CA1337161C - Method and apparatus for reducing the co content in waste gases from garbage incineration installations - Google Patents
Method and apparatus for reducing the co content in waste gases from garbage incineration installationsInfo
- Publication number
- CA1337161C CA1337161C CA000615143A CA615143A CA1337161C CA 1337161 C CA1337161 C CA 1337161C CA 000615143 A CA000615143 A CA 000615143A CA 615143 A CA615143 A CA 615143A CA 1337161 C CA1337161 C CA 1337161C
- Authority
- CA
- Canada
- Prior art keywords
- burners
- boiler
- rotary kiln
- flue
- waste gases
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B37/00—Component parts or details of steam boilers
- F22B37/008—Adaptations for flue gas purification in steam generators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
- F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
- F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/40—Carbon monoxide
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Incineration Of Waste (AREA)
- Muffle Furnaces And Rotary Kilns (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to a method and an apparatus for reducing the CO content of waste gases produced in garbage incineration installations, where the garbage is incinerated, for example, in a rotary kiln and the waste gases are sent to a waste heat boiler downstream of the furnace. In this boiler, the waste gases arriving from the rotary kiln are thoroughly mixed with the aid of jets of combustion gas burners, thus intensifying the reaction between CO and O2.
Description
13371~1 The invention relates to a method and an apparatus for reducing the CO content of waste gases produced in incinerators, especially incinerators for domestic and special garbage, where this garbage is incinerated, for example, in a rotary kiln and the waste gases are sent through a boiler downstream of the furnace.
Waste gases produced in garbage incin-erators, and also those derived from coal fired power plant boilers, contain, among other th1ngs, carbon monoxide, the amount of which should be kept as small as possible. The requirement for TA air is that it should be a pure gas containing less than lOOmg/m of carbon monoxide.
In the case of garbage incinerators, for example, the garbage is charged into a rotary kiln, operating in parallel flow where it is incinerated.
These kilns end up in waste heat boilers in which the slag is removed from the bottom while the waste gases or flue gases flow through the first boiler flue almost perpendicularly from bottom to top. After a deflection there follows a further heat exchange in a convection part. The waste heat boiler is followed by a waste gas cleaning processing for dehalogenizing, desulphurizing and dust removal.
The oxygen content of the boiler amounts to about 10% and the fule gas~-temperatures in the lower part of the first boiler flue usually exceed 800C.
The oxygen originates with the rotary kiln process and with the so-called secondary air supply.
Since this prerequisite per se should produce satisfactory burn out of -the CO in the waste gas, it is assumed tha-t jets form in the waste gas and that the mixing of waste gases and atmospheric oxygen is inadequate. ~
~' Now it is an object of the invention to reduce the CO content of the waste gases of incinerators.
According to the invention, this is accomplished by thoroughly mixing the waste gases in the lower part of the waste heat boiler downstream of the furnace, and for this purpose the combustion gases are injected into the boiler through burners, for example high velocity burners.
The combustion gases are, preferably injected into the boiler at right angles with respect to the direction of flow of the waste gases, preferably at a velocity of about 100 m/s or more.
It is desirable to inject the combustion gases into the boiler in several different planes or levels and from opposite sides of the boiler.
A suitable apparatus for the implementation of this method comprises a plurality of burners, e.g.
high velocity burners, which are incorporated into the first boiler flue, and which are preferably arranged immediately above the outlet from the rotary kiln into the boiler, the combustion gas outlet nozzles being directed towards the interior of the boiler.
The burners are preferably built into two opposite walls of the boiler and are directed towards each other, while being arranged in several vertical planes one above the other.
The combustion gas outlet nozzles of the burners run substantially horizontally.
The burners facing each other in the two walls of the boiler are preferably adjustable in height in relation to each other, the burners built into one wall of the boiler being alternately adjustable in height in relation -to each other.
According to another embodiment of the invention, additional burners may be provided in the boiler above these burners, the said additional burners being arranged horizontally with respect to the burners first mentioned and being staggered in relation thereto by half the distance between the centres thereof.
A preferred embodiment of the invention is described hereinafter in conjunction with the drawing attached hereto, wherein:
Fig. 1 illustrates diagrammatically the end of a rotary kiln projecting into the first boiler flue of a waste heat boiler; and Fig. 2 is a cross-section taken along line II-II of Fig. 1.
