WO1998016593A1 - Procede et installation pour le traitement de dechets solides par thermolyse - Google Patents
Procede et installation pour le traitement de dechets solides par thermolyse Download PDFInfo
- Publication number
- WO1998016593A1 WO1998016593A1 PCT/FR1997/001839 FR9701839W WO9816593A1 WO 1998016593 A1 WO1998016593 A1 WO 1998016593A1 FR 9701839 W FR9701839 W FR 9701839W WO 9816593 A1 WO9816593 A1 WO 9816593A1
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- WO
- WIPO (PCT)
- Prior art keywords
- gases
- thermolysis
- line
- zone
- uncondensed
- Prior art date
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Classifications
-
- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
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- 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
- C10B7/00—Coke ovens with mechanical conveying means for the raw material inside the oven
- C10B7/14—Coke ovens with mechanical conveying means for the raw material inside the oven with trucks, containers, or trays
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/18—Treating trash or garbage
Definitions
- the present invention relates to a method and an installation for the treatment by thermolysis of solid products, the rejection of which is harmful to the environment.
- the pumping means communicate by a fuel gas inlet line with a boiler intended to burn the thermolysis gases which are maintained at a temperature higher than the condensation temperature of the tars capable of forming in the gaseous state during thermolysis, before their application as fuel in the boiler.
- the thermolysis gases were thus used directly to generate thermal energy which was either transformed in the installation, or applied to a turbine which converts it into electrical form, or used for any other function, possibly foreign to it. 'installation.
- the boiler could also use fuel (coal) contained in solid residues. The boiler fumes were used to heat the dehydration zone.
- thermolytic transformation In order to be able to carry out the thermolytic transformation in the total absence of free oxygen, the dehydration, thermolysis and cooling zones were formed by chambers insulated from one another in a substantially sealed manner.
- the dehydration and thermolysis chambers were provided with heating means, such as catalytic radiant panels or flame burners using thermolysis gases and / or commercial combustible gases (inexpensive).
- heating means such as catalytic radiant panels or flame burners using thermolysis gases and / or commercial combustible gases (inexpensive).
- the catalytic radiant panels were supplied, on the one hand, with pure oxygen or with air and, on the other hand, with thermolysis gas originating from thermolytic decomposition.
- thermolysis gas originating from thermolytic decomposition.
- the carbon dioxide and water vapor generated by the oxidation of the thermolysis gases in the catalytic radiant panels could participate in the heating by convection and radiation.
- the fumes produced by the boiler could also participate in the heating of these rooms.
- the temperature of the thermolysis chamber was for example maintained around 600 ° C, while that of the dehydration chamber, lower, was maintained above 100 ° C, for example around 120 ° C.
- thermolysis zone proposes a process for treating solid products, the rejection of which is harmful to the environment, comprising in particular a step of thermolysis of solid products in a thermolysis zone, according to which: the gases from the thermolysis zone are aspirated; at least part of the aspirated gases are cooled to a temperature below about 80 ° C; the condensed products from the cooling are separated from the uncondensed gases from this same cooling; a part of the gases sucked in is heated by combustion of at least part of the uncondensed gases; and - the heated part of the gas is recycled by reintroduction into the thermolysis zone.
- the invention thus teaches to replace the burners or catalytic radiant panels by a direct introduction of a stream of hot gases comprising thermolysis gases recycled in the thermolysis zone. This avoids any creation of hot spots or a possible explosive reaction between oxygen and hydrogen.
- thermolysis gases further contributes to the self-sufficiency of the treatment process of the present invention.
- thermolysis carried out by forced circulation of a current of hot gases, resulting from the introduction of the current into the thermolysis zone, direct contact with the load, then suction of the gases coming from the thermolysis zone, proves particularly regular, but above all significantly faster than the thermolysis performed in accordance with the teachings of document EP-A-0 610 120.
- a maximum of solid products treated using the treatment process of the present invention is transformed into energy.
- the tars from cooling may, for example, be mixed with fuels (coal) from solid residues from the thermolysis zone and constitute a fuel which can be recovered later.
- thermolysis zone The cooling of at least part of the gases from the thermolysis zone also allows easy recovery of the thermolysis products. Indeed, the transformation of part of the gases from the thermolysis zone into condensed products makes it possible to minimize the volume of the means of storage of these products (tars, etc.). Furthermore, the gases uncondensed are advantageously reused to heat the gas stream intended to be introduced into the thermolysis zone.
