EP3253849B1 - Réacteur pour l'extraction de gaz à partir de déchets organiques - Google Patents

Réacteur pour l'extraction de gaz à partir de déchets organiques Download PDF

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Publication number
EP3253849B1
EP3253849B1 EP15793745.9A EP15793745A EP3253849B1 EP 3253849 B1 EP3253849 B1 EP 3253849B1 EP 15793745 A EP15793745 A EP 15793745A EP 3253849 B1 EP3253849 B1 EP 3253849B1
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EP
European Patent Office
Prior art keywords
reactor
gas
chamber
accordance
cleaning chamber
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.)
Active
Application number
EP15793745.9A
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German (de)
English (en)
Other versions
EP3253849A1 (fr
Inventor
Mari Jan STANKOVICC-GANSEN
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.)
Eckhoff Peter
Original Assignee
Eckhoff Peter
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 Eckhoff Peter filed Critical Eckhoff Peter
Priority to PL15793745T priority Critical patent/PL3253849T3/pl
Priority to SI201531135T priority patent/SI3253849T1/sl
Priority to RS20200319A priority patent/RS60364B1/sr
Publication of EP3253849A1 publication Critical patent/EP3253849A1/fr
Application granted granted Critical
Publication of EP3253849B1 publication Critical patent/EP3253849B1/fr
Priority to HRP20200441TT priority patent/HRP20200441T1/hr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/04—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in shaft furnaces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/06—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in retorts
    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/18—Modifying the properties of the distillation gases in the oven
    • 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
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials

