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EP4036471B1 - Incinérateur de déchets - Google Patents

Incinérateur de déchets Download PDF

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Publication number
EP4036471B1
EP4036471B1 EP21153944.0A EP21153944A EP4036471B1 EP 4036471 B1 EP4036471 B1 EP 4036471B1 EP 21153944 A EP21153944 A EP 21153944A EP 4036471 B1 EP4036471 B1 EP 4036471B1
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EP
European Patent Office
Prior art keywords
flue gas
rotary kiln
heat exchanger
wet scrubber
waste incinerator
Prior art date
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Application number
EP21153944.0A
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German (de)
English (en)
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EP4036471A1 (fr
Inventor
Stanislav Paluda
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Individual
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Classifications

    • 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
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • 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
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/20—Rotary drum furnace
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/52002—Rotary drum furnaces with counter-current flows of waste and gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2213/00—Chimneys or flues
    • F23J2213/30—Specific materials
    • F23J2213/302—Specific materials plastic
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/50—Intercepting solids by cleaning fluids (washers or scrubbers)

Definitions

  • the present invention relates to improvements in waste incinerator plants.
  • Waste is currently treated by various technologies, including thermal treatment such as incineration. Competing technologies include recycling or landfilling. Recycling is not suitable for all types of waste, especially not for hazardous waste or for waste for which the cost of recycling is significantly higher than the cost of production. Landfilling is unsuitable for hazardous waste, and the European Union wishes to limit landfilling to minimum in the course of the next decade. Waste incineration is thus becoming a necessary and developing technology. To-day incinerators use a burner or furnace which is connected to a boiler, followed by a heat exchanger and a scrubber. The ashes and other solid residues are usually landfilled, and the gases are let out into the environment, after further cleaning when necessary.
  • the flue gas is subjected to treatment by scrubbing in order to remove chemical pollution and fine ashes.
  • the scrubbing may be dry scrubbing or wet scrubbing or a combination thereof. Dry scrubbing is more commonly used. Wet scrubbing produces a large amount of contaminated water. Semi-wet scrubbing using lime milk is a compromise between wet scrubbing and dry scrubbing.
  • the incinerators known in the art are typically adapted to a certain type of waste, require a significant amount of fuel, and produce emissions, which are usually within the set emission limits, but considering the amount of the solids and gases produced, it is desirable to further decrease the amount of emissions, i.e. emitted solids and hazardous gases. Furthermore, it is desirable to provide a stable working regimen without any problematic peak values of emissions or temperatures.
  • US 4,768,448 discloses a grate incinerator with a wet scrubber system provided with a filter press.
  • US 4,922,841 discloses a counter current drum incinerator with a dry gas cleaning system.
  • the present invention provides a waste incinerator which contains a rotary kiln the outlet of which is connected to secondary combustion chamber(s) which are in turn connected to a boiler connected to a heat exchanger which is further attached to a wet scrubber, and flue gas outlet of the wet scrubber is connected to a fan and a chimney, wherein
  • Counter current rotary kiln results in a more complete burning of the ash and less than half of the total amount of fly ash, compared to the commonly used co-current rotary kiln.
  • Counter current rotary kiln is also more suitable for burning trash comprising very varied materials.
  • the waste is incinerated in the counter current rotary kiln at temperature of at least 900 °C. In a stationary chamber of the rotary kiln, the temperatures may even exceed 1100 °C.
  • the counter current rotary kiln is provided with a slag and ash outlet in its lower part.
  • Prior art waste incinerators are typically provided with the slag and ash outlet at the bottom of secondary combustion chamber.
  • This prior art solution results in the content of unburnt carbon being about 4 % or more, due to lack of available oxygen.
  • sufficient supply of oxygen may be provided and the waste is burnt more completely, down to the content of the unburnt carbon well below 2 %.
  • Secondary combustion chamber(s) ensure complete burning of the remaining particles and matter in the flue gases.
  • the flue gas exiting the secondary retention chamber(s) is chemically stabilized.
