EP3253849A1 - Réacteur pour l'extraction de gaz à partir de déchets organiques - Google Patents

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

Info

Publication number
EP3253849A1
EP3253849A1 EP15793745.9A EP15793745A EP3253849A1 EP 3253849 A1 EP3253849 A1 EP 3253849A1 EP 15793745 A EP15793745 A EP 15793745A EP 3253849 A1 EP3253849 A1 EP 3253849A1
Authority
EP
European Patent Office
Prior art keywords
reactor
gas
cleaning chamber
space
reaction space
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
EP15793745.9A
Other languages
German (de)
English (en)
Other versions
EP3253849B1 (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 RS20200319A priority Critical patent/RS60364B1/sr
Priority to PL15793745T priority patent/PL3253849T3/pl
Priority to SI201531135T priority patent/SI3253849T1/sl
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

Links

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 known from EP 2 495 299 A1. From this document, it is also known to lead the gases obtained from the organic waste through lines in a separate cleaning tank and there to effect a purification of the gas by condensate is separated from the recovered gas.
  • a reaction container which has cooling fins on its lid, in order to separate from
  • FR 905 858 A also describes a wood gas generator
  • the object of the invention is to improve a generic reactor in such a way that it achieves as trouble-free as possible a reliable recovery of the gas. allows and simplifies the maintenance of the reactor as easy as possible.
  • the invention proposes, in other words, not to carry out the purification of the recovered gas in a separate container, which is connected to the reactor through intermediate pipes, but rather to provide a common interior, which is referred to in its lower part as a reaction space and in his Upper area as a cleaning chamber, but this cleaning chamber is not designed as a closed relative to the reaction chamber chamber, but rather allows a free gas flow from the reaction chamber into the cleaning chamber.
  • the gases obtained anyway in the reaction chamber so that they then automatically get into the proposed embodiment of the reactor in the cleaning chamber, which adjoins the top of the reaction space.
  • the gas impinges on a cooling surface, so that condensate automatically precipitates on this cooling surface and in this way the purified gas from the condensate gas can be passed through a gas outlet from the reactor, the gas outlet opens into the cleaning chamber.
  • the temperature level in the reaction space can be controlled by providing a heatable gap between the thermal insulation, which is provided outside the reaction space, and the reactor housing, which delimits the reaction space.
  • This gap can be charged, for example, with exhaust gases from a combined heat and power plant, wherein the combined heat and power plant can in turn be operated with the gas which is generated in the reactor.
  • the cleaning chamber can essentially be connected to the reaction space with a constant, internal, free cross section so that the reactor can easily be regarded as an upright tube, in the lower region of which the reaction space is provided and which in its upper region, above the reaction space forming the cleaning chamber.
  • the wall of this reactor which is considered to be a tube, has different wall thicknesses, in that the above-mentioned thermal insulation is provided in the lower area, surrounding the reaction space, while in the upper area, where the cleaning chamber is provided, such insulation can be deliberately dispensed with in this way to use the pipe wall itself as a cooling surface on which the condensate is reflected.
  • the cleaning chamber with an upper lid which, for example, can be pivoted or hinged lid or can be configured as a slider.
  • the lid When the lid is open, the organic waste can be filled into the reactor, they automatically fall through the cleaning chamber into the reaction chamber down to the lower section, which is referred to as collecting space for the organic waste. Subsequently, the lid is closed again and the reaction space heated, for example to a temperature level of 360 to 430 ° C. Under pyrolytic conditions, so under
  • the organic waste can now be converted and gas extracted from them.
  • the gas rises in the reaction chamber upwards, thus enters the designated as the gas chamber portion of the reaction space, and from there further up into the cleaning chamber, where it passes against the cooling surface.
  • the operation of the reactor is carried out batchwise, ie in each case to the fullest possible utilization or implementation of the organic waste. Subsequently, the reactor is opened and a new batch of organic waste is introduced into the reactor. Since the organic material is almost completely reacted, only a very small amount of unreacted material remains in the reactor in relation to the initially used volumetric amount of the organic wastes. After a certain number of batches, the reactor can be cleaned of these residues and emptied.
  • Condensate which precipitates on the cooling surface of the cleaning chamber, can flow down or drips and gets there again in the reaction chamber, so that in the manner of a return a repeated and possibly repeated treatment of these substances takes place in the reaction chamber, which is the total supported the fullest possible implementation of the originally submitted organic waste.
  • a second gas line may be provided for discharging the recovered gases.
  • This second gas line is referred to as a bypass and serves in particular to remove 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 pipe in the cleaning chamber should become clogged by condensate, with the temperature inside the cleaning chamber, for example, in the range of 180 ° C to 200 ° C, it can be assumed that due to the much higher temperature level in the Gas space of the reaction chamber does not clog the mouth of the bypass and, accordingly, the gas can be passed through the bypass from the reactor, so that a dangerous increase in pressure in the reactor can be avoided. It can be provided that for simplification of the structural design of the reactor, the bypass need not be configured arbitrarily long, but rather opens at its second end in the gas outlet, so that from here on the gas can be forwarded in its usual way.
  • a condensate separator can be provided in the gas outlet line, so that a cleaning of the gas takes place, similar to what is already provided in the cleaning chamber.