- thermolysis makes it possible to preserve the treatment installation and in particular the pumping means.
- the heated part of gas is advantageously injected in the immediate vicinity of a static charge of solid products to be treated.
- the part of the gases intended to be heated consists of a second part of the uncondensed gases coming from the cooling.
- thermolysis gases a fraction of uncondensed thermolysis gases is burned and used to heat a second part of uncondensed gases which are recycled and returned to the thermolysis zone to enrich in thermolysis gas and in particular in hydrogen and hydrocarbons (methane, ethane , ethylene ).
- a first fraction of the aspirated gases is cooled to about 60 ° C - 80 ° C and a second fraction of the aspirated gases to about 230 ° C - 330 ° C, at least one part of the uncondensed gases coming from said first fraction, the uncondensed gases coming from said second fraction are heated by means of the gases coming from this combustion, the second heated fraction of gas constituting said heated part of gas, and the condensed products coming from cooling of said first and second fractions.
- the fraction of gas intended to be heated and recirculated in the thermolysis zone is maintained as a stream of hot gases at a higher temperature than the fraction intended to be burned. This fraction to be heated will therefore require less heating before reintroduction into the thermolysis zone.
- thermolysis a dehydration of the solid products is carried out before thermolysis, in the thermolysis zone and by means of a part of the gases resulting from the combustion.
- the combustion is carried out in a boiler equipped with fiber burners.
- Such burners are capable of burning relatively lean gases, and in particular the thermolysis gases from a thermolysis zone of waste constituting the solid products to be treated. In addition, this combustion process maintains a low level of NO x in the fumes.
- thermolysis gases such as propane, in the boiler. If necessary, to ensure correct combustion, a certain proportion of liquefied gas may also be added to the thermolysis gases intended to be burned.
- liquefied gas such as propane
- thermolysis gases In order not to be dependent on the composition of the thermolysis gases or on their production, they are compressed and stored in a tank, before combustion.
- the gases sucked are passed through a heat exchanger as hot fluid, then these gases are passed through a fractionation train to obtain separate fractions containing, respectively, heavy hydrocarbons, light hydrocarbons, water and uncondensed gases at low temperatures; part of the uncondensed gases at low temperature is reinjected into the heat exchanger, as cold fluid, to raise the temperature before heating them by combustion of another part of these uncondensed gases at low temperature.
- the boiler is equipped with multi-fuel burners (gases and liquids) to be able to burn uncondensed gases but also light hydrocarbons, organic compounds dissolved in water and which would be separated therefrom, fuel or propane.
- an installation for the treatment of solid products comprising a zone for thermolysis of solid products by direct contact with hot gases; a line for introducing a stream of hot gases into the thermolysis zone, a line for extracting gases from the thermolysis zone; means adapted to cool at least part of the gases extracted from the thermolysis zone to a temperature below about 80 ° C and to separate the condensed products from the cooling of the uncondensed gases from this same cooling, arranged on the line extraction; characterized in that it comprises pumping means (pump, booster, fan, ...) communicating by the extraction line with the thermolysis zone to suck out the gases therefrom; a boiler capable of burning at least part of the uncondensed gases and communicating via an inlet line with the cooling and separation means; a recycling line for part of the gases extracted from the thermolysis zone, this recycling line being fluidly connected to the extraction line and to the introduction line and passing through the boiler to heat the gases circulating in this line
- the installation can in particular also include an inlet line for liquefied gas in the boiler, such as propane, which makes it possible to maintain a mixture with PCI acceptable in terms of combustion performance and to ensure the phase of start of installation.
- an inlet line for liquefied gas in the boiler such as propane
- FIG. 1 is a block diagram of an installation in accordance with an embodiment of the present invention
- FIG. 2 is a diagram of another embodiment of this installation
- FIG. 1 is a diagram of a preferred embodiment of this installation.
- the installation of FIG. 1 comprises an airlock 1 into which the solid products penetrate, then a thermolysis zone 2 in which the solid products are first partially or completely dehydrated, then brought to their thermal decomposition temperature (known and fixed at advance) for example around 600 ° C.
- this thermolysis zone is followed by a cooling zone 3 where the solid residues from the heat treatment are brought to room temperature, for example by spraying water.
