CA2276221A1 - Device for performing catalytic chemical reactions of a fluid in the gas phase - Google Patents
Device for performing catalytic chemical reactions of a fluid in the gas phase Download PDFInfo
- Publication number
- CA2276221A1 CA2276221A1 CA002276221A CA2276221A CA2276221A1 CA 2276221 A1 CA2276221 A1 CA 2276221A1 CA 002276221 A CA002276221 A CA 002276221A CA 2276221 A CA2276221 A CA 2276221A CA 2276221 A1 CA2276221 A1 CA 2276221A1
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- Prior art keywords
- catalyst bed
- catalyst
- bed
- flow
- housing
- Prior art date
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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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
-
- 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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0403—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 the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0407—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 the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0411—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 the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being concentric
-
- 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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0465—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
With a device for performing catalytic chemical reactions of a fluid in the gas phase, besides avoiding the known disadvantages, a device with two catalyst beds of different life spans are supposed to be designed in such a way that the catalysts can be changed independent of one another, without taking into account unutilised dead spaces and with the possibility of being able to circumvent each bed.
This is achieved, in that a) the first catalyst bed (6) in the flow path has a lesser catalyst volume than the second catalyst bed (7);
b) the first and second catalyst bed (6, 7) are designed largely cylindrical, whereby the cylindrical boundary wall (12) of the inner catalyst bed (6) forms the cylindrical inner wall of the second catalyst bed (7); and c) the first catalyst bed (6) can have a flow-through radially and the second catalyst bed (7) axially.
This is achieved, in that a) the first catalyst bed (6) in the flow path has a lesser catalyst volume than the second catalyst bed (7);
b) the first and second catalyst bed (6, 7) are designed largely cylindrical, whereby the cylindrical boundary wall (12) of the inner catalyst bed (6) forms the cylindrical inner wall of the second catalyst bed (7); and c) the first catalyst bed (6) can have a flow-through radially and the second catalyst bed (7) axially.
Description
250 A/14792 d/s "Device for Performing Catalytic Chemical Reactions of a Fluid in the Gas Phase"
The invention pertains to device of the genre mentioned in the introductory part of claim 1.
There are a series of catalytic chemical reactions of a fluid, e.g. the desulphurization of hydrocarbons - here as example desulphurization of natural gas is mentioned -in which two catalysts are connected one after the other in the flow direction of the fluid, whereby in many cases the first catalyst in flow direction has a shorter life span than the second. Thus, for example, the organic sulphur compounds present in the first stage are converted in to HZS by adding hydrogen. In a second stage, the HZS is absorbed in a zinc bed, whereby the catalyst volume of the first stage is significantly lesser than in the second stage. It is thereby known, how to accommodate both catalysts within a common reactor pressure vessel, whereby already due to the different using times, generally a first manhole provided in the dome of the reactor is meant for replacing the first catalyst and a second manhole in the sideways outer jacket opens up a space from which the second catalyst can be removed for changing. 1'he disadvantage in this design is that this second space between both the catalyst beds cannot be utilized.
For the state-of the-art-technology, please refer to the documents EP-0 400 698-A1 or US-3 544 264, US-3 817 716, US-3 620 685 or US-4 830 834. The device mentioned in the above European application is a converter which is supposed to be used for handling dust=laden gases. In the preferred design, two catalyst beds are used.
In the document US-4 830 843 it has to do with a heat exchanger reformer which is equipped with a burner for heat balance compensation for the conversion of natural gas steam into Hz-and COZ-containing gas mixture; this burner supplies a hot flue gas which in indirect heat exchange gives off the heat on to the process gas.
The reactor described in US-3 620 685 is meant for an oxide-hydro process.
This, on the one hand, requires large flow areas of the catalyst layers and, on the other hand, high exhaust gas flow velocities after completion of the catalytic treatment.
The invention pertains to device of the genre mentioned in the introductory part of claim 1.
There are a series of catalytic chemical reactions of a fluid, e.g. the desulphurization of hydrocarbons - here as example desulphurization of natural gas is mentioned -in which two catalysts are connected one after the other in the flow direction of the fluid, whereby in many cases the first catalyst in flow direction has a shorter life span than the second. Thus, for example, the organic sulphur compounds present in the first stage are converted in to HZS by adding hydrogen. In a second stage, the HZS is absorbed in a zinc bed, whereby the catalyst volume of the first stage is significantly lesser than in the second stage. It is thereby known, how to accommodate both catalysts within a common reactor pressure vessel, whereby already due to the different using times, generally a first manhole provided in the dome of the reactor is meant for replacing the first catalyst and a second manhole in the sideways outer jacket opens up a space from which the second catalyst can be removed for changing. 1'he disadvantage in this design is that this second space between both the catalyst beds cannot be utilized.
