EP0267654A2 - Procédé et dispositif de retraitement en continu des huiles usagées - Google Patents

Procédé et dispositif de retraitement en continu des huiles usagées Download PDF

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Publication number
EP0267654A2
EP0267654A2 EP87202165A EP87202165A EP0267654A2 EP 0267654 A2 EP0267654 A2 EP 0267654A2 EP 87202165 A EP87202165 A EP 87202165A EP 87202165 A EP87202165 A EP 87202165A EP 0267654 A2 EP0267654 A2 EP 0267654A2
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EP
European Patent Office
Prior art keywords
reactor
tube
stage
waste oil
oil
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP87202165A
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German (de)
English (en)
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EP0267654B1 (fr
EP0267654A3 (en
Inventor
Christian O. Schön
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Individual
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Individual
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Priority claimed from DE19863638606 external-priority patent/DE3638606A1/de
Application filed by Individual filed Critical Individual
Priority to AT87202165T priority Critical patent/ATE74953T1/de
Publication of EP0267654A2 publication Critical patent/EP0267654A2/fr
Publication of EP0267654A3 publication Critical patent/EP0267654A3/de
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Publication of EP0267654B1 publication Critical patent/EP0267654B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
    • 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
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/06—Reactor-distillation

Definitions

  • the invention relates to a method and a device for the continuous treatment of waste oil, in which the waste oil is heated and subjected to a subsequent fractionation and distillation into products of different qualities (side fractions) and precautions are taken to keep deposits free.
  • Single-stage or multi-stage distillation processes are known for this, in which the waste oil is heated to the processing temperature of approx. 300 ° C by tube heaters or other heat exchangers and then processed in large-volume reaction columns, generally in a first stage under atmospheric pressure and in one second stage under vacuum. In a third stage, the residues can then be distilled under negative atmospheric pressure.
  • a known such method is e.g. B. the sulfuric acid bleaching earth process.
  • the waste oil remains in the system for a very long time. Because of the large-volume containers, temperature and pressures are difficult to control.
  • the vacuum that can be achieved in practice is 60 to 100 mbar.
  • Corresponding to the boiling and evaporation temperature of the fractions in question correspondingly high temperatures have to be applied, some of which are just below the cracking temperature of the oils in question. Cracking must be prevented in order to maintain the lubricating effect.
  • the present invention has for its object to provide a method and an apparatus for performing this method for the treatment of waste oil, in which the yield is as high as possible and the reaction and residence time is as short as possible and which do not have the disadvantages of the known devices and methods Has.
  • the invention solves the problem by a separation process in which the waste oil is gradually heated higher and higher in a single-tube reactor, in each step to a precise temperature and the correspondingly accurate pressure (negative or positive pressure) required for the desired quality (side fraction) ), and that at the end of each stage, the heated oil is separated immediately without storage and thus without dwell time and distilled to the desired product.
  • reactor is also understood to mean a single-tube still, since in most cases, but not always, a chemical reaction takes place in the single-tube reactor.
  • a method according to the invention works with a significantly higher yield, depending on the quality of the used oil up to 90%. Only about 1 to 2% acid tar is generated.
  • the waste products to be disposed of are used as fuel and chemical auxiliaries in the cement industry.
  • the waste oil is expediently preheated before being fed into the single-tube reactor.
  • the pressure is preferably reduced from stage to stage to a vacuum of up to 1 mbar. This was not possible with the known systems.
  • the preheating can also be done in the single-tube reactor.
  • the increasing heating of the waste oil in the direction of flow can take place in many ways, for example by electrical heating, inductive or resistance heating. Can be advantageous In the last stage, where there may be caking on the tube walls, indirect high-frequency heating of the product can also be considered. Likewise, as described further below, positively guided heat transfer media which wash around the single pipe in countercurrent can also be used advantageously.
  • the ability to run sections of the reactor under different pressures means that chemical reactions can be carried out continuously. For example, by feeding sodium, harmful chlorine can be bound to table salt, which can then e.g. can be excreted with coke at the end of the reactor.
  • table salt which can then e.g. can be excreted with coke at the end of the reactor.
  • other known methods can also be used for this.