  • the minimum total volume of secondary combustion chamber(s) is 1.8 times the volume of the rotary kiln. More preferably, the volume of secondary combustion chamber(s) is 1.8-3 times the volume of the rotary kiln. Most preferably, the volume of secondary combustion chamber(s) is 2-2.5 times the volume of the rotary kiln. Sufficient volume of secondary combustion chambers results in thorough burning of the waste and reduction of load on the following components of the incinerator plant. This leads to economically and environmentally effective operation of the plant.
  • At least two secondary combustion chambers in a more preferred embodiment three secondary combusion chambers are provided.
  • the necessary retention time of the flue gas in the secondary combusion chamber of 2 seconds was achieved by causing rotation of the flue gases using a suitably directed burner.
  • such solution causes unnecessary use of energy (gas) by the burner, and especially causes a peak increase of undesirable emissions upon the start of the burner, and are not needed in the present invention.
  • the use of at least two secondary combusion chambers having a sufficient total volume allows to achieve the retention time of significantly more than 2 seconds for the flue gas in a simple and effective way.
  • the flue gas must be maintained at a temperature of at least 850 °C in the secondary combustion chamber(s) for at least 2 seconds, as required by technological norms.
  • the herein described volume and optionally number of the secondary combustion chambers allows to increase the retention time to at least 5 seconds, preferably to at least 7 seconds.
  • the temperature of burning in the secondary combustion chambers is at least 1100 °C.
  • the boiler uses the heat of the flue gas to convert water into steam, the steam may be used as an energy resource, e.g., for heating or for producing electricity.
  • the heat exchanger allows to further decrease the temperature of the flue gas before it enters the wet scrubber.
  • the heat exchanger is configured to bring into thermal contact the flue gas entering the heat exchanger from the boiler or from the secondary combustion chamber(s) with the flue gas entering the heat exchanger from the wet scrubber.
  • a typical temperature of the hot flue gas (from the boiler or even directly from the secondary combustion chamber(s)) is about 400 to 800 °C, while a typical temperature of the cold flue gas (from the wet scrubber) is about 70 to 100 °C.
  • the heat exchanger is preferably configured to maintain the volume flow ratio of the hot flue gas to the cold flue gas from 2:1 to 1:2, more preferably about 1:1.
  • the heat exchanger contains substantially concentric tubes wherein the hot flue gas passess through the inner tube and the cold flue gas passes through the outer tube.
  • the closed liquid circulation includes at least two decanting tanks in which the solids are decanted, the decanted solid portion is moved to a filter press which, by pressing the decanted portion, produces a filter cake and returns the liquid back to the decanting tank or to the wet scrubber.
  • the liquid from the last decanting tank is returned to the wet scrubber to be used repeatedly for scrubbing the flue gas.
  • the wet scrubber may be configured to use water or aqueous hydroxide or lime solution to remove in particular acidic compounds (HCl, HF etc.) and/or sulfur oxides from the flue gas. Furthermore, the wet scrubber may be configured to utilize carriers (e.g., ring-shaped carriers) for deposition and removal of salts produced by wet scrubbing.
  • carriers e.g., ring-shaped carriers
  • the liquid in the wet scrubber preferably contains an alkali metal or an alkaline earth metal hydroxide, such as NaOH. This allows to remove acidic contaminants such as hydrochloric, hydrofluoric, sulfuric, nitric acids and acidic oxides.
  • the closed liquid circuit preferably contains a stock tank for storing hydroxide solution and for adding it to the wet scrubber liquid in a controlled manner.
  • the volume of wet scrubber is about 0.8 to 1.5 times the volume of the rotary kiln, more preferably the volume of wet scrubber is about the same as the volume of the rotary kiln.
  • the first decanting tank may or may not be connected to the filter press, while the second (and further) decanting tank is provided with a bottom outlet for solids or suspensions, said bottom outlet being connected to the filter press. This ensures that majority of the solids remains in the first decanting tank, and the second (or further) decanting tank(s) thus achieve(s) an additional fine cleaning, resulting in an increased purity of water which is returned to the wet scrubber.
  • the filter press functions more effectively especially in the arrangements in which the first decanting tank is not connected to the filter press - such an arrangement results in a lower load and thus an increased effectiveness of the filter press.
  • the overall effects of this arrangement include less frequent need for outages and less need for cleaning of the components of the wet scrubbing assembly.
  • the total volume of the decanting tanks is about 2-4 times the volume of the rotary kiln, more preferably about 3 times the volume of the rotary kiln.
  • the scrubbed flue gas existing from the wet scrubber then passes through the heat exchanger where it is employed to cool down the flue gas exiting the boiler or the secondary combustion chamber before the flue gas enters the wet scrubber.
