EP0376971B1 - Procede et installation de recuperation par pyrolyse de gaz reutilisables contenus dans des dechets - Google Patents

Procede et installation de recuperation par pyrolyse de gaz reutilisables contenus dans des dechets Download PDF

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Publication number
EP0376971B1
EP0376971B1 EP88907293A EP88907293A EP0376971B1 EP 0376971 B1 EP0376971 B1 EP 0376971B1 EP 88907293 A EP88907293 A EP 88907293A EP 88907293 A EP88907293 A EP 88907293A EP 0376971 B1 EP0376971 B1 EP 0376971B1
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EP
European Patent Office
Prior art keywords
gas
water
washing
pyrolysis residue
installation
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.)
Expired - Lifetime
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EP88907293A
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German (de)
English (en)
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EP0376971A1 (fr
Inventor
Bernd Michael Wolf
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PKA Pyrolyse Kraftanlagen GmbH
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PKA Pyrolyse Kraftanlagen GmbH
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Priority to AT88907293T priority Critical patent/ATE69614T1/de
Priority to IN689/CAL/88A priority patent/IN170715B/en
Publication of EP0376971A1 publication Critical patent/EP0376971A1/fr
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Publication of EP0376971B1 publication Critical patent/EP0376971B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • 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
    • C10K1/02—Dust removal
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • the invention relates to a method for recovering usable gas from waste by pyrolysis according to the preamble of claim 1.
  • a system for carrying out the method for this is described in the preamble of claim 11.
  • the object of the present invention is to achieve a further reduction in environmentally harmful substances requiring disposal while maintaining a low-wastewater treatment process, with a further improvement in the efficiency of the system possibly being achieved at the same time.
  • this object is achieved in that at least a portion of the amount of liquid withdrawn from the wash water circuit of the gas washing system is introduced into the water bath through which the pyrolysis residues are discharged from the degassing drum, the impurities of the carbonization gas contained in the wash water being bound by the pyrolysis residue.
  • the pyrolysis residue absorbs more than 140 percent by weight of its own weight in liquid with a sufficient residence time.
  • a sufficient dwell time for total wetting should be maintained, which can be achieved, for example, by a screw conveyor system with a correspondingly slow speed.
  • the garbage entered in the degassing drum is previously removed by sorting out inert substances. This can be done using suitable sorting devices such as, for example, comb roller sorters.
  • the pyrolysis residue is introduced as an activated carbon filter into a filter device behind the drying tower of the gas washing system.
  • Sulfur components of the pyrolysis gas which mainly depend on the sulfur content of the coke used in the gas converter, are known to be difficult to remove from the pyrolysis gas. If you now connect a filter device to the gas scrubber, sulfur or fluorine compounds that have not been fully washed out can be absorbed by the activated carbon filter. Because the pyrolysis residues are used for this purpose, there are no significant additional costs and the pyrolysis residues are even put to sensible use in this way. This also means that the sulfur content in the exhaust gas is reduced cost-effectively far below the prescribed air limit values, which means that coke with a somewhat higher sulfur content can also be used inexpensively as a further advantage in the gas converter.
  • pollutant components from other productions can advantageously be disposed of in such a way that they are mixed with the liquid portion withdrawn from the water cycle. This means that in addition to the company's own almost pollution-free treatment of waste, the method according to the invention can still be used to remove pollutants from other plants.