- zones 1, 2 and 3 are chambers insulated from one another in a substantially sealed manner, for example by guillotine doors (not shown) actuated by cylinders; the door between rooms 1 and 2 and the door between rooms 2 and 3 being transversely movable in sealed housings (registers).
- guillotine doors not shown
- watertight doors are provided at the entrance to chamber 1 and at the exit from chamber 3, whereby the airlock 1 and the cooling zone 3 are, at will, isolated from the outside. and / or the thermolysis zone 2; they can be movable vertically or horizontally or around a joint according to the dimensions of the installation, the space available and the free choice of the designer.
- thermolysis chamber 2 is insulated to limit heat loss.
- Chamber 2 is maintained at a constant pressure which can be set between 200 mbar and 1.2 bar.
- a constant pressure which can be set between 200 mbar and 1.2 bar.
- This pressure is maintained for example by pumping means 10 communicating with chamber 2 by an extraction line 11.
- pumping means 10 communicating with chamber 2 by an extraction line 11.
- the means for pumping the cooling zone and the airlock have not been shown in FIG. 1.
- a cyclone 12, disposed on the extraction line 11, supplied with water by an inlet 13 operates a division of the gases from the thermolysis chamber 2 into a fraction containing water and tars recovered in a pitch pan 14 and a fraction of uncondensed gases.
- This last fraction of uncondensed gases is cooled in a cooler constituted by a tube exchanger 15 in which a refrigerant circulates, disposed downstream of the cyclone 12 on the extraction line 11.
- thermolysis gases extracted from chamber 2 thus pass from a temperature of approximately 500 ° C. at the outlet of chamber 2 to a temperature in the region of 80 ° C. in cyclone 12, then to a temperature of approximately 60 ° C. at the outlet of the exchanger 15.
- the water vapors are separated in particular from the thermolysis gases, which, as will be described below, are at least partly intended to be burned in a boiler 16.
- this cooling also has the advantage of preserving the conventional mechanical pumping means 10 which would wear excessively if the gases which they pumped had a temperature above about 80 ° C.
- a first part of the fraction of uncondensed gases is burned in the boiler 16, while a second part of this fraction of uncondensed gases is heated by means of the gases resulting from the combustion of said first part within of the boiler 16, this second heated part of uncondensed gases being recirculated in the thermolysis chamber 2.
- said first part of the fraction of uncondensed gases is brought to the boiler 16 by an inlet line of uncondensed thermolysis gases 17 communicating with the first pumping means 10 via a valve 18.
- a second thermolysis gas bypass is constituted by a recycling line 19 communicating with the extraction line 11 between the tube exchanger 15 and the pumping means 10.
- This recycling line 19 is connected to the extraction line 11 by a distribution valve 20, at one of its ends, and a coil 21 mounted in the chimney 16, at its other end.
- Second pumping means 22 are also arranged on this recycling line 19, between the distribution valve 20 and the coil 21, here near the latter.
- the outlet of the coil 21 communicates with a line 23 for introducing hot gases into the chamber 2.
- this line 23 allows direct injection of the stream of hot gases heated in the boiler 16, in the immediate vicinity of the load of solid products to be treated, by means of a hood 24 covering the carriage (s) 25 located in the chamber 2 at the time of the thermolysis step.
- these carriages are, conventionally, moved within chambers 1, 2 and 3 by a mechanical system of the pinion and rack type for example, or even of the electromagnetic drive type.
- These carriages are moreover also designed so that solid residues - glass, rubble, metals, for example - remain in the carriages 25 while being easily removed at the outlet of the cooling chamber 3.
- the introduction line 23 also makes it possible to introduce gases from the combustion into the boiler 16, or fumes, into the chamber 2 in order to dehydrate the charge of solid products to be treated, prior to thermolysis.
- a dehydration line, marked 26, communicating, on the one hand, with an outlet line 27 of fumes or gases from combustion of the boiler 16, through a control valve 28 and, on the other hand, with the introduction line 23 via a connection valve 29.
- the fumes leaving the boiler and which are not used, are sent via a fan 30 to a washer 31 used to purify these fumes before they exit into the atmosphere.
- a second fan 32 is provided at the outlet of the washer 31.
