CA2019960C - Process for treating mineral mixtures - Google Patents
Process for treating mineral mixturesInfo
- Publication number
- CA2019960C CA2019960C CA002019960A CA2019960A CA2019960C CA 2019960 C CA2019960 C CA 2019960C CA 002019960 A CA002019960 A CA 002019960A CA 2019960 A CA2019960 A CA 2019960A CA 2019960 C CA2019960 C CA 2019960C
- Authority
- CA
- Canada
- Prior art keywords
- process according
- mixture
- free fall
- grain
- fluidized bed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C7/00—Separating solids from solids by electrostatic effect
- B03C7/006—Charging without electricity supply, e.g. by tribo-electricity or pyroelectricity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C7/00—Separating solids from solids by electrostatic effect
- B03C7/003—Pretreatment of the solids prior to electrostatic separation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C7/00—Separating solids from solids by electrostatic effect
- B03C7/02—Separators
- B03C7/12—Separators with material falling free
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Extraction Or Liquid Replacement (AREA)
- Electrostatic Separation (AREA)
- Medicines Containing Material From Animals Or Micro-Organisms (AREA)
- Combined Means For Separation Of Solids (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
A mineral mixture is divided up into various grain size fractions and each fraction is individually separated by electrostatic means in free fall separators.
Description
~ -2- 2019960 It is a known fact that mixtures of minerals, such as raw potassium salts, can be electrostatically separated into their individual components. Thisis done by grinding up the mineral mixture, mixing it with chemical conditionersand charging it triboelectrically in ambient air of predetermined relative humidity 5 and temperature, before finally feeding it to a free fall separator having an electrostatic field in which the particles of the mineral mixture are deflected,according to their charge, from the vertical direction of fall towards the oppositely charged electrode. Such processes are adequately well known and in the case of potassium raw salts they have been described in detail, along 10 with the associated equipment, by Singewald et al. in "Chem.lng.Techn." 55 (1983), pages 39-45.
When the mineral mixtures are ground, they do not break up into particles of uniform size, but instead the ground material possesses a spectrum of grain sizes. The difference in grain size of the individual particles in the 15 mixture makes it very difficult to separate such mixtures electrostatically on an industrial scale and in particular has a very negative effect on the separating result.
Therefore, ways were sought by means of which these disadvantages could be eliminated and mixtures with a broad grain size spectrum could be 20 separated with good results in electrostatic free fall separators.
According to the present invention, a process is provided for treating mineral mixtures, especially salt mixtures, in the electrostatic field of a free fall separator, after grinding, chemical conditioning and triboelectric charging in air having a predetermined relative humidity and temperature. The mineral mixture 25 first undergoes selective coarse grinding and is then divided up into fractions of defined grain size, and each of these fractions is separated in turn into individual fractions in free fall separators of specific vertical field height.
The mineral mixture, which is first ground to grain sizes of preferentially < 5 mm, is separated by classification and/or screening into fractions having 30 a predetermined narrow grain size spectrum. Classifiers and screening devicesC
of a known type can be used for this purpose. The screening is normally carried out before conditioning with the organic reagent. However, it was found that the screening can also be advantageously carried out after the conditioning, thus saving the separate conditioning steps.
The invention will now be described taking the processing of raw potassium salt by way of example.
The raw potassium salt is first ground to a grain size of < 5 mm. The grain size fraction having grain sizes of <0.15 mm is then removed from this mineral mixture, advantageously in a fluidized bed, by injecting the lowest possible volume of air, and it then separately undergoes further processing.
At the same time, the necessary conditioners can be added to the mineral mixture while it is in the fluidized bed. In addition, the air which is passed through the fluidized bed can be adjusted to a predetermined relative humidity and temperature, which favours the triboelectric charging of the particles in the mixture.
This makes it possible for the <0.15 mm grain fraction of the mineral mixture, which is suspended in the air leaving the fluidized bed, to be fed directly to an electrostatic free fall separator to be separated. It has proved advantageous, in this connection, if in addition a vertical air flow is maintained from the inlet end to the bottom end of the free fall shaft in this free fall separator. The fall trajectory of the grain size fraction through the horizontally oriented electrostatic field of the free fall separator should be at least 1 m.
According to the example used to describe the invention, a further grain fraction having grain sizes of 2 to 5 mm is separated from the ground-up raw potassium salt. This separation is advantageously accomplished after the chemical conditioning of the raw potassium salt and before it is triboelectrically charged.