  • the wet scrubber may be followed by a filter to remove the remaining solid and ash particles from the flue gas, and/or by sorbent columns for adsorbing remaining gaseous contaminants.
  • filters and sorbent columns are known to a person skilled in the art and are commonly used in waste incinerators.
  • the filters located between the heat exchanger and the fan may include a dioxin filter or a mechanical filter for filtering off solids.
  • the fan ensures the movement of flue gas through the device.
  • the low pressure (vacuum) generated by the fan draws the flue gas from the rotary kiln and through the device.
  • the pipes connecting the individual components are typically made of metals such as steel.
  • metallic tubes are mechanically rigid and tend to collect deposits of solid particles and ashes in any bends or elbows, thus requiring regular cleaning which requires outages.
  • metallic straight parts of the piping and plastic elbows or bends are flexible and tend to slightly vibrate, thus not collecting the solid deposits to a significant extent. This further increases time between maintenance outages.
  • the plastic material must be selected so that it withstands the relevant temperatures - this information is available from producers of various plastics.
  • the present invention further encompasses a method of incineration of waste, comprising the steps of:
  • the present invention thus provides improvements in waste incinerators which lead to surprisingly significant decrease in emissions, and which result in significantly less frequent need for maintenance outages.
  • FIG. 1 An example embodiment of the present invention is schematically shown in Figure 1 .
  • the arrows in the figure show the direction of the flow of the waste and of the flue gas.
  • the waste incinerator has a waste inlet 1 through which the waste to be incinerated enters the system and is led to a counter current rotary kiln 2.
  • the rotary kiln 2 is provided with a slag and ash outlet 3 at its lower part.
  • the waste is burnt in the rotary kiln 2 and converted into flue gas.
  • the flue gas exits the rotary kiln via outlet 4 and enters secondary combustion chambers 51 and 52, one after another.
  • the flue gas exiting from the secondary combustion chamber 52 may enter the boiler 6, or may by-pass the boiler. In the boiler 6, the flue gas transfers energy to water, thus producing steam which can be used in downstream technologies or heating.
  • the water from the boiler 6 or from the by-pass enters a heat exchanger 7 in which it is brought into thermal contact with cold flue gas from wet scrubbing.
  • the cooled flue gas from the heat exchanger 7 enters a wet scrubber 8.
  • the wet scrubber 8 is provided with two decanting tanks 91 and 92.
  • the decanting tanks 91 and 92 are connected by a tube in approximately the upper third of their height.
  • Water from the wet scubber 8 enters the the decanting tank 92 where larger solid particles precipitate. Water then passes into the decanting tank 91 via the connecting tube which is in a height which ensures that only fine suspension enters the decanting tank 91. From the tank 91 water is led back to the wet scrubber 8.
  • the scrubbed flue gas exiting the wet scrubber 8 is led back to the heat exchanger 7 to cool down the flue gas to be scrubbed.
  • the exit of the cold flue gas from the heat exchanger 7 leads the flue gas to a filter 11 and dioxin filter 12, and then via a fan into a chimney 13.
  • Secondary combustion chambers 51 and 52 have a total volume of about 2 times the volume of the rotary kiln 2.
  • the decanting tanks 91 and 92 have a total volume of about 3 times the volume of the rotary kiln 2, and the ratio of volumes of the tanks 91 and 92 is about 1:1.
  • the wet scrubber 8 has about the same volume as the rotary kiln.
  • Example 1 The embodiment described in Example 1 was compared with a comparative embodiment shown in Figure 2 which contained a waste inlet 101, a counter current rotary kiln 102 equipped with a slag and ash outlet 103 in its lower part.
  • Outlet 104 is connected to secondary combustion chambers 151, 152, which are in turn connected to a boiler 106 (which can be by-passed) from which the flue gas is led to a heat exchanger 107 followed by a wet scrubber 108.
  • the wet scrubber is provided with one decanting tank 109 provided with a filter press 110.
  • the flue gas from the wet scrubber 108 is led directly into a filter 111 and dioxin filter 112, followed by a fan and a chimney 113.
  • the amounts of contaminants and emissions were measured in samples drawn from a sampling spot located in the chimney, downstream from the fan.
  • the content of solid contaminants (TZL) was measured gravimetrically, SO 2 was measured using UV spectrometry, CO was measured using infrared spectrometry, NO x was measure unsing chemiluminescence, O 2 was measured using paramagnetic measurements, total organic carbon (TOC) was measured using by gas chromatography with flame ionization detection. Content of solid particles of size fractions PM 10 and PM 2.5 were calculated as 85% and 60% proportion of TZL. The measurements and calculations were carried out by a certified laboratory service.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)