- a discharge line 33 for the fumes extracted from the chamber 2 during dehydration connected by one of its ends to the valve 18 and at its other end to the washer. 31.
- the boiler 16 is equipped with burners 34 of the fiber type, that is to say comprising a lattice of fibers.
- This type of burner is particularly interesting because it makes it possible to burn gases which are relatively poor from an energy point of view.
- An example of such a burner is that of the "BEKITHERM AC" type sold by the company ACOTECH.
- thermolysis gas for example propane
- inlet line 35 for liquefied gas for example propane
- thermolysis gas is connected to the inlet line 17 between the valve 18 and the inlet valve 36, via a connection valve 38.
- Compression means (not shown) are also provided for compressing the gases before their storage in the reservoir 37.
- the gases from combustion having a temperature of approximately
- a line 39 equipped with a heat exchanger to produce steam or heating water vapor is connected to the introduction line 23.
- the thermal energy thus recovered can be applied in situ to a turbine (not shown) which converts it into electrical form, for, for example, supply the pumping means 10 and 22 and the fans 30 and 32, or serve any other function, possibly foreign to the installation.
- a line of oxidizing oxygen 40 is connected to the inlet line 17 downstream of the liquefied gas inlet line 35, via a connection valve 41.
- This line can convey pure oxygen or more simply l 'air.
- pressure and temperature control means are mounted on the different chambers 1, 2 and 3, as well as on the boiler 16.
- means for regulating the gas flow rate by burner in boiler inlet 16, also not shown in FIG. 1, are provided at the inlet of this boiler 16.
- the valve marked 42 on the introduction line 23 allows the isolation and regulation of the gas flow coming from lines 26 and 19.
- the solid residues leaving the cooling zone 3 are treated wet to separate the mineral fines from the coal.
- the coal can be mixed with the tars recovered by decantation in the pitch pan 14 to produce a combustible mixture.
- This combustible mixture could, for example, be burned in the boiler 16 or outside the installation, in particular to produce electrical energy.
- the treatment installation of the present invention operates as follows:
- Solid products (household waste in particular) are brought through the airlock 1 into bedroom 2.
- the boiler 16 is started by combustion of liquefied gas alone, or, if thermolysis gases are present in the tank 37, by combustion of the latter, or even by a mixture of the latter with liquefied gas, in order to produce combustion gases or fumes. These fumes are sent by the dehydration line (via the introduction line 23) to a chamber 2 to carry out the dehydration of the solid products, having been cooled at the level of the line 39.
- thermolysis taking place between 250 ° C. and 750 ° C. approximately.
- the hot gases introduced into chamber 2 are enriched, on contact with the charge of solid products to be treated, of hydrogen, of hydrocarbons
- a part of the uncondensed thermolysis gases leaving the exchanger 15 is sent to the tank 37 or directly to the boiler 16, for combustion, while a second part is sent to the recycling line 19 where, after acceleration to the by means of pumping means 22, this second part of the gases is heated by passing through the coil 21, then introduced by the reintroduction line 23 into the chamber 2.
- the hot gases intended to be introduced into the chamber 2 have a temperature higher than approximately 650 ° C., it will be possible, as during dehydration, to operate the heat exchange line 39 in order to lower the temperature.
- thermolysis gas stored in the tank 37, sent by the dehydration line 26 in the introduction line 23 and cooled to the required temperature. It should be noted here that in other embodiments, it is also possible to use, for this recycling, thermolysis gases originating from the reservoir 37, by providing an appropriate connection to the recycling line 19.
- Figure 2 shows another embodiment where elements similar to those of Figure 1 are designated by the same reference numerals.
- this installation comprises cooling and separation or division means arranged in a specific manner.
- these means include a cyclone 12 which cools the gases from the thermolysis chamber 2 to a temperature between about 230 ° C and about 330 ° C. Part of these gases is used in the recycling line 19 (branch at the location of the valve 20 '), while another part of the gases, intended to be burned in the boiler 16, is sent by a line of cooling 51 in the tube exchanger 15 to be cooled to about 60 ° C - 80 ° C.
- the pumping means 22 constituted by a vacuum pump in the case of the installation of FIG. 1, have been replaced by a fan.