For the state-of the-art-technology, please refer to the documents EP-0 400 698-A1 or US-3 544 264, US-3 817 716, US-3 620 685 or US-4 830 834. The device mentioned in the above European application is a converter which is supposed to be used for handling dust=laden gases. In the preferred design, two catalyst beds are used.
In the document US-4 830 843 it has to do with a heat exchanger reformer which is equipped with a burner for heat balance compensation for the conversion of natural gas steam into Hz-and COZ-containing gas mixture; this burner supplies a hot flue gas which in indirect heat exchange gives off the heat on to the process gas.
The reactor described in US-3 620 685 is meant for an oxide-hydro process.
This, on the one hand, requires large flow areas of the catalyst layers and, on the other hand, high exhaust gas flow velocities after completion of the catalytic treatment.
The document US-3 817 716 describes the treatment of exhaust gases which contain higher hydrocarbons and aerosoles, whereby ultimately US-3 544 264 shows an exhaust gas catalyst system for motor vehicles for reducing harmfial substances like NO~ and CO
It is the task of the invention, apart from avoiding the above described disadvantages, to design a device with two catalyst beds of different life spans in such a way, that the catalysts can be changed independent of one another, without taking into account non-utilised dead spaces and with the possibility of circumventing each bed.
This task is fulfilled with the help of a device of the type described above as per the invention, in that the first catalyst bed in the flow path has a smaller catalyst volume than the second catalyst bed, the first and second catalyst beds are mainly designed in cylindrical form, whereby the cylindrical boundary wall of the inner catalyst bed forms the inner wall of the second catalyst bed, and the first catalyst bed can have a flow passing through radially and the second catalyst bed axially.
Due to the fact that the first catalyst bed is surrounded by the second catalyst bed, it is possible to functionally change both catalysts through the same manhole in the dome of a reactor vessel, independent of one another Further advantages of the invention are given in the subclaims, whereby the design propagated here additionally makes it possible to shape the first catalyst bed radially and the second catalyst bed axially flowing, whereby it is obviously also possible to design both catalyst beds for flow axially or radially.
It is advantageous if the measurements of the receivers for the smaller first catalyst bed and the larger second catalyst bed are tuned to one another in such a way, that the filling heights of both catalyst beds are largely identical in the total housing of the catalysts, as foreseen by the invention.
In the dome of the total catalyst housing, a feed stud to the inner first catalyst bed provided in the dome can be foreseen and/or a second feed stud for circumventing the first catalyst.
If the inner catalyst bed has a flow from outwards to inwards and if the feed lies in an upper dome above the first catalyst bed, as already described above, then generally the fluid flowing through the first catalyst bed is led away through a centric collecting pipe which leads into the upper dome, in order to thus act upon the catalyst bed from above. In such a design it can also be foreseen that the centric inner exhaust flow pipe is led out of the total housing, so that also the first catalyst bed can be further operated, if for example, the second catalyst bed is supposed to be circumvented. The invention is described in detail below on the basis of the drawing. The following are shown:
Fig. l A suitable reactor according to the state-of the-art technology; and Fig.2 A device as per the invention.
The reactor generally denoted by 1 according to the state-of the-art technology consists of a pressure vessel 2 with an inlet stud 3 in the upper dome and an outlet stud 4 in the lower dome, as well as a manhole 5 between an upper catalyst bed 6 and a lower catalyst bed 7. The upper catalyst bed could for example represent the Co-Mo-catalyst for converting organic sulphur compounds into HZS and the lower catalyst bed could be the Zn0-catalyst for absorbing the sulphur from HZS. The upper catalyst bed rests on a carrier grate 8, below this carrier grate 8 there is a catalyst-free space 9 into which the stud of the manhole S leads in, whereby the upper catalyst can be changed through the feed stud 3 and the lower catalyst can be changed through the manhole 5.
In fig. 1 general height data of the catalyst beds of the dead space 9, as well as further measurements are given, whose equivalent are also given in fig. 2; the relevant dimensions are reproduced as an example in a table further below.
As far as possible, in fig. 2, where device as per the invention is depicted, the same reference numbers are chosen as in the case of the description of the state-of the-art technology as mentioned in fig. I.
There the reactor 1 consists of a pressure vessel 2 with an inlet stud 3 and an outlet stud 4 for the fluid to be treated. In the dome of the pressure vessel 2 a manhole 5 is centrically situated, whereby in the inner part of the housing 2 a second cylindrical housing 12 is arranged, which contains centrically a perforated cylinder 9 or an exhaust flow pipe 9 and around it centrically further outwards a perforated pipe 10, whereby the space between the perforated pipes 9 and forms the first catalyst bed 6. The outer wall 12 of the first catalyst vessel forms the inner wall for the second catalyst 7, whereby in the example shown, the first catalyst bed is arranged for flow radially and the second catalyst bed for flow axially, without the invention being restricted only to this.
