CA2050248C - Reformers, particularly autothermic secondary reformers - Google Patents
Reformers, particularly autothermic secondary reformersInfo
- Publication number
- CA2050248C CA2050248C CA 2050248 CA2050248A CA2050248C CA 2050248 C CA2050248 C CA 2050248C CA 2050248 CA2050248 CA 2050248 CA 2050248 A CA2050248 A CA 2050248A CA 2050248 C CA2050248 C CA 2050248C
- Authority
- CA
- Canada
- Prior art keywords
- feed
- reformer according
- reformer
- reaction chamber
- mixing
- 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
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/386—Catalytic partial combustion
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1005—Arrangement or shape of catalyst
- C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1276—Mixing of different feed components
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
A reformer, particularly an autothermic secondary reformer, is equipped with a central gas feed pipe penetrating the catalyst bed from the lower side and connected to a mixing and reaction chamber. A feeding device for the oxidizing agent is arranged at least at one level above the catalyst bed and penetrates reaction chamber wall from the external side, the device consisting of at least two inlet nozzles. The outlet end of centre feed pipe is located near the level of the feeding device for the oxidizing agent or above said level.
Description
20~0248 Reformers Particularlv autothermic secondarv reformers The invention relates to a reformer, particularly to an autothermic secondary reformer, equipped with a gas feed pipe arranged in the centre, penetrating the catalyst bed from the lower side and connected to a mixing and reaction chamber,and with a feeding device for the oxidizing agent.
Patent DE-C 37 35 193 describes such a reformer which has a common feed pipe forgas and oxidizing agent, said pipes being arranged in the centre, penetrating the catalyst bed from the lower side and communicating with the upper section ofthe reaction chamber. This unsophisticated design of a common inlet stream of process gas and oxidizing agent, however, may cause insufficient mixing and distribution of the two components required to optimize the reaction process in the catalyst bed. The reactor described in DE-A 15 42 539 is of the cross-flow type.
The aim of the invention is to design a device for an optimum distribution of the oxidizing agent and a thorough mixing with the process gas by means of a centre feed pipe penetrating the reactor from the lower end.
The invention provides for a reactor of the type mentioned above, with a feedingdevice arranged at one level above the catalyst bed, penetrating the reaction chamber wall from the external side and consisting of at least two inlet nozzles.
Said inlet nozzles are used as mixing and distributing components and permit andoptimum mixing of the reactants in the combustion chamber.
DE-A 28 41 127 describes a seondary reformer in which jet-type elements are deployed for mixing and distributing the oxidizing agent and the process gas.
The disadvantage of this design is that the process gas is not fed via a centre pipe through the catalyst bed into the mixing and reaction chamber, the inherentmerits of the centre pipe thus being abandoned. This applies also to the configuration recommended in DE-A 35 32 413.
Patent DE-C 37 35 193 describes such a reformer which has a common feed pipe forgas and oxidizing agent, said pipes being arranged in the centre, penetrating the catalyst bed from the lower side and communicating with the upper section ofthe reaction chamber. This unsophisticated design of a common inlet stream of process gas and oxidizing agent, however, may cause insufficient mixing and distribution of the two components required to optimize the reaction process in the catalyst bed. The reactor described in DE-A 15 42 539 is of the cross-flow type.
The aim of the invention is to design a device for an optimum distribution of the oxidizing agent and a thorough mixing with the process gas by means of a centre feed pipe penetrating the reactor from the lower end.
The invention provides for a reactor of the type mentioned above, with a feedingdevice arranged at one level above the catalyst bed, penetrating the reaction chamber wall from the external side and consisting of at least two inlet nozzles.
Said inlet nozzles are used as mixing and distributing components and permit andoptimum mixing of the reactants in the combustion chamber.
DE-A 28 41 127 describes a seondary reformer in which jet-type elements are deployed for mixing and distributing the oxidizing agent and the process gas.
