WO1992019705A1 - Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe - Google Patents
Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe Download PDFInfo
- Publication number
- WO1992019705A1 WO1992019705A1 PCT/EP1992/000933 EP9200933W WO9219705A1 WO 1992019705 A1 WO1992019705 A1 WO 1992019705A1 EP 9200933 W EP9200933 W EP 9200933W WO 9219705 A1 WO9219705 A1 WO 9219705A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stage
- energy
- product
- reactor
- tube
- Prior art date
Links
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/242—Tubular reactors in series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00058—Temperature measurement
- B01J2219/00063—Temperature measurement of the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00157—Controlling the temperature by means of a burner
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
Definitions
- the invention relates to a method and a device for processing flowable organic waste materials containing harmful and polluting components, e.g. Waste oils, preferably chlorine-containing ones, using a multi-stage single-tube reactor which can be fed by a conveying device, in which an energy exchange, in particular thermal energy, takes place through the tube with the waste material, the waste material being at least partially converted into a gaseous phase and the energy flow and time, during which each molecule of the waste material is exposed to this flow of energy is regulated in such a way that the activation energy required for the separation of the harmful or environmentally harmful constituents is established for a binding solution between the respective molecules or atoms of the constituents and the reusable substances .
- harmful and polluting components e.g. Waste oils, preferably chlorine-containing ones
- Flowable organic waste materials are here to be understood as liquid waste materials which, together with undesirable toxic or environmentally harmful constituents, contain recyclable raw materials.
- waste oil for example, the oil should be reused as new oil, ie without the contaminants contained in the waste oil, for example from internal combustion engines.
- chlorine- and sulfur-containing hydrocarbon compounds, as well as bottom products, which are obtained as distillation residues in known processing methods and are to be further processed, are meant.
- Dwell time is to be understood as the time during which the product is exposed to a certain influencing variable, that is to say in particular a certain temperature or energy, when it flows through the reactor.
- the single-tube reactor therefore makes it possible for every particle down to the molecule to be exposed to absolutely the same adjustable variables, which can be used to act specifically on the molecules or atoms of the product.
- the present invention is based on the object of further improving this method, which is in itself quite good, of expanding its application possibilities and, in particular, of making it even more economical. Furthermore, the separation of two valuable material components into two individual components should be made possible, e.g. Mixtures of mineral and vegetable waste oils.
- the invention solves the problem in that, after each stage, the pollutant fractions separated in this stage are separated into a sump and in each stage the activation energy required for the respective product and previously experimentally obtained and possibly modified by an activation energy regulated in the respective stage is set again each time.
- the desired product is preferably at least partially condensed.
- the condensation can be carried out either as total or partial condensation or as fractional condensation.
- necessary conveying devices umps, turbo blowers, etc.
- the activation energy in the second stage is lower than in the first stage and energy can be removed from this stage in a controlled manner, for example by cooling. It is crucial that the energy is adjusted in each stage so that an optimal reaction is obtained.
- the reaction that fulfills customer requirements or that ensures optimal disposal is optimal. It can be of high quality, for example with used oil, if the pollutants are removed and the lubricating properties are good. It is even possible to determine the quality of the product, for example the degree of refining for waste oil, either by the percentage of the Sodium or by changing the activation energy or the residence time. Quantitatively, it is optimal if, for example, in the case of PCBs (polychlorinated biphenyls), these are removed to below the officially prescribed permissible value.
- PCBs polychlorinated biphenyls
- a vacuum pump is expediently connected between the condensation zone and the gasification zone via a liquid separator is.
- the energy supply is expediently regulated in individual sections within a stage between two separators for the pollutant fractions, i.e. For example, one section for the condensation, one for the subsequent conversion back into the gaseous phase and possibly another for a reaction when metering in auxiliary chemicals.
- auxiliary chemicals can be metered in in individual stages depending on the product and according to the process requirements or the disposal requirements along the reactor.