- the liquid hydrocarbons At the outlet of the tube exchanger 15, the liquid hydrocarbons
- the gases of this line 53 have a temperature of approximately 50 ° C. and are mixed with the gases of the recycling line downstream of the fan 22, which allows the recovery of gases at a temperature of the order of 230 ° C.
- thermolysis gas circulating in the recycling line 19, before mixing with these depleted and cooled gases, is sent to the tube exchanger 15 by a line marked 54 at the location of the valve marked 63.
- gases have, in practice, a temperature of approximately 150 ° C in this line and arrive at a temperature of approximately 120 ° C at the inlet of the tube exchanger 15. This makes it possible to drain the overflow of thermolysis gas at partially condense.
- steam is produced, or it is heated, for later recovery, not only on the dehydration line 26, but also on line 54 (cf. lines marked 39 and 39 'in FIG. 2 ) and at the outlet of the boiler 16 by means of the fumes sent to the washer 31, through a heat exchanger 55.
- the fumes from the dehydration circuit pass, before entering the washer 31, through a secondary washer 31 'and pumping means 10' maintaining the desired pressure in the dehydration chamber 1, arranged on the line of dehydration fumes 56. This avoids damaging the pumping means 10 'and in particular recovers the liquid hydrocarbons (tars) recovered at the outlet of the washer 31' (arrow 57).
- FIG. 3 shows a preferred embodiment where elements similar to those of Figure 1 are designated by the same reference numerals.
- the introduction line 23 communicates by means of fluid connection 70, directly with the interior of each of the carriages 25.
- Each of the carriages 25 is, for its part, equipped with a drilled bottom adapted to carry the load of products to be treated and to transmit the hot gases to this load.
- the fluid connection means 70 can, for example, be constituted by a telescopic device bringing a bellows mounted on one end of a pipe to a connection zone provided at the bottom of the carriage 25.
- the carriage 25 may, for example, carry a grid for receiving the solid products to be treated or a container with nozzles opening out, in a regularly distributed manner, from the bottom of the container and fluidly connected by a tubular system to the connection zone.
- the hot gases can be injected directly into the charge of waste to be treated, which makes it possible in particular to reduce the risk of unburnt, thanks to intimate contact of the hot gases with the charge of waste to be treated, without preferential passage.
- thermolysis step there is a drainage area 4 for the carriages 25, after the cooling area 3.
- the residues are poured into a swimming pool 73 from which they are then extracted and sorted.
- the gases present in the chamber 2 are sucked by the extraction line 11 at a temperature, which is in the case of this preferred embodiment, of approximately 330 ° C.
- This circuit comprises a contact cooling means 76, called an oil quench by a person skilled in the art, a pump 77 and a heat exchanger 78.
- the recycling line 19 opens into the cooler 76 from the bottom thereof.
- the pump 77 and the heat exchanger 78 are placed on a branch 19 ′ of the recycling line 19 which leaves from the bottom of the cooler 76 and returns to this cooler 76 from the top.
- a draw-off line 79 for heavy hydrocarbons is connected to this branch 19 ', between the pump 77 and the exchanger 78.
- the cold fluid of the exchanger 78 is water supplied by the line 80. This water is transformed into steam which comes out through line 81, connected to a steam recovery unit (not shown).
- the gases entering the cooler 76 are cooled by spraying heavy hydrocarbons which have been previously recovered from the bottom of the cooler 76, sucked in by the pump 77, cooled in the heat exchanger 78 to a temperature of approximately 120-130 ° C and reinjected into the cooler 76 from the top thereof. Heavy hydrocarbons are thus continuously formed which are partly withdrawn by the line 79 and partly recirculated in the cooler 76.
- the uncondensed gases leave the cooler 76 at a temperature of about 150 ° C. and are brought by the recycling line 19 in a condenser 82 intended to cool them down to a temperature of approximately 45 ° C.
- This condenser 82 is supplied by a refrigerant circulating in a cooling circuit comprising a pump 83 and a fan 84.
- the condensed products accumulate at the bottom of the condenser 82, are extracted from it and introduced into a separator 85 (of the lamellar decanter type), to separate the light hydrocarbons from the water and the organic compounds which are dissolved therein.
- the light hydrocarbons are extracted via line 86 while the aqueous phase is introduced via line 87 into another separator 88, such as a distillation unit, to separate the water from the organic compounds which are dissolved there.