The temperatures in the first radiation flue of the boiler, immediately above the end of the rotary kiln, are about 1000 - 1500C, about 750 - 850C in the middle of the flue, and about 600 - 700C at the upper end in the area of deflection of the flue. These temperatures fluctuate, depending upon the composition of the garbage, the method of operating the furnace, and the degree of contamination of the boiler, as cause for example by fly-ash and/or other solid or liquid deposits produced by the combustion reaction within the boiler, for instance by residues of incomplete combustion within the boiler.
However, in view of these temperatures, mechanical circulation devices seem undesirable, especially for reasons of operating safety.
According to the invention, therefore, flue gases are thoroughly mixed with the aid of burners, more particularly high velocity burners.
High velocity burners are to be understood to mean burners in which combustion takes place in a combustion chamber provided in the burner, the combustion gases flowing into the boiler or boiler flue at speeds of 100 m/s or more.
The waste gases or flue gases flowing through the boiler are drawn in and are thoroughly mixed by the high outlet pulses of the combustion gases emerging from the burners, in order to achieve a reaction which is as complete as possible between CO and 2 Fig. 1 illustrates diagrammatically the end of a rotary kiln 10 projecting into the first radiation flue or boiler flue 14 of a boiler marked generally 12. Between the outer periphery of rotary kiln 10, and the opening in boiler flue 14, there is an annular gap between 10 and 40 mm wide, for example, through which so called secondary air enters boiler 12. However, this gap is not shown in Fig. 1.
Waste gases from rotary kiln 10 flow vertically in boiler flue 14 from bottom to top.
According to the invention they are thoroughly mixed in the flue with each other and with secondary air.
Above the inlet end of rotary kiln 10, in boiler flue 14, preferably directly above, there are provided burners 16, 18, 20, 22, 24, 26, more particularly so called high velocity burners. These burners are mounted and installed in opposed side walls 36, 38 of boiler flue 14.
In the example illustrated, three burners are built into each side wall in boiler flue 14, namely burners 16, 18, 20 in side wall 38 and burners 22, 24, 26 in side wall 36.
Burners 16, 18, 20 thus face burners 22, 24, 26 and the jets of combustion gas emerging from nozzles 30 are direc,ed towards one another.
In the vertical direction, individual burners are adjustable in height in relation to each other. For example, burners 16, 18, 20 may lie in one plane while burners 22, 24, 26 may lie in another higher plane.
It has also been found desirable for the burners installed in one of walls 36 or 38 to be adjustable in height in relation to each other, as shown in Fig. 1.
Thus burners 16 and 20, installed in wall 38, lie in a horizontal plane extending through burners 16 and 20, but burner 18 lies in a higher plane. The same applied to burners 22, 24, 26 mounted in wall 36 of boiler flue 14. In this case, as shown in Fig. 1, burners 22 and 26 lie in the upper plane whereas burner 24, built into wall 36 between burners 22 and 26, is arranged in a lower plane.
Both the vertical and horizontal cross-section of the burners can be selected as a function of the radiation cone 32 of the combus-tion gases emerging from burner nozzles 30.
Measurements have shown that the angle of this cone 32 amounts to about 20.
It is desirable for the horizontal distance between the burners to be such that radiation cones 32 meet and in-tersect approximately at the central plane 40 of the boiler flue 14.
The same applies to the vertical distance A
between the two groups of burners.
The centre line of burner nozzles 30 (and thus the centre line of radiation cones 32) preferably extends horizontally and at right angles to side wall 36 or 38. It must be emphasized however that this need not be the case, i.e. the centre lines of the burner nozzles or radiation cones centre lines may also be upwardly or downwardly inclined at an acute angle with respect to the horizontal. They may also form with relevant side wall 36 or 38 an angle other than 90. (The term horizontal relates to the fact that boiler flue 14 is arranged vertically and that the waste gases from rotary kiln 10 flow vertically from bottom to top).
With this arrangement of burners 16 - 26, the horizontal and vertical spacing of which corresponds to the diameter of the jet 1n the middle of the boiler flue 14, very thorough mixing of the waste gases flowing in boiler flue 14 from bottom to top is already obtained, since this arrangement already covers a very large part of the cross-sectional area of the boiler flue. The alternate displacement of individual burners causes frequent deflection of the waste gases ascending in the boiler flue, thus intensifying the mixing and reaction. The burners are preferably arranged as close as possible, i.e. immediately above the outlet from rotary kiln 10, thus ensuring that secondary air is drawn up from the burner jets at the highest possible temperature and that the longest possible time is provided for the oxygen to react with the carbon monoxide.