Definitions

  • the invention relates to a reactor according to the preamble of claim 1.
  • Such a reactor is from the EP 0 075 060 A1 known.
  • a device for converting plastic into oil is known, and from the FR 914 272 A3 a device for distillation from solid fuels is known.
  • a reaction vessel is known which has cooling fins on its lid in order to promote the separation of condensate on the inside of the lid.
  • a wood gas generator is known, the lid of which is also designed for the separation of condensate, so that it can be cooled by means of an air stream.
  • the FR 905 858 A describes a wood gas generator
  • the object of the invention is to improve a generic reactor in such a way that it enables the gas to be obtained in a manner that is as trouble-free and reliable as possible and enables the reactor to be maintained as simply as possible.
  • the invention proposes not only to clean the gas obtained in the cleaning chamber, which is not designed as a chamber closed off from the reaction chamber, but rather enables a free gas flow from the reaction chamber into the cleaning chamber.
  • a condensate separator is provided in the gas outlet line, so that the gas is additionally cleaned, similarly as is provided in the cleaning chamber anyway.
  • This condensate separator enables a particularly effective purification of the gas in that it results in a two-stage purification of the gas as post-purification.
  • the condensate separator has a condensation surface protruding into the gas flow and a condensate collection space located underneath, into which the condensate that collects on the condensation surface can drip.
  • the gases obtained rise anyway in the reaction chamber, so that, in the proposed design of the reactor, they then automatically get into the cleaning chamber which connects to the reaction chamber at the top.
  • the gas meets a cooling surface, so that condensate automatically precipitates on this cooling surface and in this way the gas cleaned from the condensate can be led out of the reactor through a gas outlet line, the gas outlet line opening into the cleaning chamber.
  • a second gas line is provided for discharging the gases obtained. This second gas line is referred to as a bypass and is used, in particular, to draw the gases not from the cleaning chamber but from the gas space of the reactor.
  • This bypass serves as a safety device: If the opening of the gas outlet line in the cleaning chamber should become blocked by condensate, the temperature inside the cleaning chamber being, for example, in the range from 180 ° C to 200 ° C, it can be assumed that due to the significantly higher temperature level in the Gas space of the reaction space does not block the mouth of the bypass and, accordingly, the gas can be led out of the reactor through the bypass, so that a dangerous pressure increase in the reactor can be avoided.
  • the bypass does not have to be of any length, but rather ends at the second end in the gas outlet line, so that the gas can be passed on from here on in its usual way ,
  • the temperature level in the reaction space can be controlled by providing a heatable space between the thermal insulation which is provided outside the reaction space and the reactor housing which delimits the reaction space.
  • This intermediate space can, for example, be fed with exhaust gases from a cogeneration plant, the cogeneration plant in turn being able to be operated with the gas which is generated in the reactor.
  • the cleaning chamber can essentially connect to the reaction chamber with a constant, internal, free cross-section, so that the reactor can be viewed simply as an upright tube, in the lower region of which the reaction chamber is provided and which in its upper region, above the Reaction chamber that forms the cleaning chamber.
  • the wall of this reactor which is simply regarded as a tube, has different wall thicknesses, in that the thermal insulation mentioned is provided in the lower region, surrounding the reaction space, while in the upper region, where the cleaning chamber is provided, such insulation can be intentionally dispensed with in this way to use the pipe wall itself as a cooling surface on which the condensate is deposited.
  • the reaction chamber can be filled quickly and easily from above, for example by providing the cleaning chamber with an upper cover which, for example, can be pivoted or hinged lid or can be designed as a slide.
  • the lid When the lid is open, the organic waste can be poured into the reactor, it automatically falls through the cleaning chamber into the reaction space down to its lower section, which is called the collecting space for the organic waste.
  • the lid is then closed again and the reaction space is heated, for example to a temperature level of 360 to 430 ° C.
  • the organic waste Under pyrolytic conditions, i.e. without air, the organic waste can now be converted and gas can be extracted from it.
  • the gas rises upwards in the reaction chamber, that is, it reaches the section of the reaction chamber referred to as the gas space, and rises further upwards into the cleaning chamber, where it reaches the cooling surface.
  • the reactor is operated in batches, in other words until the organic waste is recycled or converted as completely as possible.
  • the reactor is then opened and a new batch of organic waste is introduced into the reactor. Since the organic material is almost completely converted, only a very small amount of unreacted material remains in the reactor in relation to the volumetric amount of organic waste initially used. After a certain number of batches, the reactor can be cleaned of these residues and emptied. Condensate, which is deposited on the cooling surface of the cleaning chamber, can flow down or drip and get there again into the reaction space, so that in the manner of a recycle, these substances are treated again and possibly repeatedly in the reaction space, which in total supports the fullest possible implementation of the originally submitted organic waste.
  • the condensate separator provided according to the proposal can advantageously be arranged downstream of the point where the bypass opens into the gas outlet line. In this way, when the gas is withdrawn from the reaction space through the bypass, at least one-stage cleaning of the gas is ensured, since this gas flowing through the bypass subsequently reaches the condensate separator.
  • the condensate separator it can advantageously be provided that the condensate obtained is returned to the reaction space, so that a return line can advantageously be provided which opens at one end into the condensate collection space of the condensate separator and at the other end into the reaction space. Similar to that described above for the condensate, which can flow downward from the cooling surface of the cleaning chamber into the reaction space, the condensate separator also causes the return line, the re-treatment of the condensate in the reaction space and supports in this way the most complete possible conversion of the organic waste originally introduced.