  • the amount of wastewater from a pyrolysis gas plant that processes household waste is reduced by more than 50% and that in general, less than 100 liters of wastewater per ton of household waste disposal.
  • This amount of waste water is usually so polluted that untreated discharge is ecologically undesirable.
  • it can be achieved a significant and cost-effective reduction in pollutant pollution if it is provided in a further development according to the invention that the amount of liquid withdrawn from the water circuit of the gas washing system is pretreated in batches by ozone injection so that after the treatment the concentration of cyanide ⁇ 10 g / m3 and or phenols ⁇ 40 g / m3.
  • Such a pyrolysis residue which has a liquid content of approx. 60 percent by weight, is a particularly nutrient-rich carrier substance for anaerobic methane gas generators, which convert the absorbed biologically convertible groups of substances into useful gas, due to the balanced load values of phenols and cyanides due to the high carbon and ammonium content from gas scrubbing.
  • the ozone-controlled homogenization of the pollutants minimizes the risk of overdoses and thus the destruction of culture.
  • a short ozonization which is generally less than a quarter of a full ozonization time, is sufficient to achieve this homogenization effect.
  • the excess water not bound by the pyrolysis residue which generally corresponds to less than 50% of the portion withdrawn from the water cycle of the gas washing system, is fed to a rest ozonization. This can be done either in parallel with a use in a biogas plant or instead.
  • the COD can be reduced to below 400 mg oxygen per liter, the BOD to approx. 60 mg / m3 and the proportion of cyanide and phenols to generally below 0.1 g / m3.
  • this pyrolysis residue can be used for the energetic supply in lime kilns.
  • it can preferably be pressed into egg briquette-like pellets.
  • its calorific value may correspond approximately to that of lignite, which is sufficient for a smelting process. If the correct mixing ratios are observed, the inert substances are calcined or ceramized, which in particular also includes heavy metals.
  • ceramization of the metals is that the molar ratio of SiO2, Al2O3, CaO. ZnO, Fe2O3 and / or MgO on the one hand to the total molar proportion of the metals lead, chromium, manganese, cadmium, berilium, barium, selenium, arsenic, vanadium, antimony, bismuth, strontium and / or zircon is at least 6: 1.
  • a prerequisite for the integration of sulfur, chlorine and fluorine compounds is that the molar ratio of calcium, magnesium and sodium on the one hand to the total sulfur, chlorine and fluorine is at least 2: 1.
  • the mixing product should contain a maximum of 40 percent by weight of liquid and the calorific value should be at least 100 kilocalories / kg so that the fuel, for example, placed in a lime kiln, with the necessary dwell time and temperature can burn up, whereby the introduced metals oxidize and are taken up in the melts of CaO and MgO, where they form relatively inert ceramic complexes.
  • Sulfur compounds are absorbed as sulfites or sulfates, liquid chlorine and fluorine are bound to CaCl2 and CaF2.
  • the available useful energy can increase by more than 5% through a reduction in the own electricity requirement for the ozone plant for gas cleaning and through the improved energetic use of the pyrolysis residue.
  • the residues requiring final storage in the method according to the invention are several times smaller than the residues in a waste incineration plant, which are also highly toxic and must be disposed of as special waste.
  • the garbage is conveyed via a conveyor belt 1 into a primary crusher 2 for coarse crushing, a conveyor trough 3 and a conveyor belt 4 with a magnetic separating device 5 Garbage in a sorting device 6.
  • the heavier, wet, vegetable fraction is separated and falls into an underlying container or onto a conveyor belt 7.
  • inert substances can also be separated off in order to increase the carbon content of the pyrolysis substance.
  • the remaining waste fraction is fed to a thermal screw press 14 via a further conveyor belt 8, a further shredding device 9 and a downstream hydrocyclone 10, in which heavy parts are separated again via a line 11.
  • the waste together with the separated waste from the container 7 is fed via a feed line 12 to a biogas plant 13, which can be preceded by a fluid classifier for the pre-selection of inert heavy parts, which works, for example, according to the flushing method.
