras porteurs (9) sont inclinées vers le bas, d'un angle y compris entre 5 et 45°, et la largeur des spires (2) et des bras porteurs (9) est supérieure au diamètre des corps de remplissage ou au diamètre hydraulique de ces corps.
4- Dispositif suivant les revendications 1 à 3, caractérisé en ce que l'inclinaison des spires hélicoïdales (2) est comprise entre 20 et 30°, les spires (2) forment, avec la paroi (7) du réacteur, un angle compris y entre 65 et 75°, et les bras porteurs (9) sont inclinés d'um angle y compris entre 15 et 25°.
5- Dispositif suivant les revendications 1 à 4, caractérisé en ce que les spires (2) forment au moins un pas.
6- Dispositif suivant la revendications 1 à 5, caractérisé en ce que la distance entre l'arête extérieure (6) des spires (2) et la paroi (7) du réacteur est au maximum égale à 75% du diamètre des plus petits des corps de remplissage.
7- Dispositif suivant les revendications 1 à 6, caractérisé en ce que la distance entre le bras porteur (9) inférieur et le fond (10) du réacteur est au maximum égale à 75% du diamètre des plus petits des corps de garnissage.
8- Dispositif suivant la revendication 1 à 7, caractérisé en ce que l'arête avant (5) des bras porteurs (9) est réalisée en forme d'aube ou de coin.
9- Dispositif suivant les revendications 1 à 8, caractérisé en ce que le rapport entre la hauteur et la largeur de la masse des corps de garnissage (4) dans le réacteur se situe entre 0,75 et 1,5.
10- Dispositif suivant les revendications 1 à 9, caractérisé en ce que le rapport hauteur/largeur est compris entre 0,9 et 1,1.
EP83101052A 1982-02-17 1983-02-04 Procédé et appareil pour la destruction thermique des substances organiques et minérales Expired EP0090148B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3205569 1982-02-17
DE3205569A DE3205569C2 (de) 1982-02-17 1982-02-17 Verfahren und Vorrichtung zur thermischen Zersetzung von organischen und anorganischen Substanzen

Publications (3)

Publication Number Publication Date
EP0090148A2 EP0090148A2 (fr) 1983-10-05
EP0090148A3 EP0090148A3 (en) 1984-06-13
EP0090148B1 true EP0090148B1 (fr) 1986-07-23

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP83101052A Expired EP0090148B1 (fr) 1982-02-17 1983-02-04 Procédé et appareil pour la destruction thermique des substances organiques et minérales

Country Status (5)

Country Link
EP (1) EP0090148B1 (fr)
JP (2) JPS58156340A (fr)
CA (1) CA1190383A (fr)
DE (2) DE3205569C2 (fr)
ES (2) ES519130A0 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4609430A (en) * 1984-03-07 1986-09-02 Ngk Insulators, Ltd. Liquid material drying apparatus
DE3918718C2 (de) * 1989-06-08 1994-02-17 Nukem Gmbh Vorrichtung zur thermischen Behandlung von organischen und anorganischen Stoffen
AU2002240707B2 (en) * 2001-03-22 2005-12-15 Srl Performance Limited Liquid phase reactor
AUPR391401A0 (en) * 2001-03-22 2001-04-12 Ceramic Fuel Cells Limited Liquid phase reactor

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1218265B (de) * 1962-08-01 1966-06-02 Basf Ag Wendelruehrer
DE1607776A1 (de) * 1967-11-29 1970-07-09 Kranz Gmbh Karl Vorrichtung zum Mischen pulverfoermiger Stoffe
DE2714812A1 (de) * 1977-04-02 1978-10-12 Basf Ag Vorrichtung zur durchfuehrung von polymerisationen aus der gasphase

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE646182C (de) * 1935-07-04 1937-06-10 Hermann Niggemann Dr Verfahren und Vorrichtung zum Schwelen von bituminoesen Brennstoffen
DE1061299B (de) * 1958-04-30 1959-07-16 Bayer Ag Reduktionsofen zur Herstellung pulverfoermiger Hydrierungskatalysatoren
US3380721A (en) * 1965-07-09 1968-04-30 Zd Normal Ussr Conveyor furnace for heat-treatment of parts
JPS5230539A (en) * 1975-09-02 1977-03-08 Koji Ihara Pachinko (pinball game) island using square iron pipe as pole
JPS56128592A (en) * 1980-03-12 1981-10-08 Doryokuro Kakunenryo Method and device for heating with microwave
DE3028193C2 (de) * 1980-07-25 1984-11-22 Nukem Gmbh, 6450 Hanau Verfahren und Vorrichtung zur pyrolytischen Zersetzung von Halogene und/oder Phosphor enthaltenden organischen Substanzen

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1218265B (de) * 1962-08-01 1966-06-02 Basf Ag Wendelruehrer
DE1607776A1 (de) * 1967-11-29 1970-07-09 Kranz Gmbh Karl Vorrichtung zum Mischen pulverfoermiger Stoffe
DE2714812A1 (de) * 1977-04-02 1978-10-12 Basf Ag Vorrichtung zur durchfuehrung von polymerisationen aus der gasphase

Also Published As

Publication number Publication date
DE3364576D1 (en) 1986-08-28
ES284567U (es) 1985-09-16
ES284567Y (es) 1986-05-01
JPH04122639U (ja) 1992-11-04
JPS58156340A (ja) 1983-09-17
ES8403154A1 (es) 1984-03-01
JPH0523216Y2 (fr) 1993-06-15
CA1190383A (fr) 1985-07-16
DE3205569C2 (de) 1983-12-15
DE3205569A1 (de) 1983-09-08
EP0090148A2 (fr) 1983-10-05
ES519130A0 (es) 1984-03-01
EP0090148A3 (en) 1984-06-13

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