  • the cleaning chamber is designed as a separate element, that is to say not only as a certain section of the reactor housing which is provided above the reaction space.
  • the configuration as a separate element enables the reactor housing to be divided into a lower part, which receives the reaction space, and an upper part, which receives the cleaning chamber. A thermal separation of these two parts of the reactor housing is possible and also advantageous if the interior of the reactor extends continuously through the reaction space and the cleaning chamber.
  • the thermal separation prevents heat conduction from the heated wall of the reaction chamber to the wall of the cleaning chamber and thus supports the achievement of two different temperature zones in the reactor, so that, for example, the wall of the cleaning chamber can be used as a cooling surface on which condensate originating from the gas accumulates , Even if the cleaning chamber is mechanically connected to the reaction chamber, it can be thermally insulated from the reaction chamber, so that the effect of the cooling surface is impaired as little as possible and in this way an optimal cleaning effect of the cleaning chamber is supported.
  • the reaction space has a diameter of at most 300 mm.
  • the height of the reaction space can, for example be about 1.5 m, and the height of the cleaning chamber, for example, about 0.3 m.
  • the diameter of the reaction space can be particularly advantageously limited to a maximum value of 170 mm.
  • the performance of a plant for the production of gas from organic waste can advantageously not be increased by increasing the reaction space, for example by increasing the diameter, but by using a larger number of reactors.
  • the reactor is not operated continuously, but in batches.
  • the advantage of a quasi-continuous operation of the entire system can therefore also be achieved, namely the most uniform possible output of the gas obtained.
  • the gas is not to be led into a store, temporarily stored and called up as required, but is to be used directly, for example to be burned in a combined heat and power plant (CHP).
  • a storage can be provided as a buffer for possible fluctuations in the gas yield or fluctuations in the needs of the CHP. In comparison to not using the gas obtained immediately, but in principle storing it in a store for a longer and possibly indefinite period of time, this buffer store can be made considerably smaller and, accordingly, less expensive.
  • the multiple reactors are not operated synchronously, with simultaneous interruptions for refilling, emptying or cleaning the reactors. Rather, these interruptions in the operation of the reactor are each offset from one reactor to the other, so that the gas output of the plant takes place as evenly as possible over a longer period of time in this way, downstream components, such as the mentioned CHP, can be operated as constantly as possible and at an optimal operating point.
  • the cleaning effect in the cleaning chamber can advantageously be influenced by consciously tempering the cooling surface. If, as indicated above, the cooling surface is formed, for example, by the tube wall of the cleaning chamber, an outer shield can run around this wall, so that a double-walled configuration of the cleaning chamber is brought about and by introducing liquid or gaseous media into this double-shell Wall of the cleaning chamber the temperature of the cooling surface can be controlled.
  • a reactor 1 denotes a reactor, which can be viewed in simplified terms as an upright pipe.
  • a lower section of the reactor 1 has a reaction space 2 which is subdivided into a lower collecting space 3 for the organic waste and into an upper gas space 4, this subdivision automatically resulting from how fully the reaction space 2 is filled with organic waste.
  • the reaction space 2 is delimited by a reactor housing 5, which is adjoined radially outwards by a heatable intermediate space 6, which in turn is encased on the outside with a thermal insulating layer 7.
  • a reactor housing 5 which is adjoined radially outwards by a heatable intermediate space 6, which in turn is encased on the outside with a thermal insulating layer 7.
  • heating gases can be passed through the intermediate space 6 in order in this way to heat the reaction chamber 2 from the outside, namely by heating the reactor housing 5.
  • Another nozzle in the reactor housing 5 is indicated in the form of a measuring nozzle 10, which is used, for example, to record parameters in the interior of the reaction chamber 2, for example gas composition, temperature or the like.
  • the reactor 1 has a cleaning chamber 11 which is designed like an extension of the tubular reactor housing 5, but is designed as a separate element.
  • An upper flange 12 is fixedly connected to the wall of the cleaning chamber 11, and a lower flange 14 is fixedly connected to the reactor housing 5, which surrounds the reaction space 2.
  • Both the reactor housing 5 and the lower flange 14 are thermally insulated from the housing of the cleaning chamber 11, so that the wall of the cleaning chamber 11 forms a tubular cooling surface 15, on which condensate from the gas, which has been obtained from the organic waste, is deposited and has risen from the gas space 4 of the reactor 1 upwards into the cleaning chamber 11.
  • the cleaned gas is led through a gas outlet line 16 out of the cleaning chamber 11 and into a condensate separator 17 which has a condensation surface 18 which is cooled by means of a cooling connection 19. Condensate from the gas precipitates on this condensation surface 18 and drips from there into a condensate collection space 20.
  • a return line 21 connects to the condensate collection space 20 at the bottom and leads the condensate to a location (not shown in the drawing) where it reaches the reaction space 2 ,
  • a bypass 22 is provided, via which the gas obtained cannot be drawn off from the cleaning chamber 11 but directly from the gas space 4.
  • the bypass 22 opens upstream of the condensate separator 17 into the gas outlet line 16.
  • a throttle valve 23 indicated schematically enables it to selectively open or close the bypass 22.
  • the reactor 1 is closed at the top by a cover 24 which, like a bottom 25 provided at the bottom of the reactor 1, is designed as a horizontally movable slide and enables the reactor 1 to be opened over its full free internal cross section, so that access is particularly easy the inner surfaces of the cleaning chamber 11 or the reaction chamber 2 is made possible and in this way a simple and quick cleaning of the reactor 1 can be carried out.
  • Actuators for actuating the respective slide of the cover 24 or base 25 are each designated by 26.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing Of Solid Wastes (AREA)