Claims (12)

  1. Incinérateur de déchets qui contient un four rotatif (2) dont la sortie (4) est reliée à une ou des chambre(s) de combustion secondaire(s) (51, 52) qui sont à leur tour reliées à une chaudière (6) reliée à un échangeur de chaleur (7) qui est relié à un épurateur (8) par voie humide, et la sortie des gaz de combustion de l'épurateur (8) par voie humide est reliée à un ventilateur et à une cheminée (13),
    caractérisé en ce que
    - le four rotatif (2) est un four rotatif à contre-courant,
    - le épurateur (8) par voie humide comporte circuit de liquide fermé muni d'au moins deux bacs de décantation (91, 92) et d'un filtre-presse (10), et
    - la sortie des gaz de combustion de l'épurateur (8) par voie humide est reliée au ventilateur et à la cheminée (13) par l'échangeur de chaleur (7).
  2. Incinérateur de déchets selon la revendication 1, où le four rotatif (2) à contre-courant est pourvu dans sa partie inférieure d'une sortie (3) de scories et de cendres.
  3. Incinérateur de déchets selon la revendication 1 ou 2, où le volume minimum de la ou des chambre(s) de combustion secondaire(s) (51, 52) est de 1,8 fois le volume du four rotatif (2).
  4. Incinérateur de déchets selon l'une quelconque des revendications 1 à 3, où au moins deux chambres de combustion secondaires (51, 52) sont prévues.
  5. Incinérateur de déchets selon l'une quelconque des revendications 1 à 4, où l'échangeur de chaleur (7) est configuré pour mettre en contact thermique des fumées chaudes entrant dans l'échangeur de chaleur (7) en provenance de la chaudière (6) ou de la ou des chambre(s) de combustion secondaire(s) (51, 52) avec des gaz de combustion froids entrant dans l'échangeur de chaleur (7) à partir de l'épurateur (8) par voie humide, et pour maintenir le rapport de débit volumique des gaz de combustion chauds sur les gaz de combustion froids de 2:1 à 1:2, plus préférablement environ 1:1.
  6. Incinérateur de déchets selon l'une quelconque des revendications 1 à 5, où l'échangeur de chaleur (7) contient des tubes sensiblement concentriques dans lesquels les fumées chaudes traversent le tube interne et les fumées froides traversent le tube externe.
  7. Incinérateur de déchets selon l'une quelconque des revendications 1 à 6, où le volume de l'épurateur (8) par voie humide est de 0,8 à 1,5 fois le volume du four rotatif (2).
  8. Incinérateur de déchets selon l'une quelconque des revendications 1 à 7, où le volume des bacs de décantation (91, 92) est d'environ 2 à 4 fois le volume du four rotatif (2).
  9. Incinérateur de déchets selon l'une quelconque des revendications 1 à 8, où les au moins deux bacs de décantation (91, 92) sont orientés verticalement et reliés par un tube dans leur moitié supérieure, de préférence dans leur tiers supérieur.