  • the process in the final stage of the reactor is operated at a temperature in the range from approx. 3oo to 9oo ° C and the pressure is between 1 mbar and 10 bar, preferably atmospheric pressure. Bitumen or coke comes out of the reactor as the last product. This end product largely contains the contaminants and pollutants and is e.g. used by the cement industry as a fuel and chemical additive.
  • the quality of the side fractions can be improved in a known manner by adding reflux.
  • the enrichment can take place in place of the return admixture of the steam or mixture separated from the cutters.
  • mechanically driven rotor bodies excrete the liquids contained in the steam and feed them back to the next product or the bottom.
  • the returned product or the returned sump can be swirled with the product steam or gas in a one-pipe part.
  • the gases or vapors leaving via the top of the respective return admixtures are condensed as usual and processed further.
  • the side fractions can be processed in an outgoing single tube reactor for further distillations.
  • chemicals can be dosed or fed exactly to improve the product at precise pressures and temperatures as in the main line.
  • Hydrogenation can take place both in the main strand and for a certain side fraction in a side strand. If the hydrogenation takes place in a side strand, this is advantageously also designed as a single-tube reactor.
  • hydrogen can advantageously be fed in at various points along the single-tube reactor either in the main line or in a side line in such an amount that under hydrogenation conditions at least 20% by weight, preferably at least 30% by weight and particularly preferably at least 35% by weight. % are dissolved in the suspension.
  • hydrogen should be dissolved in the suspension up to saturation. As much hydrogen as possible is thus fed in at the start of the hydrogenation reaction, but under the above conditions. Since hydrogen is consumed during the hydrogenation reaction, the reactor is replenished at several points along the way according to the consumption - again under the above conditions. The higher the hydrogenation pressure, the more hydrogen can be fed in at the beginning and also along the reactor. At high hydrogenation pressures, fewer make-up points are required than at low pressures.
  • the single-tube reactor is particularly favorable for cooling, ie the heat dissipation of the exothermic hydrogenation process. Harmful overheating during hydrogenation, such as in autoclaves, does not occur. It is possible to dissipate the entire heat of reaction via the reactor wall to an external cooling medium and, if necessary, to recover it. A Recovery results in a reduction in production costs. Oil can also be fed in at one or more points along the reactor below the hydrogenation temperature. A uniform reaction temperature can thus be controlled in a simple manner over the entire tubular reactor. This uniform reaction temperature contributes to a higher selectivity. A at the same maximum temperature in the autoclave reactor results in a higher hydrogenation rate and thus a greater oil gain. The mixture emerging from the reactor is separated in the separator into a liquid fraction and a gas fraction, both of which are worked up in a manner known per se.
  • the tubes can be provided with a non-smooth surface (e.g. twisted or cross-twisted tubes) or with ribbing (lengthways or crosswise) on the surface with hot gas heating.
  • a non-smooth surface e.g. twisted or cross-twisted tubes
  • ribbing lengthways or crosswise
  • the quality of the products obtained from the waste oil can be further improved in such a single-tube reactor and the yield can be increased if, according to a very advantageous development of the invention, in one of the last stages of the single-tube reactor leading to a distilled-off fraction, an increased flow rate compared to the initial speed of the waste oil brought about and the temperature level above the general cracking temperature from 300 ° to 320 ° C to about 325 ° to 800 ° C is raised briefly.
  • the single-tube reactor makes it possible to keep the waste oil's residence time in the reactor extremely short and to keep it exactly to seconds or even milliseconds to control accuracy, depending on how far the cracking temperature has been exceeded, so that with the short residence time that can be achieved with this, the temperature can be raised far above the normal cracking temperature without cracking - ie hydrogen separation and splitting of the molecules - taking place.
  • the speeds can increase to or even exceed the speed of sound, and thus the residence time can be reduced considerably, ie the higher the temperature is selected, the greater the speed and thus the corresponding shortening of the residence time.
  • the waste oil after the dewatering stage is heated in a single stage until it reaches approximately 800 ° C. at the end of this stage and is conveyed through the reactor to a very high final speed, which can be in the range of the speed of sound, and at the end suddenly cooled to a temperature below the normal critical cracking temperature and then the various Fractions are gradually distilled off at appropriate steam pressures and boiling points.
  • the dewatered waste oil is practically chased through the reactor.
  • a high vacuum and the very high temperatures up to 800 ° C in the reactor turn the waste oil into steam, which flows at a speed up to the speed of sound at the end of this single stage.
  • the entire steam mixture is then suddenly cooled to such an extent that the cracking temperature is not reached, so that no cracking can take place.