The disadvantage of this design is that the process gas is not fed via a centre pipe through the catalyst bed into the mixing and reaction chamber, the inherentmerits of the centre pipe thus being abandoned. This applies also to the configuration recommended in DE-A 35 32 413.
- 2 - 2 0 ~ 0 2 ~ 8 According to a further embodiment, a specific advantage is obtained by arrangingthe gas outlet of the centre feed pipe for the process gas on the level of the oxidizing agent inlet or even higher in order to optimize gas mixing.
It is useful to place the gas feed pipe outlet and the feed nozzles in parallel and to arranged them vertically to the vertical centre axis of the mixing and reaction chamber.
The embodiment of the invention provides for inlet nozzles that are flush with the internal side of the internal liner. A circular feed line may be provided for the supply of the fluids to the inlet valves.
According to a further embodiment of the invention, a distributor is mounted to the outlet of the ce`ntre feed pipe and - as a specific feature - it is designedas swirl inducer. This construction improves and intensifies the swirl effect inthe mixing and reaction chamber, the gas leaving the chamber at a substantially lower temperature and forming a protective blanket around the distributor.
In this case, it is recommended that the vertical axis of the box-type gas distributor coincide with that of the mixing and reaction chamber and that the distributor be provided with external oblong holes flanked by vertical deflectors.
It is of particular advantage to place the deflectors symmetrically to the vertical axis of the mixing and reaction chamber, i.e. at an angle of <90 measured from the radius; it is also possible to arrange the axis of the inlet nozzles at an angle of <90 measured from the radius concerned, which serves to optimize the flow pattern. This special inlet configuration also permits a larger space for the flame by providing an adequate coning angle. The invention also provides for inlet nozzles that can be placed at a certain angle measured from the position of their free ends.
It is of course possible to provide a cooler for the inlet nozzles, said cooler having a closed or open jacket cooled by water, steam, etc.
It may also be useful to equip the inlet nozzles with a device for controlling the flame shape.
It is useful to place the gas feed pipe outlet and the feed nozzles in parallel and to arranged them vertically to the vertical centre axis of the mixing and reaction chamber.
The embodiment of the invention provides for inlet nozzles that are flush with the internal side of the internal liner. A circular feed line may be provided for the supply of the fluids to the inlet valves.
According to a further embodiment of the invention, a distributor is mounted to the outlet of the ce`ntre feed pipe and - as a specific feature - it is designedas swirl inducer. This construction improves and intensifies the swirl effect inthe mixing and reaction chamber, the gas leaving the chamber at a substantially lower temperature and forming a protective blanket around the distributor.
In this case, it is recommended that the vertical axis of the box-type gas distributor coincide with that of the mixing and reaction chamber and that the distributor be provided with external oblong holes flanked by vertical deflectors.
It is of particular advantage to place the deflectors symmetrically to the vertical axis of the mixing and reaction chamber, i.e. at an angle of <90 measured from the radius; it is also possible to arrange the axis of the inlet nozzles at an angle of <90 measured from the radius concerned, which serves to optimize the flow pattern. This special inlet configuration also permits a larger space for the flame by providing an adequate coning angle. The invention also provides for inlet nozzles that can be placed at a certain angle measured from the position of their free ends.
It is of course possible to provide a cooler for the inlet nozzles, said cooler having a closed or open jacket cooled by water, steam, etc.
It may also be useful to equip the inlet nozzles with a device for controlling the flame shape.
The drawings and diagrams listed below serve to illustrate the invention:
Fig. 1: cross-sect;onal view of the upper part of a secondary reformer according to the invention Fig. 2: cross-sectional view II-II of the device in Fig. 1.
The secondary reformer (1) shown in the figures has - inter alia - reaction chamber 2 and gas feed pipe 3 placed in the centre, said pipe penetrating catalyst bed 4 and communicating with mixing and reaction chamber 5.
The outlet of gas feed pipe 3 is equipped with gas distributor 6, inlet nozzles 7 for the oxidizing agent being arranged underneath the outlet end of feed pipe 3 and fed via circular feed line 3.