- the auxiliary chemicals perform various functions, which also depend on the temperatures at which the flowing product is located.
- the same forms of energy for changing the activation energy can be used in the present invention, as are mentioned in the above-mentioned property rights of the same inventor, such as, for example, washing the pipes with a liquid or gaseous heating or cooling medium or with elementary particle bombardment by high-energy ones Electron, proton or neutron radiation in the megarad range, high voltage in the range from 10,000 to 100,000 volts, ion implantation by suitable ionization, ie electromagnetic vibration excitation over the megahertz range, preferably in the gigahertz range, etc.
- the regulation of the energy effect in each stage can be carried out in a known manner by measuring the temperature at the end of the stage and thus regulating the energy to be supplied or removed.
- the control of the energy effect with constant energy flow is carried out by regulating the flow velocity in each tube step, ie by influencing the duration of this energy flow on the flowing product.
- the constant energy flow can be generated by a centrally regulated energy source. Inevitable inaccuracies in the tube diameters or different properties of the tube inner surfaces are thereby compensated for with regard to the high levels of accuracy required for controlling the flow of energy to the flowing product in the method according to the invention.
- a hydrogenation process is initiated in one stage, preferably the second stage.
- the second stage in the case of certain products, can also be carried out as a fractional condensation in a two-stage process, as described in the above-mentioned publications by the inventor.
- a device for carrying out the method according to the invention with a plurality of stages arranged one behind the other is characterized by a reactor in which the tube of each stage has a length to diameter ratio of at least 200: 1 (for example length 1000 cm, diameter 5 cm) with a minimum diameter of 10 mm and has a separator after each stage for separating the separated harmful substances into a sump.
- the tube diameter can be 0.5 m or less, for example, but a diameter of 0.5 ra can also be provided with a length of 700 m. Also the diameters can vary over the length.
- a condensing device e.g. for fractional condensation.
- the tubes of the individual stages can be designed as double-wall tubes, which can be acted upon by a heating or cooling medium, or the tubes can be surrounded by a boiler room, in which e.g. Flue gases heated by a burner rinse and heat the pipes.
- Devices can be installed in the separator, e.g. High-voltage charges or baffle plates, as are known in gas technology for the separation of dusts and dirt. The same also applies to internals that serve to agglomerate aerosols.
- an intermediate condenser is expediently arranged at this point, through which the gaseous product can be liquefied again, and then in a subsequent section of this stage to be converted back into the gaseous phase.
- the product can also be fed in from the outset in gaseous form, possibly with impurities, just as the cleaned product can also leave the reactor in gaseous or partially gaseous form for further processing.
- the invention is explained below with reference to examples in the drawing. Show in it
- Fig. 3 in the scheme a four-stage device according to the
- FIG. 5 shows a detail from FIG. 4 with an alternative embodiment of this cut-off
- the product to be processed e.g. an old oil
- the heating chamber 4 is heated by a burner 5, the flue gases emerging from the chamber 4 at 6.
- the flow rate of the product in the tubular reactor 3 is constantly regulated by a controller 7.
- a separator 8 is arranged for bottom products separated in this stage, which exit into the bottom 10 at 9, while the product converted into a gaseous phase in the first stage comes out of the separator at 11 8 exits.
- the temperature of the product is measured at 12 and fed back to the burner control unit for regulating the burner to a constant temperature.
- dashed lines As shown by dashed lines
- auxiliary chemicals may be metered in at these points.
- the product emerging from the separator 8 is passed via the pipeline 14 into the second stage 16 of the tubular reactor.
- a funding facility 15 can be provided to support the funding.
- the second stage 16 and third stage 17 are identical in terms of heating and separation to the first stage, with the difference that in the example shown, no device for metering in auxiliary chemicals is provided in the third stage.
- the finished product is removed after the third stage via a condenser 18 and a pull-off pump 19.
