EP2986914B1 - Améliorations dans le traitement des déchets - Google Patents

Améliorations dans le traitement des déchets Download PDF

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Publication number
EP2986914B1
EP2986914B1 EP14717839.6A EP14717839A EP2986914B1 EP 2986914 B1 EP2986914 B1 EP 2986914B1 EP 14717839 A EP14717839 A EP 14717839A EP 2986914 B1 EP2986914 B1 EP 2986914B1
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EP
European Patent Office
Prior art keywords
processing chamber
chamber
syngas
gas
oxygen
Prior art date
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Application number
EP14717839.6A
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German (de)
English (en)
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EP2986914A1 (fr
Inventor
Rifat Al Chalabi
Ophneil Henry Perry
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Chinook End Stage Recycling Ltd
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Chinook End Stage Recycling Ltd
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Publication of EP2986914A1 publication Critical patent/EP2986914A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/101—Combustion in two or more stages with controlled oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/104—Arrangement of sensing devices for CO or CO2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste

Definitions

  • the present invention relates to waste processing and particularly to a system and method for generating energy from waste material and/or reclaiming material from waste.
  • the invention relates to an apparatus and a method for processing municipal waste by thermally removing coatings and/or impurities from materials which are capable of being recovered from the waste, for example removing coatings and impurities from metals that are capable of being recycled, and then post-processing any carbonaceous residue.
  • Pyrolysis and gasification are processes that convert organic materials, such as biomass, or materials containing organic content into carbon monoxide and hydrogen by heating the raw material to high temperatures in an environment containing little or no oxygen.
  • the resulting gas mixture is called synthesis gas or syngas.
  • Synthetic gas is made predominately of carbon monoxide (CO), and hydrogen.
  • Pyrolysis is an efficient method for extracting energy from many different types of organic materials and provides clean waste disposal.
  • the material is heated in an atmosphere comprising substantially no oxygen.
  • a by-product of the pyrolysis process can be carbonaceous residue which may include carbon, cokes and char. Such residues are collectively referred to herein as "char".
  • Energy recovered from combustion of syngas from pyrolysis is more efficient than direct combustion of the solid original waste, particularly since more of the organic materials contained in the processed material are converted into energy (higher thermal efficiency). Gasification is similar to pyrolysis except insofar as a small amount of oxygen is present.
  • Syngas may be burned directly in internal combustion engines or used to produce alcohols such as methanol, ethanol and propanol, and also hydrogen.
  • a waste-heat boiler is used to recover the heat generated from combusting the syngas. It is known to use thermal treatment chambers to destroy the gases, tars, and other environmentally unsound components that are emitted from the material as it is processed and become entrained in the gas produced. To destroy these components they must be heated to a temperature in excess of approximately 850°C for a minimum residency time. Excess hot gasses from this thermal treatment chamber can have heat recovered therefrom for use in powering, for example, a waste heat boiler which drives a steam turbine and thereby generates electricity.
  • Continuous processing is good for large volumes of substantially consistent supply material that enables steady state process conditions.
  • the material passes constantly through some form of oven at a steady speed so that by the time it exits from oven it is fully pyrolysed/de-coated.
  • This process is very good for large volumes of a substantially homogeneous mixture of waste, as it relies on steady state conditions to ensure the complete process is achieved, i.e. the oven temperatures and feed rates are set at a desired level and remain constant.
  • Batch processing is beneficial where either low volumes are being processed or where there is a large variation in the type of material to be processed from batch to batch, e.g. calorific content, water content etc.
  • a batch containing predominantly paper and wood would require different processing conditions than, for example, a batch containing predominantly shredded rubber (e.g. car tyres).
  • One problem with the batch process is that, while it enables great flexibility in the processing cycle by allowing process variation between batches, the batch process does not produce a steady rate of syngas, in particular at the beginning and at the end of each batch where there is a ramp up and a ramp down of syngas production.