  • the formation of granules in a rapidly degassable structure and a size of approximately 3 to 50 mm is achieved in a known manner by frictional pressure at approximately 110 to 150 degrees Celsius.
  • fluff ie a loose waste form, or pellets, ie waste constituents compressed into briquettes
  • the waste components crushed in this way pass through a rotary valve 15 or other entry devices, such as stuffing screws in a degassing drum 16, in which carbonization gas is generated in a known manner at temperatures of 450 to 600 degrees Celsius, which is introduced into a high-temperature gas converter 19 via a discharge line 17 and a dust separating device 18.
  • the processing or conversion of the carbonization gas takes place in the gas converter 19 over a coal or coke bed.
  • a gas converter of this type is described, for example, in DE-A-33 17 977.
  • the gas After passing through a heat exchanger 20, the gas passes into a gas scrubbing system which essentially consists of a water spray tower 21, a blower 22 and a cleaning cylon 23 and a droplet separator 24. Via a gas line 25, the cleaned gas reaches a gasometer 26, in which excess gas can be supplied to a flaring device 28 if too much gas is supplied via a secondary line 27.
  • a gas scrubbing system which essentially consists of a water spray tower 21, a blower 22 and a cleaning cylon 23 and a droplet separator 24.
  • the cleaned gas Via a gas line 25, the cleaned gas reaches a gasometer 26, in which excess gas can be supplied to a flaring device 28 if too much gas is supplied via a secondary line 27.
  • the gas normally passes from the gasometer 26 to a gas engine 29, which is connected to a generator 30, the burned exhaust gases being introduced into a chimney 32 via an exhaust gas line 31.
  • the gas converter 19 receives water via a line 33 and 34 coke via a coke inlet. Ash and slag is over a discharge line 35 is discharged. Possibly. To save energy, a coke return line 36 can also be provided for the coke freed from the slag.
  • a branch line 37 branches off from the gas line 25 and leads to a gas burner 38 which serves to supply heat to the degassing drum 16.
  • a gas burner 38 which serves to supply heat to the degassing drum 16.
  • an oil burner 39 or a separate gas burner is used to heat the smoldering drum. Subsequently, during operation, however, the heat required for the degassing drum 16 can be completely covered by the burner 38.
  • the scrubbing water obtained during gas cleaning passes into a scrubbing water tank 40 and then into a filter device 41 (usually a settling tank). Separated solids in the filter device are introduced into an ash container 43 via a line 42. The residues are removed from the ash container 43 via a discharge line 44 and introduced into the smoldering drum 16 again via the insertion device, possibly a cellular wheel sluice 15.
  • the cleaned washing water returns from the filter device 41 via a return line 45 after passing through a cooling tower 46 back into the spray tower 21 of the gas washing system.
  • a part of the cleaned wash water is in a Wash water neutralization system 47 is introduced, into which the vapor vapor condensate from the thermal screw press 14 is also introduced via a line 58, provided that it is not fed via line 65 to the reservoir 53 of the biogas system.
  • the wash water reaches the spray tower 21 via a return line 78 for circuit treatment, while a partial quantity reaches a circuit water batch treatment system 48 via a partial quantity removal line 79.
  • the washing water is chemically cleaned therein by appropriate chemicals, which are entered via line 49, provided that the chemical oxidation is not replaced by ozonization, as a result of which the residue-increasing additive addition can be greatly reduced.
  • the washing water is partially removed via a circuit line 50. passed through an air filter 51 to remove foams, exhaust gases being blown off through a line 52 over the chimney 32, and partly. there is a return via a line 80 into the spray tower 21.
  • the chemically and mechanically cleaned water passes from the circulating water batch treatment system 48 via a line 71 into the preliminary tank 53 of the biogas system. If necessary, sewage sludge, raw compost can also be placed in the storage tank or the like. What is indicated by the arrow "54".