- the capacitor 18 can be designed, for example, for fractional condensation, as is shown in the above-mentioned property rights of the same inventor.
- a vacuum pump 20 provides the required vacuum in the system.
- the embodiment according to FIG. 2 shows a device according to the invention with two parallel tube reactors in each stage.
- the product supplied here by a feed pump 1 is branched in a first stage 21 into two reactor strands 22 and 23, both of which are guided parallel to one another through the heating chamber 4 which can be heated by the burner 5 and are heated there.
- the temperature of the heating gases is regulated to a constant value by means of the regulator 24 measuring in the flue gas outlet 6.
- regulators 25 and 26 regulate the flow rate of the product separately in both reactor lines 22 and 23 via valves 27 and 28.
- Auxiliary chemicals can be metered into the two reactor strands 22 and 23 at the points indicated by dashed arrows 29.
- a common separator 30 from which separated bottom products are separated into the bottom 31, while the gaseous product via a pipe 32 and possibly a conveyor 33 into the next Level 34 reached.
- This stage and the subsequent stage 35 are generally designed in exactly the same way as the first stage 21.
- the product emerging from the third stage is fed to a condensation method known per se with a capacitor 36 via the pump 37.
- a vacuum pump 38 provides the vacuum in the system.
- FIG. 3 shows a four-stage device in which the reactor tube part 40 of each stage 41, 42, 43 and 44 is surrounded by a temperature jacket 45 at a distance, the space between each reactor tube part and jacket 45 being separated from a heating medium can be flowed through in countercurrent, which enters at 46 and exits at 47.
- Each stage is individually regulated by a temperature controller 48 to a constant temperature separately defined for each stage, while the flow rate is regulated by a controller 49 at the inlet 50 into the reactor.
- a separator 51, 52, 53 and 54 is provided for harmful components separated in the respective stage for separation into the respectively assigned sump 55, 56, 57 and 58.
- feeders 59 and 60 each with metering pumps 61, for dispensing auxiliary chemicals, are arranged in the second and third stages.
- a pipeline 62 leads to a condenser 63, known per se, with a draw-off pump 64.
- a vacuum pump 65 again provides the required negative pressure in the system.
- special facilities 66 for gas production can optionally be provided.
- a four-stage tubular reactor is shown with differently designed stages, the temperature of which is carried out in each case via a heating medium guided in double-wall tubes, as explained in more detail below.
- the product to be treated which is fed to the tubular reactor 70 via a feed pump 1, first flows through a first stage 71, which is designed as a reactor and is surrounded at a distance by a temperature jacket 72 for the temperature control medium.
- a temperature controller 73 which is regulated by a temperature controller 73, the product is converted into a gaseous one Phase transferred.
- the flow rate is regulated very precisely by a controller 74.
- a separator 75 is again provided in the sump 76 for the pollutants separated off in this first stage.
- a section 78 for a condensation and a subsequent liquid separator 79 is arranged, from which a line 80 leads to a vacuum pump (not shown).
- the section 78 for the condensation is surrounded by a temperature control jacket 81, the temperature in this area being regulated individually by the controller 82.
- a feed pump 86 is provided in front of the next section 83, in which the product is again converted into a gaseous phase and which is surrounded by a temperature jacket 84 with an individual controller 85.
- the next and last reactor section 87 of this stage is surrounded by a temperature jacket 88 with an individual controller 89 for the heating temperature.
- Lines 91 connected to a metering pump 90 lead into this reactor section for metering in auxiliary chemicals.
- stage 77 there is again a separator 92 with sump 93 for receiving the pollutant parts separated off in this stage 77.
- the next stage 94 is constructed in exactly the same way as stage 77, while in this exemplary embodiment the last stage 95 only has a reactor section 96 with a temperature jacket 97 and a temperature controller 98.
- a separator 99 is provided, from which pollutants are again discharged into a sump 100, while the product is discharged via a condenser 101 and a draw-off pump 102.