C
The grain fraction of 2 to 5 mm which is separated from the mineral mixture, such as raw potassium salt, is chemically conditioned and triboelectricaily charged, then fed to a free fall separator in which a horizontally oriented electrostatic field is maintained. The vertically measured height of this field is 5 at least 4 m, i.e. the fall trajectory of the grain fraction through this electrostatic field must be at least 4 m.
The grain fraction of 0.15 to 2 mm is left over from the mineral mixture, such as the raw potassium salt. After chemical conditioning and triboelectric charging, this grain fraction is fed to a free fall separator to be separated into 10 its individual components. In the free fall separator, the vertical height of the horizontally oriented electrostatic field is 1.5 to 2.0 m.
Excellent separating results and very good product yields are obtained by using the process according to the invention. Up until now, the very widely differing grain sizes of 0 to 5 mm in the mineral mixture to be separated have clearly 15 had a negative effect on the electrostatic deflection of the particles in the free fall separator.
This disadvantage of the previously known processes is eliminated by the method according to the invention, wherein the mineral mixture to be separated is divided up into fractions having a narrow grain size range and 20 these fractions separately undergo electrostatic separation.
The process is described in more detail in the following examples, with reference to the accompanying diagrammatic representations, wherein:
Figures 1 and 2 are diagrammatic representations of a prior art method and of a method of the invention, respectively, based on the processing of a relatively25 finely intergrown sylvinite fully ground to a size of 1.25 mm.
Figures 3 and 4 are diagrammatic representations of a prior art method and of a method of the invention, respectively, based on the processing of a coarsely and spathically intergrown sylvinite which is ground to a size of 4 mm.
C
As mentioned above, Examples 1 and 2 are based on the processing of a relatively finely intergrown sylvinite which is fully ground to a size of 1.25mm. It is conditioned with 50 g/t salicylic acid and 50 g/t fatty acid. However,the conditioning by the salicylic acid can also be carried out via the vapour 5 phase according to German Patent 26 19 026. The salt is separated in normal long separators (field length of 1.7 m) at 4-5 kV/cm 100 - 125 kV at an electrode spacing of 25 cm. The middlings are recycled to the process after the grinding step. Electrostatic separation yields the following results:
- Examcle 1, which is based on the state of the art, yields a concentrate having 50.2% K20 and a residue having 4.3% K20.
The K20 yield is 92.2%.
- Exam~le 2, which is based on the process according to the invention, separates the fines in a fines separator as described in the simultaneously claimed invention entitled "A Process and Device for the Electrostatic Processing of Mineral Mixtures, especially Raw Potassium Salts" (German Patent ... ). The 0.5 to 0.1 mm fractions and the 1.25 to 0.5 fractions are processed in different separators. Altogether, a concentrate having 52.2% K20 and a residue containing 3.4% K20 is obtained.
The K20 yield is 93.7%.
The progress achieved by the process is obvious. (Figures 1 and 2 illustrate the examples in detail).
Examples 3 and 4 are based on the processing of a coarsely and spathically intergrown sylvinite which is ground to a size of 4 mm. The salt is 25 conditioned and ground, as described in Examples 1 and 2. The following results are obtained:
C
When the mineral mixtures are ground, they do not break up into particles of uniform size, but instead the ground material possesses a spectrum of grain sizes. The difference in grain size of the individual particles in the 15 mixture makes it very difficult to separate such mixtures electrostatically on an industrial scale and in particular has a very negative effect on the separating result.
Therefore, ways were sought by means of which these disadvantages could be eliminated and mixtures with a broad grain size spectrum could be 20 separated with good results in electrostatic free fall separators.
According to the present invention, a process is provided for treating mineral mixtures, especially salt mixtures, in the electrostatic field of a free fall separator, after grinding, chemical conditioning and triboelectric charging in air having a predetermined relative humidity and temperature. The mineral mixture 25 first undergoes selective coarse grinding and is then divided up into fractions of defined grain size, and each of these fractions is separated in turn into individual fractions in free fall separators of specific vertical field height.
The mineral mixture, which is first ground to grain sizes of preferentially < 5 mm, is separated by classification and/or screening into fractions having 30 a predetermined narrow grain size spectrum. Classifiers and screening devicesC
of a known type can be used for this purpose. The screening is normally carried out before conditioning with the organic reagent. However, it was found that the screening can also be advantageously carried out after the conditioning, thus saving the separate conditioning steps.
The invention will now be described taking the processing of raw potassium salt by way of example.
The raw potassium salt is first ground to a grain size of < 5 mm. The grain size fraction having grain sizes of <0.15 mm is then removed from this mineral mixture, advantageously in a fluidized bed, by injecting the lowest possible volume of air, and it then separately undergoes further processing.