  • the vapor vapor condensate if it has not been passed through the circulating water batch treatment system 48, can be introduced directly into the preliminary container 53 via a line 65.
  • the substances to be worked up in the biogas plant 13 arrive in a hydrolysis stage or a hydrogenator 56 from the pre-tank 53.
  • a countercurrent heat exchanger 57 connects to the hydrolysis stage 56 and receives its heat through a hot water line 62, which comes from the cooling tower 46 of the wash water cleaning system branches.
  • a coil heating system ensures a temperature rise in the methane area of the septic tank of 33 to 37 degrees Celsius. In this way, the excess heat from the pyrolysis plant is used for the biogas plant 13.
  • the biogas plant 13 is constructed in the usual way. As a phase-separated biogas plant, it can have a normal acid phase in the upper region in the middle shaft 63, while an acetic acid phase is present in the lower region.
  • the methane gas formed is drawn off via a methane gas line 59 and fed to the gas line 25 or the gas washing system of the pyrolysis system for cleaning via a buffer 60 and a compressor 61.
  • the digestate is discharged through a suction line 66 and a pre-dewatering device 68 fed, whereby it is brought to about 20% dry matter.
  • the solids contained in the fermentation residue can be brought to approx. 85% dry matter via a dry press 69.
  • the remaining fermentation water is collected in a lagoon 70 and, if necessary, fed to the treatment plant 48 or fed directly into the sewage system.
  • the substances separated in the circulating water batch treatment plant 48 can be fed to a sewage treatment plant via a line 64.
  • Pyrolysis residues are discharged in the degassing drum 16 via a water bath 72, the discharge e.g. can take place via screw conveyors.
  • the water bath 72 is supplied with the liquid required for wetting the pyrolysis residue via a partial liquid line 73.
  • the partial quantity line 73 branches off from the batch treatment system 48.
  • the pyrolysis residue wetted with liquid in this way is discharged via a line and can optionally be fed to the biogas plant 13 after treatment, for example ozonization or other cleaning.
  • the biogas plant 13 is of course only mentioned for example. It is not necessary for the invention itself. Instead of one Introducing the pyrolysis residues into the biogas plant 13, the pyrolysis residues can, if necessary, also be transported via a line 74 A to a lime kiln 77.
  • the pyrolysis residue can be introduced via a line 74 B after it has dried into a filter device 75 as an activated carbon filter.
  • the filter device 75 is located between the gas washing system and the gasometer 26.
  • the activated carbon obtained from the pyrolysis residue should be at least largely free of pollutants. This means that one operates in batches and introduces fresh water through a fresh water line 81 into the water bath instead of a water supply via the partial liquid quantity line 73 with contaminated circulating water.
  • the liquid portion removed from the water cycle can also be treated in an ozone injection system 76.
  • the ozone system 76 is connected to the batch treatment system 48. If the partial quantity withdrawn from the circuit via the partial quantity extraction line 79 is appropriately cleaned before it is introduced via the liquid partial quantity line 73 into the water bath 72 in the ozone system 76, the pyrolysis residue can also be used as an activated carbon filter in the filter device 75 in this procedure.
  • the function and mode of operation of a lime kiln 77, into which the pyrolysis residue is introduced via line 74 A, are generally known, which is why it is not discussed in more detail here.
  • the pyrolysis residue may be used as fuel together with other fuel components.
  • a direct line 74 A is present between the water bath 72 and the lime kiln 77.
  • the system according to the invention is designed so that not all units have to be in one place. For example, the biogas plant 13 and the lime kiln 77 are at a different location, and the substances can be transported there in any way.
  • the partial liquid quantity which has not been completely absorbed by the pyrolysis residue in the water bath 72 can, if necessary, also be passed through the ozone system 76, if necessary for full ozonization, before it is introduced into a sewage treatment plant.