- a vacuum pump 103 ensures sufficient negative pressure in the system.
- FIG. 5 shows a detail of an alternative embodiment in the area of the separator 79 of FIG. 4.
- a side fraction for gases which are undesirable in the end product is drawn off via the line 80 and the condenser 104.
- Condensed liquid is drawn off via a separator 105 and pump 106, while line 107 leads to a vacuum pump, not shown.
- This arrangement shown here can be provided in the same way at the corresponding point in stage 94 of FIG. 4.
- Fig. 6 another embodiment is shown for the hydrogenation of dewatered waste oil.
- the waste oil supplied by the pump 1 is converted into a gaseous phase in the first reactor stage 109 with reactor tube 110, temperature jacket 111 and temperature controller 112. Harmful constituents are discharged into the sump 114 via the separator 113.
- an alkaline earth oxide hydrate for example hydrated lime
- sodium is fed in at around 310 ° C. along the tube reactor in such a way that the waste oil is refined in a controlled manner.
- the sodium content largely depends on the chlorine-sodium content and the desired degree of refining of the oil. In the case of conventional waste oil, this can be around 0.4-2%.
- the chlorine components are also converted to NaCl.
- the bottom product is separated off.
- bleaching earth is metered in at around 340 ° C to optically brighten the oil.
- a hydrogenation process is carried out in the second stage, about 0.5 to 1% of Bayer mass (red mud) being mixed in as catalyst in this stage and about 10 to 15% of H, based on reactive oil, along the reactor.
- Bayer mass red mud
- a mixture of mineral and vegetable waste oils is to be separated and worked up, using a device according to FIG. 1 with three stages.
- the mixture is heated to about 200 to 250 ° C.
- the separator 8 of this stage the vegetable oil is separated from the mixture.
- the temperature of the product is cooled down to at least 100 ° C.
- the mineral oil is separated in the separator 8 'of this second stage.
- the vacuum pump 20 ensures that the entire process is carried out at a vacuum of approx. 3-5 mbar.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE59203239T DE59203239D1 (de) | 1991-05-07 | 1992-04-29 | Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe. |
BR9205975A BR9205975A (pt) | 1991-05-07 | 1992-04-29 | Processo e dispositivo para reprocessamento de resíduos orgânicos, fluidos, contendo componentes nocivos e poluentes do meio ambiente |
JP4508520A JPH06510674A (ja) | 1991-05-07 | 1992-04-29 | 有害な成分を含有する流動性有機廃棄物の処理方法及び装置 |
EP92909403A EP0585260B1 (de) | 1991-05-07 | 1992-04-29 | Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe |
AU16536/92A AU667303B2 (en) | 1991-05-07 | 1992-04-29 | Process and device for processing free-flowing organic waste materials containing noxious substances |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US89414090A | 1990-01-16 | 1990-01-16 | |
US55998590A | 1990-07-30 | 1990-07-30 | |
DEP4114883.5 | 1991-05-07 | ||
DE4114883A DE4114883A1 (de) | 1991-05-07 | 1991-05-07 | Verfahren und vorrichtung zum aufarbeiten wiederverwertbare oder schaedliche bestandteile enthaltender fliessfaehiger organischer abfallstoffe |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1992019705A1 true WO1992019705A1 (de) | 1992-11-12 |
Family
ID=27202448
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1992/000933 WO1992019705A1 (de) | 1990-01-16 | 1992-04-29 | Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe |
Country Status (1)
Country | Link |
---|---|
WO (1) | WO1992019705A1 (de) |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0267654A2 (de) * | 1986-11-12 | 1988-05-18 | Christian O. Schön | Verfahren und Vorrichtung zur kontinuierlichen Aufbereitung von Altöl |