  • This condensate separator allows a particularly effective cleaning of the gas in that it causes a total of two-stage cleaning of the gas as a post-purification.
  • the condensate separator has a condensation surface protruding into the gas flow and a condensate collecting space below, into which the condensate which collects on the condensation surface can drip off.
  • This possibly provided condensate separator can advantageously be arranged downstream of the point where the bypass opens into the gas outlet line. In this way, if the gas is withdrawn from the reaction space through the bypass, at least one-stage cleaning of the gas is ensured, since this gas passing through the bypass then passes into the condensate separator.
  • the condensate can advantageously be provided to return the recovered condensate in the reaction chamber, so that advantageously a return line may be provided, which opens with its one end in the Kondensatsammeiraum the Kondensatabscheiders and with its other end into the reaction space.
  • a return line may be provided, which opens with its one end in the Kondensatsammeiraum the Kondensatabscheiders and with its other end into the reaction space.
  • the cleaning chamber is designed as a separate element, that is not only as a certain portion of the reactor housing, which is provided above the reaction space.
  • the design as a separate element is a division of the reactor housing into a lower part which receives the reaction space, and an upper part which receives the cleaning chamber is possible. 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, accumulates at the originating from the gas condensate , Even if the cleaning chamber is mechanically firmly connected to the reaction space, it can be thermally insulated from the reaction space, so that in this way the effect of the cooling surface is affected 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 be, for example, 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 efficiency of a plant for the recovery of gas from organic waste can advantageously not be increased by enlarging the reaction space, for example by increasing the diameter, but by using a larger number of reactors.
  • the operation of the reactor is not continuous, but batchwise.
  • the gas is not directed into a memory, cached and retrieved as needed, but should continue to be used directly, for example, in a combined heat and power plant (CHP) to be burned.
  • a memory can be provided as a buffer for any fluctuations in the gas yield or fluctuations in the demand of the CHP. In comparison to not using the gas obtained immediately, but basically to preserve it in a memory for a longer and possibly indefinite time, this buffer memory can be considerably smaller and therefore designed less expensive.
  • the multiple reactors are not operated synchronously, with simultaneous interruptions for refilling or emptying or cleaning of the reactors. Rather, these interruptions of the reactor operation are provided offset from one to the other reactor, so that the gas output of the plant also over a longer period as evenly as possible and in this way downstream components, such as the mentioned CHP, as constant as possible and can be operated at an optimal operating point.
  • cooling surface is deliberately tempered. If, as indicated above, the cooling surface is formed, for example, by the pipe wall of the cleaning chamber, then an outer shield can run around this wall, so that a quasi-double wall configuration of the cleaning chamber is effected and by introducing liquid or gaseous media into This double-walled wall of the cleaning chamber, the temperature of the cooling surface can be controlled.
  • a total of 1 designates a reactor that can be considered simplified as upright aligned 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 wastes and into an upper gas space 4, this subdivision automatically resulting from how full the reaction space 2 is filled with organic waste.
  • the reaction space 2 is delimited by a reactor housing 5, which is adjoined radially outward by a heatable gap 6, which in turn is encased externally with a thermal insulation layer 7.
  • a reactor housing 5 which is adjoined radially outward by a heatable gap 6, which in turn is encased externally with a thermal insulation layer 7.
  • heating gases can be passed through the gap 6, in order in this way to heat the reaction space 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 serves, for example, to detect parameters in the interior of the reaction chamber 2, for example gas composition, temperature or the like.
  • the reactor 1 has a cleaning chamber 1 1, 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 1 1, and a lower
  • Flange 14 is fixedly connected to the reactor housing 5, which surrounds the reaction space 2. Thermally, both the reactor housing 5 and the lower flange 14 with respect to the housing of the cleaning chamber 1 1 is isolated, so that the wall of the cleaning chamber 1 1 forms a tubular cooling surface 15 at which condensate precipitates from the gas, which recovered from the organic waste was and has ascended from the gas space 4 of the reactor 1 up into the cleaning chamber 1 1.
  • the purified gas is passed through a gas outlet 16 from the cleaning chamber 1 1 and enters a condensate 17, which has a condensation surface 18 which is cooled by means of a cooling connection 19. At this condensation surface 18, condensate precipitates out of the gas and drips from there into a condensate collecting space 20.
  • a return line 21 connects at the bottom to the condensate collecting space 20 and leads the condensate to a point not apparent from the drawing, where it enters the reaction space 2 passes.
  • a bypass 22 is provided, via which the recovered gas can not be withdrawn from the cleaning chamber 1 1, but directly from the gas space 4.
  • the bypass 22 opens upstream of the condensate separator 17 into the gas outlet line 16.
  • a schematically indicated throttle flap 23 opens. allows the bypass 22 to be selectively opened or closed.
  • the reactor 1 is closed by a lid 24, which, like a bottom 25 provided at the bottom of the reactor 1, is designed as a horizontally movable slide and allows the opening of the reactor 1 in each case over its full free internal cross section, so that a particularly easy accessibility the inner surfaces of the cleaning chamber 1 1 and the reaction chamber 2 is made possible and in this way a simple and quick cleaning of the reactor 1 can be performed.
  • Actuators for actuating the respective slide of the lid 24 and bottom 25 are each denoted 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)