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  • 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)
  • Processing Of Solid Wastes (AREA)
  • Medicines Containing Plant Substances (AREA)
  • Coke Industry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)
  • Treating Waste Gases (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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Claims (13)

1. Procédé de récupération de gaz utilisable par pyrolyse d'ordures, dans lequel les ordures préalablement déchiquetées sont préparées en vrac, en granulés ou en boulettes agglomérees d'une taille de 1 à 50 mm, sont portées à un taux de substances sèches d'au moins 75% et sont ensuite introduites dans un tambour de dégazage chauffé dans lequel du gaz de distribution est produit et séparé des résidus tels que des cendres et d'autres composants, et où le gaz de distillation est décomposé, dans un convertisseur de gaz, en gaz combustible qui est lavé dans une installation subséquente de lavage par de l'eau en circuit fermé où, pour limiter la concentration en polluants dans l'eau du circuit de lavage de gaz, une fraction de l'eau de lavage est prélevée et remplacée par de l'eau propre, et où les résidus de pyrolyse à évacuer du tambour de distillation sont évacués à travers un bain d'eau, caractérisé en ce qu'au moins une partie de la fraction de liquide prélevée au circuit fermé de l'installation de lavage de gaz (21-24 et 47-51) est introduite dans le bain d'eau (72), de sorte que les polluants du gaz de distillation qui se trouvent dans l'eau de lavage sont fixés par le résidu de pyrolyse.
2. Procédé selon la revendication 1, caractérisé en ce que, dans les ordures introduites dans le tambour de dégazage (16), des matières inertes sont retirées au préalable par triage en quantité telle que les résidus de pyrolyse évacués du tambour de dégazage contiennent au moins 25% en poids de carbone.
3. Procédé selon la revendication 1, caractérisé en ce que le résidu de pyrolyse traité avec la fraction prélevée au circuit d'eau de lavage est employé comme filtre à charbon actif.
4. Procédé selon la revendication 3, caractérisé en ce que le résidu de pyrolyse servant de filtre à charbon actif est introduit dans un dispositif de filtration (75) en aval de l'installation de lavage de gaz (21-24).
5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que des composants polluants provenant d'autres productions sont mélangés au concentrat d'eau prélevé au circuit d'eau de lavage, en vue de leur traitement.
6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce que la fraction de liquide prélevée au circuit d'eau de l'installation de lavage de gaz est traitée par charges par injection d'ozone de manière à avoir, après le traitement, une concentration en cyanures ≦ 10 g/m3 et/ou une concentration en phénols < 40 g/m3.
7. Procédé selon l'une des revendications 1 à 5, caractérisé en ce que la fraction de liquide qui est prélevée au circuit d'eau de l'installation de lavage de gaz et qui n'est pas absorbée par le mouillage du résidu de pyrolyse est soumise à une autre ozonisation par charges, jusqu'à ce que sa DCO soit inférieure à 400 mg O₂/litre.
8. Procédé selon la revendication 1, caractérisé en ce que le résidu de pyrolyse mouillé par le liquide est introduit dans des installations d'épuration ou à biogaz (13).
9. Procédé selon la revendication 1, caractérisé en ce que le résidu de pyrolyse mouillé par le liquide est introduit dans des fours à chaux (77).
10. Installation pour la mise en oeuvre du procédé selon l'une des revendications 1 à 9, comportant un dispositif de déchiquetage des ordures, un dispositif de séchage et un tambour de dégazage pourvu d'une entrée pour les ordures déchiquetées au préalable, d'une sortie pour des résidus solides de pyrolyse et d'une conduite d'extraction de gaz de distillation à laquelle est raccordé un convertisseur de gaz pour l'obtention de gaz de craquage, une installation de lavage de gaz disposée en aval du convertisseur de gaz, et un bain d'eau adjacent à la sortie des résidus de pyrolyse pour l'évacuation de ceux-ci, caractérisée en ce qu'une conduite (73) pour une fraction de liquide va d'un dispositif (48) de l'installation de lavage de gaz au bain d'eau (72).
11. Installation selon la revendication 10, caractérisée en ce qu'un dispositif de triage (6) est disposé en amont du tambour de dégazage (16), pour trier des matières inertes.
12. Installation selon la revendication 10 ou 11, caractérisée en ce qu'un dispositif de filtration (75), dans lequel le résidu de pyrolyse peut être employé comme filtre à charbon actif, est disposé en aval de l'installation de lavage de gaz (21-24 et 47-51).
13. Installation selon l'une des revendications 10 à 12, caractérisée en ce qu'un dispositif d'injection d'ozone (76) est prévu pour la fraction de liquide prélevée au circuit d'eau de l'installation de lavage de gaz (21-24).
EP88907293A 1987-08-13 1988-08-03 Procede et installation de recuperation par pyrolyse de gaz reutilisables contenus dans des dechets Expired - Lifetime EP0376971B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AT88907293T ATE69614T1 (de) 1987-08-13 1988-08-03 Verfahren und anlage zur rueckgewinnung von verwertbarem gas aus muell durch pyrolyse.
IN689/CAL/88A IN170715B (fr) 1987-08-13 1988-08-16

