EP1015527A1 - Procede de traitement thermique d'une matiere contenant des constituants combustibles volatiles - Google Patents

Procede de traitement thermique d'une matiere contenant des constituants combustibles volatiles

Info

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)
English (en)
Other versions
EP1015527B1 (fr
Inventor
Hans-Jürgen WEISS
Udo Zentner
Jörg SCHMALFELD
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.)
MG Technologies AG
Original Assignee
Metallgesellschaft AG
MG Technologies AG
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 Metallgesellschaft AG, MG Technologies AG filed Critical Metallgesellschaft AG
Publication of EP1015527A1 publication Critical patent/EP1015527A1/fr
Application granted granted Critical
Publication of EP1015527B1 publication Critical patent/EP1015527B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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

L'invention concerne une charge contenant des constituants combustibles volatiles, pouvant avoir une teneur en eau de 20 % en poids maximum. Cette charge est mélangée à des solides granuleux chauds dans un réacteur de pyrolyse. Les solides chauds sortent d'un réservoir collecteur à des températures comprises entre 700 et 1100 DEG C et sont acheminés jusqu'à la partie supérieure du réacteur de pyrolyse. Le réacteur présente dans sa partie supérieure une zone d'écoulement et, sous cette dernière, un lit mobile ou un lit fluidisé dont la température est comprise entre 650 et 1000 DEG C. Les solides granuleux chauds et la charge sont acheminés de façon descendante, au moins partiellement ensemble, par la zone d'écoulement jusqu'au lit mobile ou lit fluidisé. Les gaz et vapeurs remontent, passant par la zone d'écoulement à contre-courant des solides chauds, et sont soutirés de la zone supérieure du réacteur. Un mélange de solides est retiré de la base du réacteur et au moins une partie de ce mélange est chauffée à l'extérieur du réacteur puis renvoyée au réacteur de pyrolyse par l'intermédiaire du réservoir collecteur.
EP98945153A 1997-09-01 1998-08-06 Procede de traitement thermique d'une matiere contenant des constituants combustibles volatiles Expired - Lifetime EP1015527B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19738106 1997-09-01
DE19738106A DE19738106C2 (de) 1997-09-01 1997-09-01 Verfahren zum thermischen Behandeln von flüchtige, brennbare Bestandteile enthaltendem Material
PCT/EP1998/004889 WO1999011736A1 (fr) 1997-09-01 1998-08-06 Procede de traitement thermique d'une matiere contenant des constituants combustibles volatiles

Publications (2)

Publication Number Publication Date
EP1015527A1 true EP1015527A1 (fr) 2000-07-05
EP1015527B1 EP1015527B1 (fr) 2001-10-24

Family

ID=7840821

Family Applications (1)

Application Number Title Priority Date Filing Date
EP98945153A Expired - Lifetime EP1015527B1 (fr) 1997-09-01 1998-08-06 Procede de traitement thermique d'une matiere contenant des constituants combustibles volatiles

Country Status (5)

Country Link
EP (1) EP1015527B1 (fr)
AU (1) AU9257398A (fr)
DE (2) DE19738106C2 (fr)
ES (1) ES2165192T3 (fr)
WO (1) WO1999011736A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012004709A1 (fr) 2010-07-06 2012-01-12 Koninklijke Philips Electronics N.V. Génération d'images à grande gamme dynamique à partir d'images à faible gamme dynamique
US8764861B2 (en) 2007-07-13 2014-07-01 Outotec Oyj Process and plant for refining oil-containing solids

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19961437C2 (de) * 1999-12-20 2002-04-18 Kopf Ag Verfahren und Anlage zur Gewinnung von brennbarem Gas aus Klärschlamm
DE10157163A1 (de) * 2001-11-22 2003-06-18 Gfe Gmbh & Co Kg Ges Fuer Ents Verfahren und Vorrichtung zur Entsorgung von hochenergetische Stoffe enthaltenden Materialien, insbesondere von Granaten
DE10204815B4 (de) * 2002-02-06 2005-09-15 Eisenmann Maschinenbau Gmbh & Co. Kg Vorrichtung zur Entsorgung gefährlicher oder hochenergetischer Materialien
DE10253678A1 (de) * 2002-11-18 2004-05-27 Otto Dipl.-Ing. Heinemann Verfahren und Vorrichtung zur Gewinnung von Kohlenwasserstoffen
NL2000772C2 (nl) 2007-07-22 2009-01-23 Btg Bioliquids B V Pyrolyse-reactor.
DE102008008942B4 (de) 2008-02-13 2015-02-12 Outotec Oyj Verfahren und Anlage zur Raffination organische Anteile enthaltender Rohstoffe
DE102008008943B4 (de) 2008-02-13 2016-10-27 Outotec Oyj Verfahren und Anlage zur Raffination organische Anteile enthaltender Rohstoffe
CN104230135B (zh) * 2014-09-26 2016-11-16 中国石油天然气股份有限公司 含油污泥热解装置
CN108619890B (zh) * 2018-04-24 2019-03-08 东莞市泰昌纸业有限公司 废纸造纸废气的处理方法
CN112899000B (zh) * 2019-11-19 2022-06-03 上海工程技术大学 一种生物质废弃物挥发分催化油页岩干馏耦合系统及方法

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DE1909263C3 (de) * 1969-02-25 1974-04-25 Metallgesellschaft Ag, 6000 Frankfurt Verfahren und Vorrichtung zum Schwelen von feinkörnigen bituminösen Stoffen, die einen staubförmigen Schwelrückstand bilden
DE2537732C3 (de) * 1975-08-25 1981-12-10 Gosudarstvennyj naučno-issledovatel'skij energetičeskij institut imeni G.M. Kržižanovskogo, Moskva Verfahren zur thermischen Verarbeitung von festen bituminösen Stoffen
US4199432A (en) * 1978-03-22 1980-04-22 Chevron Research Company Staged turbulent bed retorting process
DE2946102A1 (de) * 1979-11-15 1981-05-27 Metallgesellschaft Ag, 6000 Frankfurt Verfahren und vorrichtung zum schwelen von feinkoernigem schwelgut mit heissem, feinkoernigem waermetraegermaterial
DE3835941A1 (de) * 1988-06-09 1990-04-26 Artur Richard Greul Verfahren der kunststoffpyrolyse im sandkoker

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9911736A1 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8764861B2 (en) 2007-07-13 2014-07-01 Outotec Oyj Process and plant for refining oil-containing solids
WO2012004709A1 (fr) 2010-07-06 2012-01-12 Koninklijke Philips Electronics N.V. Génération d'images à grande gamme dynamique à partir d'images à faible gamme dynamique

Also Published As

Publication number Publication date
DE19738106A1 (de) 1999-03-04
DE19738106C2 (de) 2001-01-04
EP1015527B1 (fr) 2001-10-24
AU9257398A (en) 1999-03-22
DE59801891D1 (de) 2001-11-29
ES2165192T3 (es) 2002-03-01
WO1999011736A1 (fr) 1999-03-11

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