  • syngas is normally treated in a treatment chamber after production to heat and/or combust it, and the hot exhaust gases are then often used for power generation, e.g. to power a boiler.
  • the thermal treatment chamber must be sized to accommodate maximum syngas production and is therefore underutilised for much of the cycle. This is compounded by the batch to batch fluctuation in the material which may result in different peaks of maximum syngas production. Specific types of material produce short, high peaks and other materials producing long, flat peaks.
  • the thermal oxidiser must be sized to be able to destroy all the syngas produced at the maximum peak, resulting in it being run substantially under capacity for much of its operational life.
  • virgin fuel typically natural gas
  • US 2009/020052 discloses an apparatus having the features specified in the preamble of claim 1 and a method having the features specified in the preamble of claim 10. It is the purpose of the present invention to produce a batch process system that addresses at least some of the problems associated with the state of the art.
  • an apparatus arranged to process waste having an organic content, the apparatus comprising: a first processing chamber arranged to receive and heat said waste in a reduced or substantially zero-oxygen atmosphere to produce syngas and carbonaceous material; a second processing chamber arranged to receive and heat carbonaceous material in a reduced oxygen atmosphere to gasify it to produce carbon monoxide; and a thermal treatment chamber having a syngas inlet configured to receive syngas from the first chamber and the carbon monoxide from the second chamber, said thermal treatment chamber configured to heat the gas therein to break down any volatile organic compounds or long chain hydrocarbons therein.
  • the apparatus comprises means for controlling the oxygen content within the second processing chamber comprising a control system configured to monitor a property of the gas produced in the first processing chamber and to control a flow of oxygen containing gas into the second processing chamber in response to said property.
  • a reduced or substantially zero-oxygen atmosphere may comprise an atmosphere with an oxygen level lower than atmospheric air or standard conditions.
  • the atmosphere may be oxygen-depleted.
  • the reduced or substantially zero-oxygen atmosphere may comprise less than 20% oxygen.
  • the reduced or substantially zero-oxygen atmosphere may comprise less than 15%, 12%, 10%, 8%, 6%, 5%, 4%, 3%, 2%, or 1% oxygen by volume.
  • the oxygen level is at trace levels, or 0%.
  • the reduced or substantially zero-oxygen atmosphere may comprise an oxygen level sufficiently low to prevent the organic waste being fully oxidised, for example, to prevent the formation of carbon dioxide.
  • a gasification process occurs in the second processing chamber.
  • the oxygen reacts with the carbon to produce carbon monoxide and accordingly carbonaceous materials can be consumed in a gasification process in the second processing chamber. This enables more of the energy to be recovered from the waste as the energy stored within the carbonaceous residue created in the first processing chamber can be recovered.
  • the first processing chamber and/or the second processing chamber may be batch processing chambers.
  • the means to control the oxygen content of the second batch processing chamber may be such that the oxygen content in the second batch processing chamber is higher than the oxygen content in the first batch processing chamber.
  • Means may be provided for providing a flow of hot gas to the first processing chamber and a flow of hot gas to the second processing chamber for heating the material therein, the system further comprising valve means for introducing oxygen containing gas into the flow of hot gas to the second chamber.
  • the apparatus may further comprise valve means to selectively divert at least a portion of the gas exiting the first processing chamber to pass through the second processing chamber prior to entering the thermal treatment chamber.
  • a conduit can be provided between the thermal treatment chamber and the first processing chamber for re-circulating hot gas from the thermal treatment chamber to the first processing chamber.
  • a diverter valve can be provided in said conduit, said diverter valve for selectively diverting the re-circulating hot gas between the first processing chamber and the second processing chamber.
  • the apparatus may also comprise a flow rate controller to control the flow rate of re-circulated gas.
  • the apparatus may comprise an outlet from the thermal treatment chamber leading to at least one of a waste-heat boiler and a syngas engine.