In addition, more burners 28 may be provided above burners 16 - 26, e.g. two burners in each of two further planes and which are constructed in the same way as burners 16 - 26. However, burners 28 are preferably arranged horizontally in relation to burners 22, 18, 26 and are staggered by half the distances between the centres thereof.
With these additional burners 28 it is possible to mix jets of waste gas not yet covered by the lower groups of burners, thus still further improving the reaction between CO and 2 The burners themselves, which are available on the market, may be operated with propane gas, for example.
Waste gases produced in garbage incin-erators, and also those derived from coal fired power plant boilers, contain, among other th1ngs, carbon monoxide, the amount of which should be kept as small as possible. The requirement for TA air is that it should be a pure gas containing less than lOOmg/m of carbon monoxide.
In the case of garbage incinerators, for example, the garbage is charged into a rotary kiln, operating in parallel flow where it is incinerated.
These kilns end up in waste heat boilers in which the slag is removed from the bottom while the waste gases or flue gases flow through the first boiler flue almost perpendicularly from bottom to top. After a deflection there follows a further heat exchange in a convection part. The waste heat boiler is followed by a waste gas cleaning processing for dehalogenizing, desulphurizing and dust removal.
The oxygen content of the boiler amounts to about 10% and the fule gas~-temperatures in the lower part of the first boiler flue usually exceed 800C.
The oxygen originates with the rotary kiln process and with the so-called secondary air supply.
Since this prerequisite per se should produce satisfactory burn out of -the CO in the waste gas, it is assumed tha-t jets form in the waste gas and that the mixing of waste gases and atmospheric oxygen is inadequate. ~
~' Now it is an object of the invention to reduce the CO content of the waste gases of incinerators.
According to the invention, this is accomplished by thoroughly mixing the waste gases in the lower part of the waste heat boiler downstream of the furnace, and for this purpose the combustion gases are injected into the boiler through burners, for example high velocity burners.
The combustion gases are, preferably injected into the boiler at right angles with respect to the direction of flow of the waste gases, preferably at a velocity of about 100 m/s or more.
It is desirable to inject the combustion gases into the boiler in several different planes or levels and from opposite sides of the boiler.
A suitable apparatus for the implementation of this method comprises a plurality of burners, e.g.
high velocity burners, which are incorporated into the first boiler flue, and which are preferably arranged immediately above the outlet from the rotary kiln into the boiler, the combustion gas outlet nozzles being directed towards the interior of the boiler.
The burners are preferably built into two opposite walls of the boiler and are directed towards each other, while being arranged in several vertical planes one above the other.
The combustion gas outlet nozzles of the burners run substantially horizontally.
The burners facing each other in the two walls of the boiler are preferably adjustable in height in relation to each other, the burners built into one wall of the boiler being alternately adjustable in height in relation -to each other.
According to another embodiment of the invention, additional burners may be provided in the boiler above these burners, the said additional burners being arranged horizontally with respect to the burners first mentioned and being staggered in relation thereto by half the distance between the centres thereof.
A preferred embodiment of the invention is described hereinafter in conjunction with the drawing attached hereto, wherein:
Fig. 1 illustrates diagrammatically the end of a rotary kiln projecting into the first boiler flue of a waste heat boiler; and Fig. 2 is a cross-section taken along line II-II of Fig. 1.
The temperatures in the first radiation flue of the boiler, immediately above the end of the rotary kiln, are about 1000 - 1500C, about 750 - 850C in the middle of the flue, and about 600 - 700C at the upper end in the area of deflection of the flue. These temperatures fluctuate, depending upon the composition of the garbage, the method of operating the furnace, and the degree of contamination of the boiler, as cause for example by fly-ash and/or other solid or liquid deposits produced by the combustion reaction within the boiler, for instance by residues of incomplete combustion within the boiler.
However, in view of these temperatures, mechanical circulation devices seem undesirable, especially for reasons of operating safety.
According to the invention, therefore, flue gases are thoroughly mixed with the aid of burners, more particularly high velocity burners.
High velocity burners are to be understood to mean burners in which combustion takes place in a combustion chamber provided in the burner, the combustion gases flowing into the boiler or boiler flue at speeds of 100 m/s or more.
The waste gases or flue gases flowing through the boiler are drawn in and are thoroughly mixed by the high outlet pulses of the combustion gases emerging from the burners, in order to achieve a reaction which is as complete as possible between CO and 2 Fig. 1 illustrates diagrammatically the end of a rotary kiln 10 projecting into the first radiation flue or boiler flue 14 of a boiler marked generally 12. Between the outer periphery of rotary kiln 10, and the opening in boiler flue 14, there is an annular gap between 10 and 40 mm wide, for example, through which so called secondary air enters boiler 12. However, this gap is not shown in Fig. 1.