- another separator 88 such as a distillation unit
- the water leaving the separator 88 is brought by a line 89 to a water treatment installation, while the soluble organic compounds leaving this separator 88, by a line 90, can be brought from this line 90 to the boiler 16, to be burned there.
- water spraying device 91 also called a water quench by a person skilled in the art.
- This device 91 is intended to wash the uncondensed gases to rid them in particular of acids, such as hydrochloric acid.
- water is circulated in the device 91, by means of a circuit 92 incorporating a pump 93.
- This circuit 92 includes a bypass 94 allowing the wastewater to be brought to a treatment installation. waters, for example that mentioned above.
- the uncondensed gases leaving device 91 at a temperature of the order of 45 ° C. are, for a first part, reinjected into the exchanger heat 75, via a booster 95 which raises their temperature to about 100 ° C.
- This part of gas passes through the heat exchanger 75, as a cold fluid, and leaves it at a temperature of the order of 300 ° C, to then pass through a coil 21 in which the gases of this part of uncondensed gas are heated to a temperature of the order of 650 ° C. by combustion gases from the boiler 16.
- the heated gases penetrate into the introduction line 23. Another part of the uncondensed gases is brought, via the arrival line 17, to the boiler 16, in which they are burned for reheat the part of gas passing through the coil 21.
- the circulation of gases on this line 17 is ensured by a fan 96.
- a third part of these uncondensed gases at low temperature (around 45 ° C) is injected, via an injection line 97, to which a booster 98 is connected, in the cooling zone 3.
- the hot gases recovered from this cooling zone 3 are also recovered on the extraction line 11.
- the hot gases present in the emptying zone 4 are also recovered and introduced into the cooler 76, from the bottom thereof, via a recovery line 99.
- this installation can in this respect be equipped with means for storing uncondensed gases.
- a smoke evacuation circuit similar to that of FIG. 1 can also be provided for the installation of this FIG. 3. Furthermore, the gases escaping from the chamber 2 towards the airlock 1 at the opening from door 71, can also be retrieved and entered in line 99.
- the installation is protected from the risks of coking originating from the condensation of tars, the risks of clogging by dust and the risks of corrosion by acid gases.
- the cyclone 12 and the tube exchanger 15 can be replaced by a cyclolaveur, that is to say a washer, operating by water spraying, adapted to fulfill the functions assigned to the cyclone and to the exchanger at tubes within the framework of the invention and in particular to lower the temperature of the fraction of uncondensed gases to approximately 60 ° C - 80 ° C.
- a cyclolaveur that is to say a washer, operating by water spraying
- the coil 21 can be replaced by any equivalent gas / gas heat exchange means.
- coal extracted from solid residues and the tars can be recovered separately.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Treating Waste Gases (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BR9706834-9A BR9706834A (pt) | 1996-10-15 | 1997-10-15 | Processo e instalação para tratamento de produtos sólidos cujo rejeito é prejudicial para o meio ambiente |
JP10518073A JPH11504984A (ja) | 1996-10-15 | 1997-10-15 | 固形廃棄物の熱処理方法及びプラント |
DE0888416T DE888416T1 (de) | 1996-10-15 | 1997-10-15 | Verfahren und anlage zur behandlung von abfällen durch thermolyse |
US09/091,302 US6168688B1 (en) | 1996-10-15 | 1997-10-15 | Method and plant for treating solid waste products by thermolysis |
KR1019980704471A KR100281312B1 (ko) | 1996-10-15 | 1997-10-15 | 열분해에의한고체폐기물처리방법및설비 |