  • the apparatus may be provided with a carbon monoxide sensor downstream of the first processing chamber that monitors and produces an electrical output signal indicative of the carbon monoxide content of the gas produced from the first processing chamber.
  • the apparatus may further comprising a diverter valve in said conduit, said diverter valve for selectively diverting the re-circulating hot gas between the first processing chamber and the second processing chamber.
  • the first processing chamber is a rotating or tilting oven having a first size and the second processing chamber has a second size smaller than the first size.
  • the apparatus may further comprise at least one heat source configured for providing a flow of hot gas to the first and second processing chambers.
  • the heat source may be configured to provide a flow of hot gas with substantially zero oxygen content to the first processing chamber so as to pyrolyse the material therein.
  • the apparatus may comprise a means of adding H 2 O to the second processing chamber to gasify the carbonaceous material therein to produce syngas comprising carbon monoxide and hydrogen.
  • a method of processing organic-based material or waste comprising: heating, in a first processing chamber, material having an organic content in a reduced or substantially oxygen free environment to produce syngas and carbonaceous material; heating in a second processing chamber carbonaceous material produced in the first processing chamber in a reduced oxygen environment to produce carbon monoxide; receiving syngas from the first processing chamber and carbon monoxide from the second processing chamber in a thermal treatment chamber and heating said syngas and carbon monoxide therein to break down any volatile organic compounds or long chain hydrocarbons entrained therein.
  • the method further comprises monitoring a property of the gas produced in the first processing chamber; and controlling a flow of oxygen containing gas into the second processing chamber in response to said property so as to control the oxygen content within the second processing chamber.
  • the first processing chamber and/or the second processing chamber may be operated in a batch processing mode. Controlling the oxygen content of the second batch processing chamber may be such that the oxygen content in the second batch processing chamber is higher than the oxygen content in the first batch processing chamber.
  • the method may further comprise: providing a flow of hot gas to the first processing chamber for heating the material therein; providing a flow of hot gas to the second processing chamber for heating the material therein, wherein the method further comprises introducing oxygen containing gas into the flow of hot gas to the second chamber.
  • the method may comprise one or more of the following:
  • the heat source may be configured to provide a flow of hot gas with substantially zero oxygen content to the first processing chamber so as to pyrolyse the material therein.
  • the method may comprise: monitoring a property of the syngas indicative of the syngas production from the first processing chamber; identifying from said monitored property when the syngas production rate from the first processing chamber falls below a first predetermined value; and increasing the oxygen content in the second processing chamber.
  • the method may include controlling the amount of hot gas and the amount of oxygen diverted through said second processing chamber so as to maintain a substantially constant flow rate of syngas into said thermal treatment chamber.
  • the method may comprise identifying when said syngas production rate from the first processing chamber falls below a second predetermined value and diverting said re-circulated gas from said thermal treatment chamber to said second processing chamber to isolate said first batch processing pyrolysis chamber from said re-circulated gas flow.
  • the method may comprise: during the processing cycle, maintaining the second processing chamber at a temperature sufficient for gasification; and controlling the flow of oxygen into the second processing chamber such that carbon dioxide can be produced upon demand.
  • the method may comprise providing a means of adding H 2 O to the second processing chamber to gasify the carbonaceous material therein to produce syngas comprising carbon monoxide and hydrogen.
  • the gas produced in the first processing chamber can be selectively diverted through a second processing chamber and have its oxygen content increased so as to cause the syngas produced by the first processing chamber to be supplemented by the carbon monoxide produced by the second processing chamber so as to enrich the gas flow from the first process.
  • FIG. 1 a graph of syngas production rate against time is shown for a full cycle of a batch processing chamber.
  • An example of an apparatus for performing this operation is disclosed in WO 2006/100512 and although described in this operation as being a pyrolysis reaction it will be appreciated by the skilled person that there could be some oxygen content within the processing chamber resulting in some gasification.
  • the chamber is loaded and the process started at T 1 .