  • the vacuum according to measure c) can e.g. be generated by a water ring pump, an oil ring pump, a gas jet or the like. These devices suck out at the end of the reactor.
  • Each measure can be combined individually or two of the same or all three.
  • the conveyance is in the middle area between the beginning and end of the single-pipe reactor is supported by at least one additional mechanical conveyor.
  • a root blower, a capsule blower or the like can serve as an additional conveying device. This results in an increase in the speed of the flow.
  • the cooling can take place in the reactor itself.
  • a particularly good and sudden cooling is achieved according to the invention in that it is brought about by impinging the flow at the end of the stage on a cooled surface with a so-called gossip effect. So far, this effect has only been used in metallurgy in the production of high-quality metals and metal compounds.
  • the pollutants are removed in appropriate cleaning stages in the total flow or in the side fractions.
  • metal balls can advantageously be used, which either pass through the reactor from time to time or continuously with the oil or are rejected.
  • Another possibility for cleaning is in particular for the last stage, in which there is a particular risk that the product will crack - that is, forms coke which bakes on the tube wall - in a carrier medium, such as. B. to mix liquid tin, salts or sand with the oil. Due to the high flow velocity, the carrier medium swirls and rubs off the deposits that build up on the wall. If there is no turbulence, this can be generated by built-in turbulators or by product recycling.
  • a carrier medium such as. B. to mix liquid tin, salts or sand with the oil. Due to the high flow velocity, the carrier medium swirls and rubs off the deposits that build up on the wall. If there is no turbulence, this can be generated by built-in turbulators or by product recycling.
  • the abrasion on the inner wall of the tube which is dependent on the flow rate can be measured by counting by means of a Geiger counter of the particles removed from a radioactively irradiated point of the tube.
  • a sufficient flow velocity is achieved when the values of the Geiger counter exceed the basic value that is already present.
  • vibrations which can be increased to the resonance can also be introduced into the oil and / or into the pipe. These vibrations can be superimposed as interference vibrations or generated as ultrasound or infrasound in the reactor. They can be designed as longitudinal or transverse vibrations.
  • the invention furthermore relates to a device for carrying out the processing method according to the invention.
  • a pump delivering from a storage container for the waste oils is connected to a single-tube reactor which is divided into sections of differently heatable temperatures and adjustable pressures and in which separators and condensers are arranged at the end of the sections.
  • the separators are of such a size that no storage takes place in them, so that they can be separated without any dwell time.
  • the separators can also be designed as rotary separators, such as. by self-impulses of the flowing mixture or powered centrifugal separators, disintegrators or the like.
  • the different pressures (overpressure or underpressure) in the single-tube reactor are maintained by separate feed pumps.
  • At the outlet of each section there are adjustable overflow valves in the event of overpressure or it is counteracted promoted manometric columns.
  • suction takes place by means of pumps or, advantageously, it takes place in a barometric arrangement.
  • the tube of such a single-tube reactor horizontally, but a vertical arrangement is also possible. It can be arranged in loops and cascades or in a ring next to and above one another in order to keep the structural dimensions small.
  • outlets at slightly different temperatures can be provided for each side fraction.
  • the outlets can also be designed as single-tube reactors, which can have the same features as the main line.
  • the monotube is preferably inserted in a tubular round or angular outer jacket and means are provided for introducing heat transfer media between the two tubes.
  • This causes the heat transfer medium to be forced, e.g. Hot pressure water, heat transfer oils or the like. Non-aggressive hot gases are particularly advantageous for this. Due to the total reflection of the heat radiation occurring in the space between the jacket tube and the actual tube reactor, high heat transfer coefficients not previously achieved can be obtained.
  • the flow velocity in the pipe also increases more and more. This is generally between 0.1 to 150 m / s, preferably 0.5 to 60 m / s.
  • the tube diameter can be of different sizes along the reactor according to a further embodiment of the invention and preferably increases in the direction of flow of the waste oil. With increasing volume, the flow rate can thus be kept equal or at least approximately equal to a critical value for the pipe. However, it can also be useful for certain waste oils, in which many gaseous parts go away initially, that the pipes become thinner again later. It depends on the composition of the waste oil in question.
  • each pipe is temperature or speed controlled.
  • Another way of influencing the sensitivity, ie the ratio of volume in the tube to the heat transfer surface, especially at the beginning, is to make the tube one from the circle to give a different cross-sectional shape.