Fig. 2 shows feed nozzles 7 which are flush with the internal liner of reaction chamber wall 2 and arranged at angle a measured from the vessel radius 11 and, if required, at an angle b (Fig. 1). Gas distributor 6 has deflectors 10 which form an angle d measured from the vessel radius 11. Arrows 12 indicate the process gas stream and when the process gas and oxidizing agent are mixed, the flames are ignited and burn in the manner shown in Fig. 2 (flame shape 13).
The process takes place as follows:
The process gas stream leaving the central feed pipe 6 flow in a swirl-type manner due to deflectors 10. Said gas streams mix with the oxidizing agent fed by means of nozzles into the mixing and reaction chamber 5 so that the reaction gas is oxidized. The reaction product subsequently flows through the catalyst bed.
It is of course possible to modify the embodiment of the invention described above without abandoning the basic configuration. Thus, the invention is not limited to the type of gas distributor described above. The deflectors may be curved or bent and their thickness is variable. Nozzles may be installed in the head of gas feed pipe 3 instead of the circular inlet ducts formed by the deflectors.
B
Fig. 1: cross-sect;onal view of the upper part of a secondary reformer according to the invention Fig. 2: cross-sectional view II-II of the device in Fig. 1.
The secondary reformer (1) shown in the figures has - inter alia - reaction chamber 2 and gas feed pipe 3 placed in the centre, said pipe penetrating catalyst bed 4 and communicating with mixing and reaction chamber 5.
The outlet of gas feed pipe 3 is equipped with gas distributor 6, inlet nozzles 7 for the oxidizing agent being arranged underneath the outlet end of feed pipe 3 and fed via circular feed line 3.
Fig. 2 shows feed nozzles 7 which are flush with the internal liner of reaction chamber wall 2 and arranged at angle a measured from the vessel radius 11 and, if required, at an angle b (Fig. 1). Gas distributor 6 has deflectors 10 which form an angle d measured from the vessel radius 11. Arrows 12 indicate the process gas stream and when the process gas and oxidizing agent are mixed, the flames are ignited and burn in the manner shown in Fig. 2 (flame shape 13).
The process takes place as follows:
The process gas stream leaving the central feed pipe 6 flow in a swirl-type manner due to deflectors 10. Said gas streams mix with the oxidizing agent fed by means of nozzles into the mixing and reaction chamber 5 so that the reaction gas is oxidized. The reaction product subsequently flows through the catalyst bed.
It is of course possible to modify the embodiment of the invention described above without abandoning the basic configuration. Thus, the invention is not limited to the type of gas distributor described above. The deflectors may be curved or bent and their thickness is variable. Nozzles may be installed in the head of gas feed pipe 3 instead of the circular inlet ducts formed by the deflectors.
B
Claims (11)
1. A reformer, in particular an autothermal secondary reformer, comprising a gas feed which is passed centrally from below through the catalyst into a mixing or reaction chamber, and an oxidation agent feed, wherein in at least one plane above the catalyst bed are at least two feed nozzles for feeding the oxidation agent, which pass through the internal insulation from the outside inwardly, wherein the outlet end of the central gas feed is disposed in the plane of the oxidation agent feed or in a still higher plane above the plane of the oxidation agent feeds.
2. A reformer according to claim 1 wherein the feed nozzles are aligned with the inside of the insulation.
3. A reformer according to claim 1 or claim 2 wherein there is provided a supply conduit in ring form for supplying the feed nozzles.
4. A reformer according to claim 1 or claim 2 wherein the central gas feed is provided at its outlet end with a gas distributor.
5. A reformer according to claim 1 or claim 2 wherein the plane in which the outlet end of the gas feed is disposed and the plane in which the feed nozzles are arranged extend parallel to each other and perpendicularly to the vertical centre line of the mixing and reaction chamber.