  • the pyrolysis process starts and the syngas production increases until, at T 2 , the material is pyrolysing at a substantially steady rate. In reality the production rate during this period will fluctuate about an average value.
  • T 3 the majority of the material in the chamber has pyrolysed and the syngas production starts to reduce until T 4 , when all of the organic material has pyrolysed.
  • the processing chamber can then be emptied of the non-pyrolysable materials (e.g. metals), refilled, and processing of the next batch started.
  • a pyrolysis reaction also forms a carbonaceous material, referred to herein as char, from these materials.
  • char carbonaceous material
  • the curve shown in Figure 1 is typical of municipal waste. It will be appreciated that the curve shown is a generic curve for this type of waste and that the actual shape of the curve will change depending on the exact content of the waste.
  • a graph of carbon monoxide production rate against time is shown for a batch processing chamber when gasifying the char formed in the first process.
  • the rate of oxidation is dependent upon the surface area of the char and the oxygen available for the oxidation process. Accordingly, the shape of the curve can be modified as required by altering the oxygen available for oxidation to occur. It will therefore be appreciated that the reaction can be stopped whilst maintaining the char at oxidation temperatures by heating the char with gas that contains no oxygen and the carbon monoxide production can be produced on demand by adding oxygen containing gas to the oxygen free gas prior to it contacting the heated char.
  • syngas/carbon monoxide being produced can either be combusted in the presence of oxygen in a thermal treatment chamber to produce heat for conversion to energy (e.g. via a boiler and steam turbine), or can be treated in the thermal treatment chamber in the absence of oxygen to break down any long chain hydrocarbons or VOC's therein and the gas can then be used to power a syngas engine to produce electricity.
  • the thermal treatment chamber must raise the temperature of the syngas to a predetermined temperature, typically in excess of 850° C for a minimum amount of time to destroy the any VOC's or long chain hydrocarbons.
  • a predetermined temperature typically in excess of 850° C for a minimum amount of time to destroy the any VOC's or long chain hydrocarbons.
  • the presence of sufficient oxygen within the treatment chamber will dictate if the syngas is combusted or if it is just heated.
  • a waste treatment apparatus of the invention is shown.
  • a first waste processing chamber 10 is heated with a flow of hot gasses from heat source 12, the flow of hot gasses being controlled by a valve 14 which is operated by a controller 16.
  • the processing chamber is preferably a tilting oven type as described in patent application WO 2006/100512 .
  • the first processing chamber 10 is used for heating 200 the material being processed, e.g. the municipal solid waste. Preferably no oxygen is present in the hot gases produced by the first heat source 12 such that the material in the first processing chamber 10 pyrolyses to release syngas.
  • the syngas production rate for this first processing chamber 10 is substantially as shown in Figure 1 , i.e. it has a ramp up phase, a production phase and a ramp down phase.
  • Syngas produced in the first processing chamber 10 passes through a conduit 18 into the thermal treatment chamber 20, via valve 22.
  • the syngas is heated or combusted in the treatment chamber 20 and the hot gases exit the treatment chamber 20 via conduit 24. If the gasses are heated but not combusted in the treatment chamber 20 then the gas exiting the treatment chamber 20 will be syngas.
  • the gases exiting the treatment chamber 20 will be hot exhaust gases.
  • heat can be recovered from the gas for conversion into usable energy, for example in a heat exchanger of a boiler.
  • the gas can be used, for example in a syngas engine, to produce electricity.
  • a second processing chamber 26 is also provided.
  • the second processing chamber 26 is loaded with char produced from the pyrolysation of the material being processed in the first processing chamber.
  • Hot gas produced from a further heat source is passed through the second processing chamber (which may also be of the type described in WO 2006/100512 ).
  • the gas entering the second processing chamber 26 via valve 28 can have its oxygen level controlled.
  • a source of oxygen containing gas 30, for example air, can be added 204 to the gas flow via valve 32.