At the same time, the necessary conditioners can be added to the mineral mixture while it is in the fluidized bed. In addition, the air which is passed through the fluidized bed can be adjusted to a predetermined relative humidity and temperature, which favours the triboelectric charging of the particles in the mixture.
This makes it possible for the <0.15 mm grain fraction of the mineral mixture, which is suspended in the air leaving the fluidized bed, to be fed directly to an electrostatic free fall separator to be separated. It has proved advantageous, in this connection, if in addition a vertical air flow is maintained from the inlet end to the bottom end of the free fall shaft in this free fall separator. The fall trajectory of the grain size fraction through the horizontally oriented electrostatic field of the free fall separator should be at least 1 m.
According to the example used to describe the invention, a further grain fraction having grain sizes of 2 to 5 mm is separated from the ground-up raw potassium salt. This separation is advantageously accomplished after the chemical conditioning of the raw potassium salt and before it is triboelectrically charged.
C
The grain fraction of 2 to 5 mm which is separated from the mineral mixture, such as raw potassium salt, is chemically conditioned and triboelectricaily charged, then fed to a free fall separator in which a horizontally oriented electrostatic field is maintained. The vertically measured height of this field is 5 at least 4 m, i.e. the fall trajectory of the grain fraction through this electrostatic field must be at least 4 m.
The grain fraction of 0.15 to 2 mm is left over from the mineral mixture, such as the raw potassium salt. After chemical conditioning and triboelectric charging, this grain fraction is fed to a free fall separator to be separated into 10 its individual components. In the free fall separator, the vertical height of the horizontally oriented electrostatic field is 1.5 to 2.0 m.
Excellent separating results and very good product yields are obtained by using the process according to the invention. Up until now, the very widely differing grain sizes of 0 to 5 mm in the mineral mixture to be separated have clearly 15 had a negative effect on the electrostatic deflection of the particles in the free fall separator.
This disadvantage of the previously known processes is eliminated by the method according to the invention, wherein the mineral mixture to be separated is divided up into fractions having a narrow grain size range and 20 these fractions separately undergo electrostatic separation.
The process is described in more detail in the following examples, with reference to the accompanying diagrammatic representations, wherein:
Figures 1 and 2 are diagrammatic representations of a prior art method and of a method of the invention, respectively, based on the processing of a relatively25 finely intergrown sylvinite fully ground to a size of 1.25 mm.
Figures 3 and 4 are diagrammatic representations of a prior art method and of a method of the invention, respectively, based on the processing of a coarsely and spathically intergrown sylvinite which is ground to a size of 4 mm.
C
As mentioned above, Examples 1 and 2 are based on the processing of a relatively finely intergrown sylvinite which is fully ground to a size of 1.25mm. It is conditioned with 50 g/t salicylic acid and 50 g/t fatty acid. However,the conditioning by the salicylic acid can also be carried out via the vapour 5 phase according to German Patent 26 19 026. The salt is separated in normal long separators (field length of 1.7 m) at 4-5 kV/cm 100 - 125 kV at an electrode spacing of 25 cm. The middlings are recycled to the process after the grinding step. Electrostatic separation yields the following results:
- Examcle 1, which is based on the state of the art, yields a concentrate having 50.2% K20 and a residue having 4.3% K20.
The K20 yield is 92.2%.
- Exam~le 2, which is based on the process according to the invention, separates the fines in a fines separator as described in the simultaneously claimed invention entitled "A Process and Device for the Electrostatic Processing of Mineral Mixtures, especially Raw Potassium Salts" (German Patent ... ). The 0.5 to 0.1 mm fractions and the 1.25 to 0.5 fractions are processed in different separators. Altogether, a concentrate having 52.2% K20 and a residue containing 3.4% K20 is obtained.
The K20 yield is 93.7%.
The progress achieved by the process is obvious. (Figures 1 and 2 illustrate the examples in detail).
Examples 3 and 4 are based on the processing of a coarsely and spathically intergrown sylvinite which is ground to a size of 4 mm. The salt is 25 conditioned and ground, as described in Examples 1 and 2. The following results are obtained:
C
2~19960 - ExamPle 3, which is based on the state of the art, yields a concentrate having 44.1% K20 and a residue containing 4.2% K20.
The K20 yield is 89.8%.
The concentrate and also the residue contain only small proportions in the > 2 mm range. The coarse grains are thus practically all found in the middlings and are reground in that fraction.
The separation was carried out in a separator of normal length and having a field length of 1.7 m.