  10. Incinérateur de déchets selon l'une quelconque des revendications 1 à 9, où le premier bac de décantation (92) n'est pas relié au filtre-presse (10), tandis que le deuxième bac de décantation (91) est pourvu d'une sortie inférieure pour les solides ou des suspensions, ladite sortie inférieure étant reliée au filtre-presse (10).
  11. Incinérateur de déchets selon l'une quelconque des revendications 1 à 10, où les parties rectilignes des tuyaux reliant les composants individuels sont en métal tel que l'acier, et au moins certains coudes des tuyaux sont en plastique.
  12. Procédé d'incinération de déchets, comprenant les étapes de:
    - incinérer les déchets dans un four rotatif (2) à contre-courant pour produire des gaz de combustion,
    - acheminer les gaz de combustion du four rotatif (2) via la ou les chambre(s) de combustion secondaire(s) (51, 52) vers une chaudière (6) ou un échangeur de chaleur (7), où les gaz de combustion sont retenus dans la ou les chambre(s) de combustion secondaire(s) (51, 52) pendant au moins 5 secondes à une température d'au moins 850 °C;
    - dans l'échangeur de chaleur (7), transférer l'énergie des gaz de combustion provenant de la chaudière (6) ou de la ou des chambre(s) de combustion secondaire(s) (51, 52) aux gaz de combustion provenant de l'épurateur (8) par voie humide,
    - lavage humide des gaz de combustion provenant de l'échangeur de chaleur (7) dans l'épurateur (8) par voie humide, et recyclage de l'eau de lavage à travers au moins deux bacs de décantation (91, 92) en circuit liquide fermé,
    - acheminer les gaz de combustion, éventuellement via des filtres (11, 12), vers un ventilateur et une cheminée (13), le ventilateur provoquant le mouvement des gaz de combustion à travers les composants de l'incinérateur.
EP21153944.0A 2021-01-28 2021-01-28 Incinérateur de déchets Active EP4036471B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP21153944.0A EP4036471B1 (fr) 2021-01-28 2021-01-28 Incinérateur de déchets

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP21153944.0A EP4036471B1 (fr) 2021-01-28 2021-01-28 Incinérateur de déchets

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Publication Number Publication Date
EP4036471A1 EP4036471A1 (fr) 2022-08-03
EP4036471B1 true EP4036471B1 (fr) 2023-09-13

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Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2590805B1 (fr) * 1985-12-02 1990-02-09 Propiorga Procede et installation de neutralisation de fumees acides provenant notamment de la combustion de residus
US4922841A (en) * 1988-09-14 1990-05-08 Kent John M Method and apparatus for using hazardous waste to form non-hazardous aggregate
US5090498A (en) * 1989-11-10 1992-02-25 M-I Drilling Fluids Company Water wash/oil wash cyclonic column tank separation system
DE102017108705A1 (de) * 2017-04-24 2018-10-25 Rea Plastik Tech Gmbh Verfahren sowie Vorrichtung zur Reinigung und Wiederaufheizung von Rauchgas

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