Waste gases from rotary kiln 10 flow vertically in boiler flue 14 from bottom to top.
According to the invention they are thoroughly mixed in the flue with each other and with secondary air.
Above the inlet end of rotary kiln 10, in boiler flue 14, preferably directly above, there are provided burners 16, 18, 20, 22, 24, 26, more particularly so called high velocity burners. These burners are mounted and installed in opposed side walls 36, 38 of boiler flue 14.
In the example illustrated, three burners are built into each side wall in boiler flue 14, namely burners 16, 18, 20 in side wall 38 and burners 22, 24, 26 in side wall 36.
Burners 16, 18, 20 thus face burners 22, 24, 26 and the jets of combustion gas emerging from nozzles 30 are direc,ed towards one another.
In the vertical direction, individual burners are adjustable in height in relation to each other. For example, burners 16, 18, 20 may lie in one plane while burners 22, 24, 26 may lie in another higher plane.
It has also been found desirable for the burners installed in one of walls 36 or 38 to be adjustable in height in relation to each other, as shown in Fig. 1.
Thus burners 16 and 20, installed in wall 38, lie in a horizontal plane extending through burners 16 and 20, but burner 18 lies in a higher plane. The same applied to burners 22, 24, 26 mounted in wall 36 of boiler flue 14. In this case, as shown in Fig. 1, burners 22 and 26 lie in the upper plane whereas burner 24, built into wall 36 between burners 22 and 26, is arranged in a lower plane.
Both the vertical and horizontal cross-section of the burners can be selected as a function of the radiation cone 32 of the combus-tion gases emerging from burner nozzles 30.
Measurements have shown that the angle of this cone 32 amounts to about 20.
It is desirable for the horizontal distance between the burners to be such that radiation cones 32 meet and in-tersect approximately at the central plane 40 of the boiler flue 14.
The same applies to the vertical distance A
between the two groups of burners.
The centre line of burner nozzles 30 (and thus the centre line of radiation cones 32) preferably extends horizontally and at right angles to side wall 36 or 38. It must be emphasized however that this need not be the case, i.e. the centre lines of the burner nozzles or radiation cones centre lines may also be upwardly or downwardly inclined at an acute angle with respect to the horizontal. They may also form with relevant side wall 36 or 38 an angle other than 90. (The term horizontal relates to the fact that boiler flue 14 is arranged vertically and that the waste gases from rotary kiln 10 flow vertically from bottom to top).
With this arrangement of burners 16 - 26, the horizontal and vertical spacing of which corresponds to the diameter of the jet 1n the middle of the boiler flue 14, very thorough mixing of the waste gases flowing in boiler flue 14 from bottom to top is already obtained, since this arrangement already covers a very large part of the cross-sectional area of the boiler flue. The alternate displacement of individual burners causes frequent deflection of the waste gases ascending in the boiler flue, thus intensifying the mixing and reaction. The burners are preferably arranged as close as possible, i.e. immediately above the outlet from rotary kiln 10, thus ensuring that secondary air is drawn up from the burner jets at the highest possible temperature and that the longest possible time is provided for the oxygen to react with the carbon monoxide.
In addition, more burners 28 may be provided above burners 16 - 26, e.g. two burners in each of two further planes and which are constructed in the same way as burners 16 - 26. However, burners 28 are preferably arranged horizontally in relation to burners 22, 18, 26 and are staggered by half the distances between the centres thereof.
With these additional burners 28 it is possible to mix jets of waste gas not yet covered by the lower groups of burners, thus still further improving the reaction between CO and 2 The burners themselves, which are available on the market, may be operated with propane gas, for example.
Claims (9)
1. An apparatus for incineration of domestic and special garbage having a rotary kiln leading into a boiler flue of a waste heat boiler, wherein an annular gap is formed between an outer periphery of the rotary kiln and an opening provided in the boiler flue and having a cleaning installation for exhaust gases downstream of the waste heat boiler, characterized in that, a plurality of high velocity burners are incorporated into the waste heat boiler, above the outlet from the rotary kiln into the boiler, said burners having outlet nozzles being directed towards the interior of said boiler.
2. An apparatus according to claim 1, characterized in that the burners are arranged immediately above the outlet from the rotary kiln into the boiler.