- ExamPle 4, which is based on the process according to the invention, separates the ground salt into four fractions. In principle, any desired separation is possible.
The fine material having a size of <0.1 mm, which is blown out of the mixture in the salt heating stage, is split into fractions in a fines separator in the manner described in the simultaneously claimed invention entitled "A
Process and Device for the Electrostatic Processing of Mineral Mixtures especially Raw Potassium Salts (German Patent .. ). The 1.25 mm to 0.1 mm fraction is fed to a separator of normal length (1.7 m), and the 2 to 1.25 mm fraction is fed to an extra long separator 3 m long, while the > 2 mm fraction is fed to an even longer separator having a field length of 4 m. The 20 following concentrates are obtained:
a) A 2 - 4 mm concentrate containing 47.3% K20. The coarse concentrate yield, relative to the amount of K20 entrained in the coarse feedstock, is 90.5%.
b) A 2 - 1.25 mm concentrate containing 49.6% K20. The K20 yield, again relative to the amount of K20 brought in with this fraction, is 90.9%.
C
-c) A 1.25 - 0.1 mm concentrate containing 52.4% K20 with a K20 yield of 92.8%, again relative to the amount brought in with this fraction.
d) A <0.1 mm fines concentrate containing 40.8% K20 with a K20 yield of 89.8%.
5 Overall, a total concentrate containing 49.7% K20 with a K20 yield of 91.8%
is obtained.
The technical progress achieved by the process according to the invention is clearly apparent from the examples.
Composition and Screen Analysis of the Raw Salt Examples 1 and 2 Examples 3 and 4 Mineral Analysis 27.4% K20 22.5% K20 43.4% Sylvite 35.6% Sylvite 55.4% Rock Salt 63.1 % Rock Salt 1.2% Miscellaneous 1.3% Miscellaneous Screen Analysis > 0.8 mm = 10.9 % > 2.0 mm = 22.
0.8-0.5 mm = 15.7% 2.0-1.25 mm = 23.
0.5-0.25 mm = 29.6% 25-0.1 mm = 43.
0.25-0.1 mm = 31.6% ~0.1 mm = 10.
<0.1 mm = 12.2%
C
The K20 yield is 89.8%.
The concentrate and also the residue contain only small proportions in the > 2 mm range. The coarse grains are thus practically all found in the middlings and are reground in that fraction.
The separation was carried out in a separator of normal length and having a field length of 1.7 m.
- ExamPle 4, which is based on the process according to the invention, separates the ground salt into four fractions. In principle, any desired separation is possible.
The fine material having a size of <0.1 mm, which is blown out of the mixture in the salt heating stage, is split into fractions in a fines separator in the manner described in the simultaneously claimed invention entitled "A
Process and Device for the Electrostatic Processing of Mineral Mixtures especially Raw Potassium Salts (German Patent .. ). The 1.25 mm to 0.1 mm fraction is fed to a separator of normal length (1.7 m), and the 2 to 1.25 mm fraction is fed to an extra long separator 3 m long, while the > 2 mm fraction is fed to an even longer separator having a field length of 4 m. The 20 following concentrates are obtained:
a) A 2 - 4 mm concentrate containing 47.3% K20. The coarse concentrate yield, relative to the amount of K20 entrained in the coarse feedstock, is 90.5%.
b) A 2 - 1.25 mm concentrate containing 49.6% K20. The K20 yield, again relative to the amount of K20 brought in with this fraction, is 90.9%.
C
-c) A 1.25 - 0.1 mm concentrate containing 52.4% K20 with a K20 yield of 92.8%, again relative to the amount brought in with this fraction.
d) A <0.1 mm fines concentrate containing 40.8% K20 with a K20 yield of 89.8%.
5 Overall, a total concentrate containing 49.7% K20 with a K20 yield of 91.8%
is obtained.
The technical progress achieved by the process according to the invention is clearly apparent from the examples.
Composition and Screen Analysis of the Raw Salt Examples 1 and 2 Examples 3 and 4 Mineral Analysis 27.4% K20 22.5% K20 43.4% Sylvite 35.6% Sylvite 55.4% Rock Salt 63.1 % Rock Salt 1.2% Miscellaneous 1.3% Miscellaneous Screen Analysis > 0.8 mm = 10.9 % > 2.0 mm = 22.
0.8-0.5 mm = 15.7% 2.0-1.25 mm = 23.
0.5-0.25 mm = 29.6% 25-0.1 mm = 43.
0.25-0.1 mm = 31.6% ~0.1 mm = 10.