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19873727004 DE3727004A1 (de) 1987-08-13 1987-08-13 Verfahren und anlage zur rueckgewinnung von verwertbarem gas aus muell durch pyrolyse
DE3727004 1987-08-13

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Publication Number Publication Date
EP0376971A1 EP0376971A1 (fr) 1990-07-11
EP0376971B1 true EP0376971B1 (fr) 1991-11-21

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EP88907293A Expired - Lifetime EP0376971B1 (fr) 1987-08-13 1988-08-03 Procede et installation de recuperation par pyrolyse de gaz reutilisables contenus dans des dechets

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Country Link
EP (1) EP0376971B1 (fr)
KR (1) KR960010986B1 (fr)
AT (1) ATE69614T1 (fr)
AU (1) AU2326288A (fr)
BR (1) BR8807663A (fr)
CA (1) CA1335863C (fr)
CS (1) CS274679B2 (fr)
DD (1) DD282023A5 (fr)
DE (2) DE3727004A1 (fr)
DK (1) DK35890D0 (fr)
ES (1) ES2007989A6 (fr)
FI (1) FI900660A0 (fr)
GR (1) GR1000301B (fr)
IN (1) IN170715B (fr)
NO (1) NO174002C (fr)
PL (1) PL154803B1 (fr)
RU (1) RU1836406C (fr)
WO (1) WO1989001505A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103624059A (zh) * 2012-08-22 2014-03-12 黄广禧 一种生活垃圾裂解处理工艺流程
CN103624055A (zh) * 2012-08-22 2014-03-12 黄广禧 利用秸秆与生活垃圾混合裂解抑制二恶英产生的方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3933809A1 (de) * 1989-10-10 1991-04-18 Pyrolyse Kraftanlagen Pka Verfahren zur entsorgung von abfallstoffen
DE4009249A1 (de) * 1990-03-22 1991-09-26 Pyrolyse Kraftanlagen Pka Verfahren und anlage zur reinigung von abwaessern
EP0495766A3 (en) * 1991-01-14 1992-12-23 Tbr Gesellschaft F. Techn. Bodenreinigung Ges.M.B.H. Method for the utilization of residual material from pyrolysis and of pyrolysis gas
CN110026268B (zh) * 2017-12-03 2020-08-14 保定雄盛建材加工有限公司 一种具有防尘功能的矿石碎石机
CN107974261A (zh) * 2017-12-27 2018-05-01 利百川环保科技有限公司 一种生活垃圾废水废气处理系统

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Publication number Priority date Publication date Assignee Title
US3862887A (en) * 1971-12-22 1975-01-28 Monsanto Enviro Chem Syst Method for processing heat-decomposable non-gaseous materials
US4126000A (en) * 1972-05-12 1978-11-21 Funk Harald F System for treating and recovering energy from exhaust gases
DE2423891A1 (de) * 1974-05-16 1975-12-04 Alfred Denne Verfahren zur gewinnung von adsorptionskohle aus der bei einem an sich bekannten muellverkokungsverfahren anfallenden muellschlacke sowie vorrichtung zur durchfuehrung des verfahrens
FI782355A (fi) * 1977-08-12 1979-02-13 Adolf H Borst Foerfarande foer kombinerat soputnyttjande och avfallsvattentillverkande och flerstegsfiltreringsanordning foer att genomfoera foerfarandet
US4256574A (en) * 1979-09-12 1981-03-17 Sterling Drug Inc. Ozone disinfection system
DE3347554C2 (de) * 1983-05-18 1986-08-07 Pka Pyrolyse Kraftanlagen Gmbh, 7080 Aalen Verfahren zur Gewinnung von verwertbarem Gas aus Müll durch Pyrolyse und Vorrichtung zum Durchführen des Verfahrens
DE3317977A1 (de) * 1983-05-18 1984-11-22 Pka Pyrolyse Kraftanlagen Gmbh, 7080 Aalen Gaswandler
DE3529445A1 (de) * 1985-08-16 1987-02-26 Pyrolyse Kraftanlagen Pka Verfahren zur rueckgewinnung von verwertbarem gas aus muell

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103624059A (zh) * 2012-08-22 2014-03-12 黄广禧 一种生活垃圾裂解处理工艺流程
CN103624055A (zh) * 2012-08-22 2014-03-12 黄广禧 利用秸秆与生活垃圾混合裂解抑制二恶英产生的方法

Also Published As

Publication number Publication date
DE3866357D1 (de) 1992-01-02
IN170715B (fr) 1992-05-09
AU2326288A (en) 1989-03-09
RU1836406C (ru) 1993-08-23
FI900660A0 (fi) 1990-02-09
DE3727004A1 (de) 1989-02-23
GR1000301B (el) 1992-05-12
NO174002B (no) 1993-11-22
PL154803B1 (en) 1991-09-30
DK35890A (da) 1990-02-12
KR960010986B1 (ko) 1996-08-14
CS274679B2 (en) 1991-09-15
WO1989001505A1 (fr) 1989-02-23
NO174002C (no) 1994-03-02
BR8807663A (pt) 1990-06-19
DK35890D0 (da) 1990-02-12
NO900670L (no) 1990-02-12
CS559288A2 (en) 1990-10-12
KR890701712A (ko) 1989-12-21
NO900670D0 (no) 1990-02-12
ATE69614T1 (de) 1991-12-15
PL274155A1 (en) 1989-04-17
ES2007989A6 (es) 1989-07-01
DD282023A5 (de) 1990-08-29
EP0376971A1 (fr) 1990-07-11
CA1335863C (fr) 1995-06-13
GR880100514A (en) 1989-05-25

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