  • the oxygen reacts with the hot char to gasify it to produce carbon monoxide which passes through CO conduit 34 to the thermal treatment chamber 20 via a valve 36.
  • the CO production rate of the second processing chamber will be dependent upon its temperature and on the oxygen content of the gas.
  • the oxygen source 30 is shown as being discrete from the heat source it will be appreciated that the oxygen level of the hot gases supplied can be controlled within the heat source 28.
  • the second processing chamber is discussed as producing carbon monoxide it may also produce hydrogen (the other main component of syngas) and carbon dioxide if any moisture is present.
  • the second processing chamber 26 is preferably maintained at a temperature sufficient for oxidation to take place. This may be done by passing substantially dry, hot gas containing no oxygen therethrough. As the material has already been fully pyrolysed it is inert in the absence of oxygen. The production of carbon monoxide in the second processing camber can then be controlled by adding oxygen to the hot, dry gas. In addition, hydrogen may be produced by adding steam to the gas passing through the second processing chamber.
  • the two processing chambers can be run in parallel for the same processing time and when the carbon monoxide sensor 38, and optionally hydrogen sensors, detect that the material in the first processing chamber is fully processed, the first and second chambers can be isolated from the hot gas, emptied, and refilled.
  • the oxygen content of the gas being supplied to the second processing chamber 26 can be controlled to ensure that all the char in the second processing chamber is gasified by the time the first processing chamber has finished its cycle.
  • the oxygen content of the gases passing through the second processing chamber 26 can be increased 204 (or alternatively gas containing oxygen can start to be passed through the second processing chamber). Accordingly the production rate of carbon monoxide, and optionally hydrogen, from the second processing chamber 26 increases and substantially balances the reduction in production rate from first processing chamber 10. This results in a more continuous production of syngas which can be particularly beneficial when the gas is being used to power a syngas engine.
  • This apparatus 100 can therefore uses the syngas produced in the second processing chamber 26 to compensate for the shortfall in the production rate of syngas from the first processing chamber 10 at the start and end of the cycle.
  • the first processing chamber 10 can be opened 210 and replenished with a fresh batch of organic-based material for processing and restarted.
  • the syngas production ramps up from the fresh batch of organic-based material in the first processing chamber the amount of oxygen being supplied to the second processing chamber 26 is reduced 214 so that the total syngas flow to the thermal treatment chamber is substantially constant.
  • the speed of the gasification reaction in the second processing chamber 26 can be controlled by the addition of a varying level of oxygen and optionally steam, it can be controlled so that gasification is complete when the first processing chamber is in peak production.
  • a further carbon monoxide sensor 46 is provided downstream of the second processing chamber 26 which detects when the gasification in the second processing chamber is complete. The second processing chamber 26 can then be opened, emptied and replenished.
  • the carbon monoxide sensor 38 located in the conduit 18 downstream of the first processing chamber 10 measures and produces an electrical signal indicative of the carbon monoxide content of the gas produced from the first batch processing pyrolysis chamber.
  • syngas is primarily a mixture of carbon monoxide and hydrogen the carbon monoxide content of the gas exiting the first processing chamber 10 is a good indicator of the level of syngas being produced therein and can be used to determine if the syngas production meets a required level 202 or if there is a shortfall in syngas.
  • a control system 16 receives the output from the carbon monoxide sensor 38 and controls the valves 14, 22, 28, 32 and 36 in response thereto. In particular the controller controls the amount of oxygen that passes into the second processing chamber 26.
  • the second processing chamber 26 receives its hot gas from the thermal treatment chamber 20.
  • the thermal treatment chamber 20 will have a burner therein for burning fuel to heat the gas therein. Accordingly some of the hot gas form the thermal treatment chamber 20 can be re-circulated through the second processing chamber 26. As this gas will not contain any oxygen the char in the second processing chamber 26 will be heated to an elevated temperature by this recirculating gas.
  • the controller 16 can increase the oxygen content, and optionally the moisture content, of the gas passing through the second processing chamber 26 to cause the material therein to gasify.