WO1989012482A1 (en) * | 1988-06-15 | 1989-12-28 | Schoen Christian O | Process and device for separating harmful substances |
-
1992
- 1992-04-29 WO PCT/EP1992/000933 patent/WO1992019705A1/de active IP Right Grant
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0267654A2 (de) * | 1986-11-12 | 1988-05-18 | Christian O. Schön | Verfahren und Vorrichtung zur kontinuierlichen Aufbereitung von Altöl |
WO1989012482A1 (en) * | 1988-06-15 | 1989-12-28 | Schoen Christian O | Process and device for separating harmful substances |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP3247775B1 (de) | Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizöl | |
EP0698075B1 (de) | Verfahren und vorrichtung zum dampfcracken einer leichten und einer schweren kohlenwasserstoffbeschickung | |
DE2520152C2 (de) | Verfahren zum trockenen Destillieren zerkleinerten organischen Abfallmaterials in einem Schneckenextruder | |
DE2628763B2 (de) | Verfahren und Vorrichtung zum Wiederaufbereiten von verbrauchten Schmierölen | |
WO2008125679A1 (de) | Verfahren und vorrichtung zur chromatographischen trennung von komponenten mit teilweiser rückführung von gemischfraktionen | |
EP0267654B1 (de) | Verfahren und Vorrichtung zur kontinuierlichen Aufbereitung von Altöl | |
EP0374198B1 (de) | Verfahren und vorrichtung zum abtrennen von schadstoffen | |
EP3883661A1 (de) | Verfahren und vorrichtung zur reinigung von verschmutztem altöl | |
EP0585260B1 (de) | Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe | |
DE202015009755U1 (de) | Anlage zum Überführen von Kunststoffabfällen in einen Brennstoff mit Eigenschaften von Diesel/Heizöl | |
DE202014010997U1 (de) | Vorrichtung zum Aufbereiten von Altöl | |
WO1992019705A1 (de) | Verfahren und vorrichtung zum aufarbeiten schädliche bestandteile enthaltender fliessfähiger organischer abfallstoffe | |
DE3224114A1 (de) | Verfahren zum erwaermen von fluessigkeiten mit dabei zur bildung von ablagerungen neigenden bestandteilen | |
DE4040145A1 (de) | Verfahren zur abtrennung von aromaten aus kohlenwasserstoffgemischen beliebigen aromatengehaltes | |
DE1795340A1 (de) | Verfahren zur Kompression von Wasserstoff | |
DE3638606A1 (de) | Vorrichtung und verfahren zur kontinuierlichen aufbereitung von altoel | |
DE102018106311A1 (de) | Verfahren und Vorrichtung zum Behandeln von Öl | |
DE4235214A1 (de) | Verfahren zur Aufbereitung von Kohlenwasserstoffverbindungen mit Hilfe eines Plasmareaktors | |
DE4410672C2 (de) | Verfahren zur Wiederverwertung von Kunststoff | |
CH691928A5 (de) | Schmelzofen zur thermischen Behandlung von schwermetallhaltigen und/oder dioxinhaltigen Sonderabfällen. | |
EP4056632A1 (de) | Verfahren und anlage zur depolymerisation von kunststoffmaterial | |
BE1029920B1 (de) | Verfahren zur Entleerung eines Lösungsmittel-Regenerierungs-Behälters sowie Vorrichtung | |
DE4235213C2 (de) | Verfahren zur Reinigung von verschmutzten Kohlenwasserstoffen | |
DE202018101508U1 (de) | Vorrichtung zm Behandeln von Öl | |
AT398428B (de) | Vorrichtung zum thermischen spalten eines gemisches mit flüssigen und gasförmigen kohlenwasserstoffen |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AU BR CA JP KR US |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FR GB GR IT LU MC NL SE |
|
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) | ||
WWE | Wipo information: entry into national phase |
Ref document number: 1992909403 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2102603 Country of ref document: CA |
|
WWP | Wipo information: published in national office |
Ref document number: 1992909403 Country of ref document: EP |
|
WWG | Wipo information: grant in national office |
Ref document number: 1992909403 Country of ref document: EP |