Abstract

L'invention concerne l'amélioration d'un réacteur pour l'extraction de gaz à partir de déchets organiques, ledit réacteur étant pourvu d'un logement en forme de colonne, dirigé vers le haut et entourant une chambre de réaction, qui présente une section pouvant être remplie de déchets organiques appelée chambre de collecte, qui comprend, placée au-dessus de ladite chambre de collecte, une chambre de gaz destinée à accueillir le gaz extrait des déchets organiques, et qui est isolée thermiquement vis-à-vis de l'extérieur, à savoir de l'atmosphère environnante, ladite amélioration consistant à raccorder par le haut une chambre de nettoyage, dont l'espace intérieur est adjacent à une surface de refroidissement, à ladite chambre de réaction et à faire déboucher dans la chambre de nettoyage une conduite d'évacuation de gaz conduisant le gaz extrait hors du réacteur.
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
RS20200319A RS60364B1 (sr) 2014-11-26 2015-11-04 Reaktor za dobijanje gasa iz organskog otpada
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
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 true EP3253849A1 (fr) 2017-12-13
EP3253849B1 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

Also Published As

Publication number Publication date
WO2016083089A1 (fr) 2016-06-02
RS60364B1 (sr) 2020-07-31
DK3253849T3 (da) 2020-03-23
SI3253849T1 (sl) 2020-10-30
CY1123171T1 (el) 2022-03-24
ES2777307T3 (es) 2020-08-04
DE102014117333A1 (de) 2016-06-02
PT3253849T (pt) 2020-03-27
EP3253849B1 (fr) 2019-12-25
HUE050612T2 (hu) 2020-12-28
PL3253849T3 (pl) 2020-08-10
HRP20200441T1 (hr) 2020-09-04
LT3253849T (lt) 2020-06-25

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