  • the tube can be pressed flat (oval) at the beginning and only later change to a round cross-section via transition pieces when there is high steam volume.
  • Such a single-tube reactor can have a length of about 1ooo to 2 ,ooo m and is preferably arranged in a larger number of loops which extend in a cascade shape, as is shown, for example, in FIG. 3 is shown.
  • the ratio of pipe diameter to length can be between 700: 1 to 20,000: 1, while the pipe diameter can be between 10 to 500 mm clear width, preferably 80 to 150 mm clear width.
  • the reactor shown in FIG. 1 has six stages A to F.
  • the waste oil which is pumped from the tank 6 into the reactor is preheated in stage A.
  • a heating medium introduced into the annular space 7 between the actual single pipe 8 and a jacket pipe 9 via supply and discharge lines 10 and 11 is used for this purpose.
  • stage A low-boiling gasolines are separated off after heating to about 90 ° C. via a separator 12 and condenser 13, and after stage B after heating up about 100 to 115 ° C water and azotropic oils, after stage C after heating to about 120 to 150 ° C heavy gasoline, after stage D after heating to about 220 to 250 ° C gas oils (neutral oils in a subsequent stage, not shown) and after stage E after heating to about 300 ° C base oils.
  • stage D and E the respective product is still hydrogenated in side-strand single-tube reactors 14 and 15 in this example.
  • Separators 12 and condensers 13 are provided after each of the stages B to E, as well as supply and discharge lines 10 and 11 for a respectively tempered heating medium.
  • stage F 18 coke emerges from the reactor.
  • a circuit 16 with a pump 17 or a conveying device for gaseous media or fluidizable solids for a carrier medium for cleaning the inner tube wall of this stage, for example a liquid metal or the like, is also provided.
  • a return column can be connected between separator 12 and condenser 13, as is described in more detail in connection with the example according to FIG. 2.
  • Fig. 2 four stages A, C, D and E of another example are shown.
  • the actual single-tube reactor 8 is in turn surrounded by a jacket tube 9, as is only partially shown in this figure.
  • the used oil in a tank 6 is pressed into the single pipe 8 by a pump 5, where it is heated to approx. 90 ° C. by hot water heated in the water heater 20 between the jacket pipe 9 and the single pipe 8.
  • Gas can be separated in three intermediate separators 12a, 12b and 12c. From the intermediate separator, the separated gas goes to the main separator 12 via a return column 21, where the condenser 22 connects.
  • low-boiling oils and water are excreted here at 23, depending on the temperature.
  • the used oil is pumped further into the second stage C (a stage corresponding to stage B in FIG. 1 is not provided in this example), where it is heated to 120 to 150 ° C. by means of thermal oil heated in the furnace 25.
  • intermediate separators 12a, 12b, 12c and, at the end of the stage, a main separator 12 with a return column 21 are provided.
  • Heavy gasoline is excreted here at 26 via the capacitor 22.
  • the used oil is heated to 220 to 250 ° C. by means of hot gases heated in the burner 28 by means of the pump 27 and brought to a negative pressure of approximately 50 to 200 mbar by means of the vacuum pump 29. After this vacuum pump, thermal afterburning can take place for non-condensable gases.
  • Gas oil (neutral oil in a subsequent step (not shown)) is deposited here via the condenser 22 at 30.
  • the pump 31 conveys the bottom product from stage C to stage E.
  • the oil can be further heated to approximately 300 ° C. by hot gases.
  • a vacuum pump 29 also brings the waste oil to a negative pressure of approximately 1 to 100 mbar. Gas separation takes place in the main separator 12.
  • the gas is fed to the condenser 22 via the return column 21.
  • 32 base oils are excreted.
  • the coking can take place at 1 mbar to 10 bar overpressure, preferably atmospheric pressure.
  • a so-called Carrier medium e.g. liquid tin, sand or the like.
  • additional single-tube reactors 14 and 15 can also be used for the hydrogenation of the derivatives in the side strands for the oils branched off here.
  • the tubes of the single-tube reactor 8 and the jacket tube 9 expand here in the direction of flow.
  • the supply and discharge pipes 10 and 11 lead to the corresponding furnaces for heating the waste oil. If the pipes are arranged horizontally, it can avoid Fixing used oil and dirt on the bottom of the pipe can be very advantageous to provide means to swirl the used oil.
  • turbulators or one or more pipe constrictions can be used for this purpose. The latter can be created, for example, by indentations in the pipe. Changes in the direction of the pipe in waves or the like can also be useful for this.
  • Carrier media can also be introduced at the beginning or at any point along the reactor.
  • the described method according to the invention and the associated device for separating and hydrogenating waste oil can also be used analogously at corresponding pressures and temperatures for pyrolysis oil which is obtained in the pyrolysis of waste materials or other substances, in particular in the pyrolysis of waste tires and plastic waste.
  • the single-tube reactor has great advantages because of its great preparation and product selectivity.