  • the source of oxygen 30 may include a source of oxygen and water, or steam, the supply of both of which can be controlled independently of one another to maintain a desired carbon monoxide and optionally hydrogen output 212.
  • a high temperature fan 40 may be provided to circulate some of the hot gases from the thermal treatment chamber 20 to the second processing chamber 26. Apart from the different heat source for the second processing chamber the apparatus operates in the same manner as described above, and the gas not circulated through the second processing chamber 26 exits the thermal treatment chamber via conduit 24.
  • FIG. 5 a further arrangement of the invention is shown.
  • the apparatus is substantially the same as described in relation to Figure 4 except that the independent heat source 12 that provides hot gas to the first processing chamber 10 is replaced with a recirculation conduit 42 connecting the thermal treatment chamber 20 to the first processing chamber 10.
  • a high temperature fan 44 is provided in the conduit 42 to drive the hot gas through the conduit.
  • the controller 16 operates the system as described above. It will be appreciated that the parallel sections of re-circulation conduit joining the thermal processing chamber 20 to the first processing chamber 10 and the second processing chamber 26 may be combined such that the conduit feeding hot gas into the second processing chamber 26 branches off from the conduit 42.
  • valves 14, 22, 28, 36 gas can be directed to the first processing chamber 10, the second processing chamber 26, or both processing chambers.
  • the valves also allow the first processing chamber 10 and the second processing chamber 26 to be isolated 208 from the hot gas flow so that they can be emptied and refilled whilst the process is maintained on the syngas produced from the other processing chamber.
  • the process operates a two-step process to pyrolyse the material to release energy and produce char, and then gasifies the char to release the remainder of the energy, the process allows more of the energy in the raw material (municipal waste) to be recovered and thereby increases the overall efficiency of the system.
  • the thermal oxidiser can be specified to a size to fully combust the substantially constant level of syngas being produced as opposed to being sized to cope with the maximum syngas as is currently the case.
  • the thermal treatment chamber can run the burner that heats the gas therein on syngas.
  • the system substantially produces a constant syngas flow there is no period during its operation when there is a large shortfall in the syngas required to maintain the thermal treatment chamber at its operational temperature. Accordingly, the system reliance on virgin fuel is reduced and the overall system efficiency and environmental credentials are increased by virtue of reduced fossil fuel consumption.
  • a further advantage of substantially steady state production is that it significantly reduces the ripple in the power output enabling a much more steady power generation to be achieved.
  • the above apparatus may also provide other benefits to the system. For example, as it is possible to enable a substantially constant amount of syngas to be produced and consumed in the thermal treatment chamber, the apparatus will provide a more steady state output of excess gas for the waste-heat boiler. This will have a knock-on effect and help to minimise any fluctuation in electrical output of a generator powered by the waste-heat boiler. Furthermore, for maximum efficiency and reliability, electrical generation equipment generally operates best under the steady state conditions that the invention helps to provide.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Processing Of Solid Wastes (AREA)

Claims (15)

  1. Appareil destiné à traiter des déchets ayant un contenu organique, l'appareil comprenant :
    une première chambre de traitement 10 destinée à recevoir et à chauffer lesdits déchets dans une atmosphère à faible teneur en oxygène ou sensiblement dépourvue d'oxygène pour produire un gaz de synthèse et une matière carbonée,
    une seconde chambre de traitement 26 destinée à recevoir et à chauffer la matière carbonée dans une atmosphère à faible teneur en oxygène pour la gazéifier afin de produire du monoxyde de carbone,
    une chambre de traitement thermique 20 possédant une admission de gaz de synthèse conçue pour recevoir du gaz de synthèse provenant de la première chambre 10 et le monoxyde de carbone provenant de la seconde chambre 26, ladite chambre de traitement thermique 20 étant conçue pour chauffer le gaz qu'elle contient afin de décomposer des éventuels composés organiques volatiles ou des hydrocarbures à longue chaîne s'y trouvant, et
    caractérisé en ce que l'appareil comprend un moyen pour régler la teneur en oxygène dans la seconde chambre de traitement 26 comprenant un système de régulation 16 conçu pour surveiller une caractéristique du gaz produit dans la première chambre de traitement 10 et pour réguler le flux de gaz contenant de l'oxygène dans la seconde chambre de traitement 26 en réponse à ladite caractéristique.