<0.1 mm = 12.2%
C
Claims (11)
1. A process for treating a mineral mixture, especially salt mixture, in the electrostatic field of a free fall separator, said method comprising the steps of:
- grinding the mixture by a selective coarse grinding;
- dividing the ground mixture into primary fractions of defined grain size;
- chemical conditioning the ground mixture - triboelectric charging of the ground mixture in air having a predetermined relative humidity and temperature; and - separating said primary fractions into a number of secondary fractions using electrostatic free fall separators of a specific vertical field.
- grinding the mixture by a selective coarse grinding;
- dividing the ground mixture into primary fractions of defined grain size;
- chemical conditioning the ground mixture - triboelectric charging of the ground mixture in air having a predetermined relative humidity and temperature; and - separating said primary fractions into a number of secondary fractions using electrostatic free fall separators of a specific vertical field.
2. A process according to Claim 1, wherein the selective coarse grinding is carried out to a grain size of <5 mm.
3. A process according to Claim 1, wherein a <0.15 mm grain fraction is removed by a very low-volume air flow injected into a fluidized bed and then separately processed.
4. A process according to one of Claims 1 or 2, wherein the chemical conditioning of the ground mixture is carried out in a fluidized bed.
5. A process according to Claim 3, wherein the chemical conditioning of the ground mixture is carried out in a fluidized bed.
6. A process according to one of Claims 1 or 2, wherein a <0 15 mm grain fraction is suspended in air exiting from a fluidized bed and is fed toan electrostatic free fall separator including a free fall shaft in which a vertical air flow is maintained from an inlet to a bottom end of the shaft.
7. A process according to Claim 3, wherein a <0 15 mm grain fraction suspended in the air exiting from the fluidized bed is fed to an electrostatic free fall separator including a free fall shaft in which a vertical air flow is maintained from an inlet to a bottom end of the shaft.
8. A process according to one of Claims 1, 2 or 3, wherein a 2 to 5 mm grain fraction separated from the ground mineral mixture is chemically conditioned and triboelectrically charged and then fed to a free fall separator having a field height of at least 4 m.
9. A process according to one of Claims 1, 2 or 3, wherein a 0.15 mm to 2 mm grain fraction separated from the ground mineral mixture is conditioned and triboelectrically charged and then fed to a free fall separator having a vertical field height of 1.5 to 2 m.
10. A process according to Claim 4, wherein, after emerging from the fluidized bed, and after the extremely fine grain sizes have been removed, the mineral mixture is screened and then the grain fractions are separately electrostatically processed.
11. A process according to Claim 5, wherein, after emerging from the fluidized bed, and after the extremely fine grain sizes have been removed, the mineral mixture is screened and then the grain fractions are separately electrostatically processed.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3921073.1 | 1989-06-28 | ||
| DE3921073A DE3921073A1 (en) | 1989-06-28 | 1989-06-28 | Electrostatically working up mineral ore - by sepg. into grain size fractions and subjecting each fraction to separate free-fall electrostatic field |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2019960A1 CA2019960A1 (en) | 1990-12-28 |
| CA2019960C true CA2019960C (en) | 1996-09-10 |
Family
ID=6383707
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002019960A Expired - Lifetime CA2019960C (en) | 1989-06-28 | 1990-06-27 | Process for treating mineral mixtures |
Country Status (4)
| Country | Link |
|---|---|
| CA (1) | CA2019960C (en) |
| DD (1) | DD300082A5 (en) |
| DE (1) | DE3921073A1 (en) |
| IT (1) | IT1247700B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102017218206A1 (en) | 2017-10-12 | 2019-04-18 | K+S Aktiengesellschaft | Process for the triboelectric charging of chemically conditioned salt mixtures |
| DE102024101862A1 (en) | 2024-01-23 | 2025-07-24 | K+S Aktiengesellschaft | Fertilizer granules containing sodium sulfate and potassium chloride |
-
1989
- 1989-06-28 DE DE3921073A patent/DE3921073A1/en active Granted
-
1990
- 1990-06-27 IT IT04809890A patent/IT1247700B/en active IP Right Grant
- 1990-06-27 DD DD342167A patent/DD300082A5/en unknown
- 1990-06-27 CA CA002019960A patent/CA2019960C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| DE3921073A1 (en) | 1991-01-10 |
| DE3921073C2 (en) | 1991-08-08 |
| IT1247700B (en) | 1994-12-30 |
| IT9048098A1 (en) | 1991-12-27 |
| DD300082A5 (en) | 1992-05-21 |
| IT9048098A0 (en) | 1990-06-27 |
| CA2019960A1 (en) | 1990-12-28 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKEX | Expiry |