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  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP87202165A 1986-11-12 1987-11-03 Procédé et dispositif de retraitement en continu des huiles usagées Expired - Lifetime EP0267654B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87202165T ATE74953T1 (de) 1986-11-12 1987-11-03 Verfahren und vorrichtung zur kontinuierlichen aufbereitung von altoel.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE3638606 1986-11-12
DE19863638606 DE3638606A1 (de) 1986-11-12 1986-11-12 Vorrichtung und verfahren zur kontinuierlichen aufbereitung von altoel
DE19873703110 DE3703110A1 (de) 1986-11-12 1987-02-03 Verfahren zur kontinuierlichen aufbereitung von altoel
DE3703110 1987-02-03

Publications (3)

Publication Number Publication Date
EP0267654A2 true EP0267654A2 (fr) 1988-05-18
EP0267654A3 EP0267654A3 (en) 1988-10-05
EP0267654B1 EP0267654B1 (fr) 1992-04-15

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EP87202165A Expired - Lifetime EP0267654B1 (fr) 1986-11-12 1987-11-03 Procédé et dispositif de retraitement en continu des huiles usagées

Country Status (7)

Country Link
US (1) US4894140A (fr)
EP (1) EP0267654B1 (fr)
BR (1) BR8706088A (fr)
CA (1) CA1296281C (fr)
DE (2) DE3703110A1 (fr)
ES (1) ES2031123T3 (fr)
MX (1) MX169346B (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1992019705A1 (fr) * 1990-01-16 1992-11-12 Schoen Christian O Procede et dispositif de traitement de dechets organiques coulants contenant des matieres nocives
AU638922B1 (fr) * 1992-10-01 1993-07-08
AU667303B2 (en) * 1991-05-07 1996-03-21 Christian O. Schon Process and device for processing free-flowing organic waste materials containing noxious substances