  2. Appareil selon la revendication 1, dans lequel la première chambre de traitement 10 et/ou la seconde chambre de traitement 26 sont des chambres de traitement par lots.
  3. Appareil selon la revendication 2, dans lequel en outre :
    le moyen pour régler la teneur en oxygène de la seconde chambre de traitement par lots 26 est conçu de telle sorte que la teneur en oxygène dans la seconde chambre de traitement par lots 26 sera plus élevée que la teneur en oxygène dans la première chambre de traitement par lots 10.
  4. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre un moyen pour fournir un flux de gaz chaud jusqu'à la première chambre de traitement 10 et un flux de gaz chaud jusqu'à la seconde chambre de traitement 26 pour chauffer la matière s'y trouvant, le système comprenant en outre un moyen de vanne 32 pour introduire du gaz contenant de l'oxygène dans le flux de gaz chaud s'écoulant jusqu'à la seconde chambre de traitement 26.
  5. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre un moyen de vanne pour détourner sélectivement au moins une partie du gaz sortant de la première chambre de traitement 10 afin de la faire circuler à travers la seconde chambre de traitement 26 avant d'entrer dans la chambre de traitement thermique 20.
  6. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre une conduite 42 entre la chambre de traitement thermique 20 et la première chambre de traitement 10 pour faire recirculer le gaz chaud depuis la chambre de traitement thermique 20 jusqu'à la première chambre de traitement 10.
  7. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre une sortie 24 de la chambre de traitement thermique 26 menant à une chaudière de récupération de chaleur et/ou un moteur à gaz de synthèse.
  8. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre un capteur de monoxyde de carbone 38 en aval de la première chambre de traitement 10 qui surveille la teneur en monoxyde de carbone du gaz produit à partir de la première chambre de traitement 10 et produit un signal de sortie électrique indiquant cette teneur.
  9. Appareil selon l'une quelconque des revendications précédentes, comprenant en outre un moyen pour ajouter de l'H2O dans la seconde chambre de traitement 26 pour gazéifier la matière carbonée s'y trouvant afin de produire du gaz de synthèse comprenant du monoxyde de carbone et de l'hydrogène.
  10. Procédé de traitement de matières ou de déchets à base organique, comprenant les opérations suivantes :
    chauffage, dans une première chambre de traitement 10, de matière ayant un contenu organique dans un environnement pauvre en oxygène ou exempt d'oxygène pour produire du gaz de synthèse et une matière carbonée,
    chauffage dans une seconde chambre de traitement 26 de la matière carbonée produite dans la première chambre de traitement 10, dans un environnement pauvre en oxygène pour produire du monoxyde de carbone, et
    réception du gaz de synthèse provenant de la première chambre de traitement 10 et de monoxyde de carbone provenant de la seconde chambre de traitement 26 dans une chambre de traitement thermique 20, et chauffage de ceux-ci à l'intérieur de la chambre pour décomposer tous composés organiques volatiles ou tous hydrocarbures à longue chaîne.
    caractérisé en ce que le procédé comprend en outre
    la surveillance d'une caractéristique du gaz produit dans la première chambre de traitement 10, et
    la régulation d'un flux de gaz contenant de l'oxygène dans la seconde chambre de traitement 26 en réponse à la dite caractéristique de façon à réguler la teneur en oxygène à l'intérieur de la seconde chambre de traitement 26.