Claims (9)

  1. Réacteur (1) pour l'extraction de gaz à partir de déchets organiques, comprenant un corps (5) de réacteur dressé à la verticale et entourant un compartiment de réaction (2) présentant un segment appelé compartiment collecteur (3) remplissable avec les déchets organiques, et qui présente au-dessus du compartiment collecteur (3) un compartiment à gaz (4) recevant le gaz extrait des déchets organiques, sachant que vis-à-vis de l'extérieur le compartiment de réaction (2) est isolé thermiquement par rapport à l'atmosphère ambiante et que vers le haut une chambre d'épuration (11) se raccorde au compartiment de réaction (2), sachant que le compartiment intérieur de la chambre d'épuration (11) jouxte une surface de refroidissement (15) et qu'une conduite de sortie (16) de gaz du réacteur (1), traversée par le gaz extrait, débouche dans la chambre d'épuration (11), et sachant que dans la conduite de sortie (16) de gaz est prévu un séparateur (17) de condensat présentant une surface de condensation (18) faisant saillie dans le flux de gaz, ainsi qu'un compartiment collecteur (20) du condensat situé en dessous, caractérisé en ce que dans le compartiment à gaz (4) débouche une deuxième conduite de gaz appelée conduite de bypass (22) sortant du réacteur (1) et également traversée par le gaz extrait, sachant que cette conduite de bypass (22) débouche dans la conduite de sortie (16) de gaz.
  2. Réacteur selon la revendication 1, caractérisé en ce qu'entre le corps (5) du réacteur et l'isolation thermique (7) est prévu un compartiment intermédiaire (6) chauffable.
  3. Réacteur selon la revendication 1 ou 2, caractérisé en ce que la chambre d'épuration (11) se raccorde vers le haut au compartiment de réaction (2), essentiellement sans réduction de la section intérieure libre.
  4. Réacteur selon l'une des revendications précédentes, caractérisé en ce que le séparateur de condensat (17) est disposé en aval de l'endroit où la conduite de bypass (22) débouche dans la conduite de sortie (16) de gaz.
  5. Réacteur selon l'une des revendications précédentes, caractérisé en ce qu'est prévue une conduite de retour (21) qui débouche à une extrémité dans le compartiment collecteur (20) de condensat et à une autre extrémité dans le compartiment de réaction (2).
  6. Réacteur selon l'une des revendications précédentes, caractérisé en ce que la chambre d'épuration (11) présente un orifice de remplissage pour les déchets organiques à traiter.
  7. Réacteur selon l'une des revendications précédentes, caractérisé en ce que la chambre d'épuration (11) est configurée en élément séparé relié à demeure avec le corps (5) de réacteur entourant le compartiment de réaction (2), et est isolée thermiquement par rapport au corps (5) de réacteur.
  8. Réacteur selon l'une des revendications précédentes, caractérisé en ce que le compartiment de réaction (2) présente un diamètre d'au maximum 300 mm.
  9. Réacteur selon la revendication 8, caractérisé en ce que le compartiment de réaction (2) présente un diamètre d'au maximum 170 mm.
EP15793745.9A 2014-11-26 2015-11-04 Réacteur pour l'extraction de gaz à partir de déchets organiques Active EP3253849B1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
PL15793745T PL3253849T3 (pl) 2014-11-26 2015-11-04 Reaktor do pozyskiwania gazu z odpadów organicznych
SI201531135T SI3253849T1 (sl) 2014-11-26 2015-11-04 Reaktor za pridobivanje plina iz organskih odpadkov
RS20200319A RS60364B1 (sr) 2014-11-26 2015-11-04 Reaktor za dobijanje gasa iz organskog otpada
HRP20200441TT HRP20200441T1 (hr) 2014-11-26 2020-03-17 Reaktor za dobivanje plina iz organskog otpada