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DE3820317A1 (de) * 1988-06-15 1989-12-21 Christian O Schoen Verfahren zum zerlegen schaedliche oder umweltbelastende bestandteile enthaltender fliessfaehiger organischer medien
US6805062B2 (en) * 1988-09-20 2004-10-19 Edward Carlton Shurtleff Apparatus and method for reclaiming useful oil products from waste oil including hydrogen injection
US5527449A (en) * 1993-03-25 1996-06-18 Stanton D. Brown Conversion of waste oils, animal fats and vegetable oils
US5362381A (en) * 1993-03-25 1994-11-08 Stanton D. Brown Method and apparatus for conversion of waste oils
US5389691A (en) * 1993-09-07 1995-02-14 Univ. Of Wyoming Process for co-recycling tires and oils
US5942127A (en) * 1993-09-21 1999-08-24 Wilcox; Steven Ian Fuel oil treatment unit and associated method
DE4410672C2 (de) * 1994-03-26 1996-04-04 Christian O Schoen Verfahren zur Wiederverwertung von Kunststoff
KR0171501B1 (ko) * 1996-08-28 1999-03-20 이성래 폐유 재생 장치 및 방법
US6132596A (en) * 1997-01-24 2000-10-17 Yu; Heshui Process and apparatus for the treatment of waste oils
US8366912B1 (en) 2005-03-08 2013-02-05 Ari Technologies, Llc Method for producing base lubricating oil from waste oil
WO2011034266A2 (fr) * 2009-09-21 2011-03-24 Korea Research Institute Of Chemical Technology Appareil pour récupérer du styrène monomère et procédé de récupération de styrène monomère à l'aide d'un solvant auxiliaire
EP2530135B1 (fr) * 2011-05-30 2022-05-25 GEA Mechanical Equipment GmbH Procédé destiné à la clarification d'huile de pyrolyse
US20140257000A1 (en) 2013-03-07 2014-09-11 Verolube, Inc. Method for producing base lubricating oil from oils recovered from combustion engine service
US9475029B2 (en) * 2013-08-28 2016-10-25 Louisiana Eco Green, L.L.C. Method of manufacturing bio-diesel and reactor
RU2694771C1 (ru) * 2019-01-14 2019-07-16 Общество с ограниченной ответственностью "ХАММЕЛЬ" Способ тепловой регенерации отработанных технологических жидкостей
RU2728970C1 (ru) * 2020-02-04 2020-08-03 Общество с ограниченной ответственностью "НефтеХимКонсалт" Способ двухступенчатой тепловой регенерации отработанных промышленных жидкостей

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US4290999A (en) * 1978-02-08 1981-09-22 The President Of Yamagata University Apparatus for direct liquefaction
DE2923974A1 (de) * 1979-02-07 1980-08-21 Montedison Spa Reaktionsvorrichtung zur durchfuehrung von reaktionen von mindestens einem gasfoermigen reaktionsteilnehmer mit mindestens einem fluessigen reaktionsteilnehmer
DE2940630A1 (de) * 1979-10-06 1981-04-09 Degussa Ag, 6000 Frankfurt Verfahren zur wiederaufbereitung von gebrauchten schmieroelen
DE3405858A1 (de) * 1983-02-16 1984-08-16 Exxon Research And Engineering Co., Florham Park, N.J. Verfahren zur wiederaufbereitung von altoelen

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1992019705A1 (fr) * 1990-01-16 1992-11-12 Schoen Christian O Procede et dispositif de traitement de dechets organiques coulants contenant des matieres nocives
AU667303B2 (en) * 1991-05-07 1996-03-21 Christian O. Schon Process and device for processing free-flowing organic waste materials containing noxious substances
AU638922B1 (fr) * 1992-10-01 1993-07-08

Also Published As

Publication number Publication date
BR8706088A (pt) 1988-06-21
EP0267654B1 (fr) 1992-04-15
EP0267654A3 (en) 1988-10-05
MX169346B (es) 1993-06-30
DE3778303D1 (de) 1992-05-21
US4894140A (en) 1990-01-16
CA1296281C (fr) 1992-02-25
ES2031123T3 (es) 1992-12-01
DE3703110A1 (de) 1987-10-08

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