6. A reformer according to claim 4 wherein the gas distributor is in the form of a swirl-producing element.
7. A reformer according to claim 4 wherein the gas distributor comprises a housing whose vertical centre line coincides with the vertical centre line of the mixing or reaction chamber and at its outside has slit-shaped openings which are defined by vertical guide walls.
8. A reformer according to claim 7 wherein the guide walls are arranged symmetrically relative to the vertical centre line of the mixing and reaction chamber and are set at an angle .delta. of less than 90° relative to the associated radius.
9. A reformer according to claim 1 wherein the feed nozzles are set at an angle .alpha. of between 25 and 45° relative to the associated radius.
10. A reformer according to one of claims 1, 2, or 9 wherein the feed nozzles are provided with a cooling device and with a device for influencing the flame shape.
11. A reformer according to claim 10 wherein the cooling device comprises a cooling agent flowing in a closed or open double casing.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19904027410 DE4027410A1 (en) | 1990-08-30 | 1990-08-30 | REFORMER, ESPECIALLY AUTOTHERMAL SECONDARY REFORMER |
| DEP4027410.1 | 1990-08-30 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2050248A1 CA2050248A1 (en) | 1992-03-01 |
| CA2050248C true CA2050248C (en) | 1997-03-18 |
Family
ID=6413212
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2050248 Expired - Lifetime CA2050248C (en) | 1990-08-30 | 1991-08-29 | Reformers, particularly autothermic secondary reformers |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0473870B1 (en) |
| CA (1) | CA2050248C (en) |
| DE (2) | DE4027410A1 (en) |
| DK (1) | DK0473870T3 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU7765200A (en) | 1999-10-05 | 2001-05-10 | Ballard Power Systems Inc. | Autothermal reformer |
| DE10359744A1 (en) | 2003-12-19 | 2005-07-14 | Uhde Gmbh | Method and device for injecting oxygen into a synthesis reactor |
| DE102004003070A1 (en) | 2004-01-21 | 2005-08-18 | Uhde Gmbh | Process and apparatus for injecting oxygen with radial catalyst flow |
| DE102008039014A1 (en) * | 2008-08-21 | 2010-02-25 | Uhde Gmbh | Multi-stage reactor cascade for soot-free production of systhesegas |
| WO2021079689A1 (en) * | 2019-10-21 | 2021-04-29 | 株式会社豊田自動織機 | Reforming device and reforming system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3340320A (en) * | 1964-06-08 | 1967-09-05 | Phillips Petroleum Co | Dehydrogenation reactor and process |
| DE1542539A1 (en) * | 1966-10-25 | 1970-09-24 | Uhde Gmbh Friedrich | Axially flowed reaction tower |
| DE2504343C2 (en) * | 1975-02-03 | 1982-07-08 | Linde Ag, 6200 Wiesbaden | Process and reactor for carrying out exothermic catalytic reactions |
| DE3532413A1 (en) * | 1985-09-11 | 1987-03-12 | Uhde Gmbh | DEVICE FOR GENERATING SYNTHESIS GAS |
| DE3735193A1 (en) * | 1987-10-17 | 1989-04-27 | Uhde Gmbh | REFORMER, ESPECIALLY AUTOTHERMAL SECONDARY REFORMER |
-
1990
- 1990-08-30 DE DE19904027410 patent/DE4027410A1/en not_active Ceased
-
1991
- 1991-03-28 DE DE91104977T patent/DE59100845D1/en not_active Expired - Lifetime
- 1991-03-28 EP EP19910104977 patent/EP0473870B1/en not_active Expired - Lifetime
- 1991-03-28 DK DK91104977T patent/DK0473870T3/en active
- 1991-08-29 CA CA 2050248 patent/CA2050248C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CA2050248A1 (en) | 1992-03-01 |
| EP0473870B1 (en) | 1994-01-12 |
| EP0473870A1 (en) | 1992-03-11 |
| DK0473870T3 (en) | 1994-05-30 |
| DE59100845D1 (en) | 1994-02-24 |
| DE4027410A1 (en) | 1992-03-05 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKEX | Expiry |