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014117333.3A DE102014117333A1 (de) 2014-11-26 2014-11-26 Reaktor zur Gasgewinnung aus organischen Abfällen
PCT/EP2015/075719 WO2016083089A1 (fr) 2014-11-26 2015-11-04 Réacteur pour l'extraction de gaz à partir de déchets organiques

Publications (2)

Publication Number Publication Date
EP3253849A1 EP3253849A1 (fr) 2017-12-13
EP3253849B1 true EP3253849B1 (fr) 2019-12-25

Family

ID=54540035

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15793745.9A Active EP3253849B1 (fr) 2014-11-26 2015-11-04 Réacteur pour l'extraction de gaz à partir de déchets organiques

Country Status (13)

Country Link
EP (1) EP3253849B1 (fr)
CY (1) CY1123171T1 (fr)
DE (1) DE102014117333A1 (fr)
DK (1) DK3253849T3 (fr)
ES (1) ES2777307T3 (fr)
HR (1) HRP20200441T1 (fr)
HU (1) HUE050612T2 (fr)
LT (1) LT3253849T (fr)
PL (1) PL3253849T3 (fr)
PT (1) PT3253849T (fr)
RS (1) RS60364B1 (fr)
SI (1) SI3253849T1 (fr)
WO (1) WO2016083089A1 (fr)

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR887439A (fr) * 1941-09-18 1943-11-12 Procédé et dispositif pour la récupération des sous-produits condensables, dans la distillation partielle du bois en vue de sa carbonisation
FR905858A (fr) * 1944-07-11 1945-12-17 Générateur pour gazogène à bois
FR914272A (fr) * 1945-04-09 1946-10-03 Procédé et appareil de distillation des combustibles solides, des schistes bitumeux et des résines et colophanes, et procédé de récupération de l'hydrogène sulfuré, du benzol et autres carbures volatils, en dérivant
DE3131476C2 (de) * 1981-08-08 1983-12-22 Fritz Werner Industrie-Ausrüstungen GmbH, 6222 Geisenheim Holzgasgenerator
IT1171542B (it) * 1981-09-21 1987-06-10 Marco Vincenzo De Dispositivo di trasformazione di gomma materiali plastici e rifiuti urbani con recupero di miscele di idrocarburi liquidi e carbone e procedimento di combustione
GB2242687B (en) * 1990-03-31 1994-08-31 Uss Kk Apparatus for converting synthetic resin into oil
EP2495299A1 (fr) 2011-03-04 2012-09-05 Eckhoff, Peter Installation d'évaluation thermique de matières organiques et récipient à fusion d'une telle installation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
PT3253849T (pt) 2020-03-27
EP3253849A1 (fr) 2017-12-13
ES2777307T3 (es) 2020-08-04
PL3253849T3 (pl) 2020-08-10
WO2016083089A1 (fr) 2016-06-02
CY1123171T1 (el) 2022-03-24
LT3253849T (lt) 2020-06-25
SI3253849T1 (sl) 2020-10-30
HUE050612T2 (hu) 2020-12-28
RS60364B1 (sr) 2020-07-31
DE102014117333A1 (de) 2016-06-02
DK3253849T3 (da) 2020-03-23
HRP20200441T1 (hr) 2020-09-04

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