3. An apparatus according to claim 1, characterized in that the burners are directed towards each other from two opposed side walls of the boiler.
4. An apparatus according to claim 1, 2 or 3, characterized in that the burners are arranged in several vertical planes, one above the other.
5. An apparatus according to claim 1, characterized in that the outlet nozzles from the burners extend substantially horizontally.
6. An apparatus according to claim 3, characterized in that the burners facing each other in the two side walls of the boiler are arranged to be adjustable in height in relation to each other.
7. An apparatus according to claim 3, characterized in that burners provided on one wall of the boiler are arranged to be alternately adjustable in height.
8. An apparatus according to one of claims 1-3 and 5-7, characterized in that the horizontal and vertical distance between the burners corresponds approximately to the diameter of a cone of a jet of combustion gas from the burners in the middle of the boiler.
9. An apparatus according to one of claims 1-3 and 5-7, characterized in that additional burners arranged horizontally in relation to the burners and staggered by half the distance between the centres thereof are incorporated into the boiler above the burners.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3839503.7 | 1988-11-23 | ||
| DE3839503A DE3839503A1 (en) | 1988-11-23 | 1988-11-23 | METHOD AND DEVICE FOR REDUCING THE CO CONTENT IN EXHAUST GAS FROM COMBUSTION PLANTS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1337161C true CA1337161C (en) | 1995-10-03 |
Family
ID=6367699
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000615143A Expired - Fee Related CA1337161C (en) | 1988-11-23 | 1989-09-29 | Method and apparatus for reducing the co content in waste gases from garbage incineration installations |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0370184B1 (en) |
| AT (1) | ATE98357T1 (en) |
| CA (1) | CA1337161C (en) |
| DE (2) | DE3839503A1 (en) |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3043279A (en) * | 1954-06-18 | 1962-07-10 | Svenska Maskinverken Ab | Steam boiler plant |
| DE1289938B (en) * | 1966-03-26 | 1969-02-27 | Duerrwerke Ag | With a coal dust-heated steam generator for the highest pressures and temperatures combined waste incineration plant |
| DE1947164A1 (en) * | 1969-09-18 | 1971-03-25 | Koppers Wistra Ofenbau Gmbh | Waste incineration plant |
| CH583881A5 (en) * | 1975-07-04 | 1977-01-14 | Von Roll Ag | |
| US4162686A (en) * | 1977-10-17 | 1979-07-31 | North American Manufacturing Company | Industrial boiler utilizing multiple fuels and having reduced particulate emission and method of combustion |
| DE3026516A1 (en) * | 1980-07-12 | 1982-02-11 | Dieter 5060 Bergisch Gladbach Popp | HOT GAS GENERATOR |
| DE3444480A1 (en) * | 1984-12-06 | 1986-06-12 | Maschinenfabrik A. Lambion, 3548 Arolsen | Furnace for lumpy waste materials |
| FR2580057B1 (en) * | 1985-04-05 | 1990-01-05 | Mediterranee Const Navales Ind | |
| DE3625397A1 (en) * | 1986-07-26 | 1988-02-04 | Gutehoffnungshuette Man | Afterburner chamber behind a combustion furnace of a combustion installation for chemical waste |
| DE3787027T2 (en) * | 1986-10-11 | 1994-03-10 | Erithglen Ltd | OVEN. |
| US4724778A (en) * | 1986-12-15 | 1988-02-16 | Westinghouse Electric Corp. | Air control for combustor |
| DE3703855A1 (en) * | 1987-02-07 | 1988-08-18 | Gutehoffnungshuette Man | COMBUSTION PLANT FOR WASTE |
-
1988
- 1988-11-23 DE DE3839503A patent/DE3839503A1/en not_active Withdrawn
-
1989
- 1989-09-05 AT AT89116364T patent/ATE98357T1/en not_active IP Right Cessation
- 1989-09-05 EP EP89116364A patent/EP0370184B1/en not_active Expired - Lifetime
- 1989-09-05 DE DE89116364T patent/DE58906375D1/en not_active Expired - Fee Related
- 1989-09-29 CA CA000615143A patent/CA1337161C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| EP0370184A1 (en) | 1990-05-30 |
| DE3839503A1 (en) | 1990-05-31 |
| ATE98357T1 (en) | 1993-12-15 |
| DE58906375D1 (en) | 1994-01-20 |
| EP0370184B1 (en) | 1993-12-08 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKLA | Lapsed |