EP97910484A EP0888416A1 (fr) | 1996-10-15 | 1997-10-15 | Procede et installation pour le traitement de dechets solides par thermolyse |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9612551A FR2754540B1 (fr) | 1996-10-15 | 1996-10-15 | Procede et installation pour le traitement de dechets solides par thermolyse |
FR96/12551 | 1996-10-15 | ||
FR9612550A FR2754539B1 (fr) | 1996-10-15 | 1996-10-15 | Procede de traitement de dechets par injection de gaz chauds directement dans la charge a traiter, installation et chariot pour la mise en oeuvre de ce procede |
FR96/12550 | 1996-10-15 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1998016593A1 true WO1998016593A1 (fr) | 1998-04-23 |
Family
ID=26233042
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR1997/001839 WO1998016593A1 (fr) | 1996-10-15 | 1997-10-15 | Procede et installation pour le traitement de dechets solides par thermolyse |
PCT/FR1997/001838 WO1998016594A1 (fr) | 1996-10-15 | 1997-10-15 | Installation de traitement de déchets par injection de gaz chauds dans la charge à traiter et recyclage des gaz de thermolyse produits |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR1997/001838 WO1998016594A1 (fr) | 1996-10-15 | 1997-10-15 | Installation de traitement de déchets par injection de gaz chauds dans la charge à traiter et recyclage des gaz de thermolyse produits |
Country Status (9)
Country | Link |
---|---|
US (1) | US6168688B1 (fr) |
EP (2) | EP0888416A1 (fr) |
JP (3) | JPH11504984A (fr) |
KR (2) | KR100281312B1 (fr) |
BR (2) | BR9706864A (fr) |
CA (2) | CA2240530A1 (fr) |
DE (2) | DE888416T1 (fr) |
ES (2) | ES2127170T1 (fr) |
WO (2) | WO1998016593A1 (fr) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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KR100602932B1 (ko) * | 1998-07-30 | 2006-07-19 | 테르모셀렉트 악티엔게젤샤프트 | 이질적으로 발생한 폐기물의 고온 재순환을 수행하기 위한 장치 및 그 투입 방법 |
Families Citing this family (8)
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BR9909884A (pt) * | 1999-02-25 | 2000-12-26 | Nexus Technologies | Instalação de tratamento termolìtico de dejetos |
KR100375819B1 (ko) * | 2000-09-06 | 2003-03-15 | (주)이앤비코리아 | 함수율 조절식 슬러지 건조장치 |
US6883444B2 (en) * | 2001-04-23 | 2005-04-26 | N-Viro International Corporation | Processes and systems for using biomineral by-products as a fuel and for NOx removal at coal burning power plants |
KR100526017B1 (ko) * | 2002-11-25 | 2005-11-08 | 한국에너지기술연구원 | 열분해 비응축성 가스를 회수하는 고분자 폐기물열분해장치 및 그 방법 |
US10163676B2 (en) | 2013-06-27 | 2018-12-25 | Taiwan Semiconductor Manufacturing Co., Ltd. | Apparatus and system for preventing backside peeling defects on semiconductor wafers |
US20160001196A1 (en) * | 2014-07-03 | 2016-01-07 | Richard Lyle Shown | System for the separation of gases from solids and fluids |
CN108384583B (zh) * | 2018-03-14 | 2024-04-02 | 深圳市水务(集团)有限公司 | 一种固体废物热解气净化与利用系统 |
KR102411128B1 (ko) * | 2020-08-19 | 2022-06-22 | 보국에너텍주식회사 | 질소산화물 저감형 열분해 가스화 시스템 |
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US3525673A (en) * | 1969-03-24 | 1970-08-25 | Eric C Cameron | Closed,controlled system for carbonizing organic refuse |
EP0505278A1 (fr) * | 1991-03-20 | 1992-09-23 | Societe Francaise De Thermolyse | Système pour le traitement par thermolyse de produits solides dont le rejet est préjudiciable pour l'environnement |
EP0524847A1 (fr) * | 1991-07-09 | 1993-01-27 | Institut Français du Pétrole | Procédé et dispositif de traitement de déchets par contact direct |
EP0610120A1 (fr) * | 1993-02-01 | 1994-08-10 | Societe Francaise De Thermolyse | Procédé et installation pour le traitement par thermolyse de déchets solides, sans condensation d'hydrocarbures |
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GB327717A (en) * | 1928-11-07 | 1930-04-07 | Eesti Patendi Aktsiaselts | Improvements in the construction of wagons and rails, applied in ovens for dry distillation, driers, kilns and similar ovens working by means of gas and vapour injections or circulations |