  11. Procédé selon la revendication 10, dans lequel :
    la régulation de la teneur en oxygène dans la seconde chambre de traitement par lots 26 est conçue de telle sorte que la teneur en oxygène dans la seconde chambre de traitement par lots 26 est plus élevée que la teneur en oxygène dans la première chambre de traitement par lots 10.
  12. Procédé selon l'une quelconque des revendications 10 ou 11, comprenant en outre :
    la fourniture d'un flux de gaz chaud jusqu'à la première chambre de traitement par lots 10 pour chauffer la matière s'y trouvant,
    la fourniture d'un flux de gaz chaud jusqu'à la seconde chambre de traitement par lots 26 pour chauffer la matière s'y trouvant, et dans lequel
    le procédé comprend en outre l'introduction de gaz contenant de l'oxygène dans le flux de gaz chaud s'écoulant jusqu'à la seconde chambre de traitement 26.
  13. Procédé selon l'une quelconque des revendications 10 à 12, comprenant en outre le détournement sélectif d'au moins une partie du gaz sortant de la première chambre de traitement 10 pour le faire circuler à travers la seconde chambre de traitement 26 avant d'entrer dans la chambre de traitement thermique 20.
  14. Procédé selon l'une quelconque des revendications 10 à 13, comprenant en outre :
    la fourniture d'une conduite de retour 42 de la chambre de traitement thermique 20 jusqu'à la première chambre de traitement 10 et la recirculation du gaz chaud à partir de la chambre de traitement thermique 20 jusqu'à la première chambre de traitement 10 via ladite conduite.
  15. Procédé selon l'une quelconque des revendications 10 à 14, comprenant en outre :
    la surveillance d'une caractéristique du gaz de synthèse indicative de la production de gaz de synthèse à partir de la première chambre de traitement 10,
    l'identification, à partir de ladite caractéristique surveillée, du moment où la cadence de production de gaz de synthèse à partir de la première chambre de traitement 10 devient inférieure à une première valeur prédéterminée, et
    l'augmentation de la teneur en oxygène dans la seconde chambre de traitement 26.
EP14717839.6A 2013-04-17 2014-04-14 Améliorations dans le traitement des déchets Active EP2986914B1 (fr)

Applications Claiming Priority (2)

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GB1306943.0A GB2513143B (en) 2013-04-17 2013-04-17 Improvements in waste processing
PCT/GB2014/051153 WO2014170647A1 (fr) 2013-04-17 2014-04-14 Améliorations dans le traitement des déchets

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EP2986914B1 true EP2986914B1 (fr) 2017-12-13

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DE112015006914T5 (de) * 2015-09-18 2018-05-30 Novelis Inc. Rotationsvorrichtung zur Entschichtung im Chargenbetrieb
CN108728140B (zh) * 2018-08-13 2024-02-06 湖南叶林环保科技有限公司 有机危废低温热解发电系统
GB201900676D0 (en) * 2019-01-17 2019-03-06 Chalabi Rifat Al Process for producing activated carbon and hydrogen

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ITRM20050207A1 (it) * 2005-05-02 2006-11-03 Pyrolb S R L Procedimento integrato per il trattamento di rifiuti mediante pirolisi e relativo impianto.
US20070266914A1 (en) * 2006-05-18 2007-11-22 Graham Robert G Method for gasifying solid organic materials and apparatus therefor
US20100319255A1 (en) * 2009-06-18 2010-12-23 Douglas Struble Process and system for production of synthesis gas
GB2471462B (en) * 2009-06-29 2014-02-26 Coldunell Ltd Waste management system
GB2470127B (en) * 2010-05-20 2011-03-23 Rifat A Chalabi Improvements in waste recycling
GB2488923B (en) * 2012-05-08 2013-02-20 Chinook Sciences Ltd Improvements in waste processing

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GB2513143A (en) 2014-10-22
WO2014170647A1 (fr) 2014-10-23
GB201306943D0 (en) 2013-05-29
EP2986914A1 (fr) 2016-02-24

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