US2208705A (en) * | 1935-06-03 | 1940-07-23 | Soubbotin Igor | Tunnel oven used for the carbonization at low temperatures of oil shale, lignite, coal, and similar materials |
DE2621392C3 (de) | 1976-05-14 | 1981-07-09 | Messerschmitt-Bölkow-Blohm GmbH, 8000 München | Verfahren und Anlage zur Aufarbeitung von Abfallstoffen |
DE3509275A1 (de) | 1984-03-23 | 1985-12-19 | Carl Still Gmbh & Co Kg, 4350 Recklinghausen | Verfahren zur thermischen behandlung von waschbergen |
DE4202321A1 (de) | 1992-01-29 | 1993-08-05 | Adolf Gorski | Anlage zum verschwelen von abfallstoffen |
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1997
- 1997-10-15 DE DE0888416T patent/DE888416T1/de active Pending
- 1997-10-15 EP EP97910484A patent/EP0888416A1/fr not_active Withdrawn
- 1997-10-15 WO PCT/FR1997/001839 patent/WO1998016593A1/fr not_active Application Discontinuation
- 1997-10-15 CA CA002240530A patent/CA2240530A1/fr not_active Abandoned
- 1997-10-15 ES ES97910483T patent/ES2127170T1/es active Pending
- 1997-10-15 BR BR9706864-0A patent/BR9706864A/pt unknown
- 1997-10-15 DE DE0879271T patent/DE879271T1/de active Pending
- 1997-10-15 KR KR1019980704471A patent/KR100281312B1/ko not_active IP Right Cessation
- 1997-10-15 JP JP10518073A patent/JPH11504984A/ja active Pending
- 1997-10-15 JP JP10518072A patent/JP2999558B2/ja not_active Expired - Lifetime
- 1997-10-15 EP EP97910483A patent/EP0879271A1/fr not_active Withdrawn
- 1997-10-15 WO PCT/FR1997/001838 patent/WO1998016594A1/fr not_active Application Discontinuation
- 1997-10-15 KR KR1019980704470A patent/KR100282759B1/ko not_active IP Right Cessation
- 1997-10-15 ES ES97910484T patent/ES2127171T1/es active Pending
- 1997-10-15 CA CA002240532A patent/CA2240532A1/fr not_active Abandoned
- 1997-10-15 US US09/091,302 patent/US6168688B1/en not_active Expired - Fee Related
- 1997-10-15 BR BR9706834-9A patent/BR9706834A/pt unknown
-
2001
- 2001-04-16 JP JP2001002206U patent/JP3081850U/ja not_active Expired - Lifetime
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US3525673A (en) * | 1969-03-24 | 1970-08-25 | Eric C Cameron | Closed,controlled system for carbonizing organic refuse |
EP0505278A1 (fr) * | 1991-03-20 | 1992-09-23 | Societe Francaise De Thermolyse | Système pour le traitement par thermolyse de produits solides dont le rejet est préjudiciable pour l'environnement |
EP0524847A1 (fr) * | 1991-07-09 | 1993-01-27 | Institut Français du Pétrole | Procédé et dispositif de traitement de déchets par contact direct |
EP0610120A1 (fr) * | 1993-02-01 | 1994-08-10 | Societe Francaise De Thermolyse | Procédé et installation pour le traitement par thermolyse de déchets solides, sans condensation d'hydrocarbures |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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KR100602932B1 (ko) * | 1998-07-30 | 2006-07-19 | 테르모셀렉트 악티엔게젤샤프트 | 이질적으로 발생한 폐기물의 고온 재순환을 수행하기 위한 장치 및 그 투입 방법 |
Also Published As
Publication number | Publication date |
---|---|
KR100282759B1 (ko) | 2001-05-02 |
ES2127171T1 (es) | 1999-04-16 |
US6168688B1 (en) | 2001-01-02 |
JP3081850U (ja) | 2001-11-22 |
CA2240530A1 (fr) | 1998-04-23 |
JPH11504984A (ja) | 1999-05-11 |
DE888416T1 (de) | 1999-06-10 |
EP0879271A1 (fr) | 1998-11-25 |
EP0888416A1 (fr) | 1999-01-07 |
BR9706864A (pt) | 1999-12-28 |
JP2999558B2 (ja) | 2000-01-17 |
WO1998016594A1 (fr) | 1998-04-23 |
ES2127170T1 (es) | 1999-04-16 |
BR9706834A (pt) | 1999-12-28 |
KR19990072140A (ko) | 1999-09-27 |
CA2240532A1 (fr) | 1998-04-23 |
KR100281312B1 (ko) | 2001-03-02 |
DE879271T1 (de) | 1999-06-10 |
JPH11504983A (ja) | 1999-05-11 |
KR19990072139A (ko) | 1999-09-27 |
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