The dome 13 of the housing of the first catalyst bed 6 is penetrated by the perforated central pipe 9 with a stud 15, whereby the first catalyst housing 12 is closed at the bottom end with a base plate 14 which goes over into the carrying grate for the second catalyst deposit denoted by 20.
The functioning method of the device as per the invention with respect to the flow path of the fluid to be treated is as follows The gas to be treated is fed to the stud 3 and reaches through a pipeline 16 into a first distributor or dome space 17 and subsequently into a feeding gap 1 I in order to then flow through the first catalyst via the perforated wall 10 or the first catalyst bed 6 radially, i.e. here from outside to inside. Through the perforated central pipe 9 via the exhaust stud 15 the gas goes into the second distributor or dome space 18 above the second catalyst deposit 7 in order to penetrate it from there and flow through axially and reach through the carrier grate ring 20 to the exhaust stud 4 which is arranged in the lower floor region 19 of the reactor vessel 2.
In fig. 2, a second feed stud 3' is shown directly in the second distributor space 18. Here the gas can be guided-in in such a way that it only flows to the second catalyst bed in order to simply circumvent the first catalyst deposit 6.
Not shown further is the possibility of guiding the exhaust stud 1 S into the second dome space I 8 outwards as and when required, in order to then be able to continue using the first catalyst, if for example, the second catalyst deposit is supposed to be circumvented.
~
~ CA 02276221 1999-06-25 _ - 5 The possibility of circumventing the first catalyst bed via the second gas inlet stud 3', can be of significant advantage for operators of such devices, if the gas to be treated is relatively clean for some time, e.g. no longer contains any organic sulphur compounds and hence the first catalyst bed need not be flowed through. or in case of using same catalysts for both beds, the first catalyst bed generates high pressure loss or even gets blocked due to impurities or disturbances.
The costs of such device are also greatly reduced, which alone makes a comparison between a reactor as per the state-of the-art technology, i.e. as shown in fig. l, and a reactor as per the invention, i.e. as shown in fig. 2 clear, whereby the dimensions shown in the figures are given in tabular form. The saving in weight which can be seen in the last line of the table is 29,000 Kg, it can be recognised extremely significantly, whereby not only material costs but also transportation and assembly costs can be saved:
Table (Please see original) Gewicht = weight Figur 1 Figur 2 Volumen 6 [m3] 13,6 13,6 Volumen 7 [m3J 66,5 66,5 ho [~,J 11.000 5.500 h [~] ho 7.500 hl [mm] 7.800 __ hz [~nJ 1.600 --h3 [nun] 1.600 --[mmJ 3.300 3.850 __ 1.700 Gewicht kg 109.000 80.000
It is the task of the invention, apart from avoiding the above described disadvantages, to design a device with two catalyst beds of different life spans in such a way, that the catalysts can be changed independent of one another, without taking into account non-utilised dead spaces and with the possibility of circumventing each bed.
This task is fulfilled with the help of a device of the type described above as per the invention, in that the first catalyst bed in the flow path has a smaller catalyst volume than the second catalyst bed, the first and second catalyst beds are mainly designed in cylindrical form, whereby the cylindrical boundary wall of the inner catalyst bed forms the inner wall of the second catalyst bed, and the first catalyst bed can have a flow passing through radially and the second catalyst bed axially.
Due to the fact that the first catalyst bed is surrounded by the second catalyst bed, it is possible to functionally change both catalysts through the same manhole in the dome of a reactor vessel, independent of one another Further advantages of the invention are given in the subclaims, whereby the design propagated here additionally makes it possible to shape the first catalyst bed radially and the second catalyst bed axially flowing, whereby it is obviously also possible to design both catalyst beds for flow axially or radially.
It is advantageous if the measurements of the receivers for the smaller first catalyst bed and the larger second catalyst bed are tuned to one another in such a way, that the filling heights of both catalyst beds are largely identical in the total housing of the catalysts, as foreseen by the invention.
In the dome of the total catalyst housing, a feed stud to the inner first catalyst bed provided in the dome can be foreseen and/or a second feed stud for circumventing the first catalyst.
If the inner catalyst bed has a flow from outwards to inwards and if the feed lies in an upper dome above the first catalyst bed, as already described above, then generally the fluid flowing through the first catalyst bed is led away through a centric collecting pipe which leads into the upper dome, in order to thus act upon the catalyst bed from above. In such a design it can also be foreseen that the centric inner exhaust flow pipe is led out of the total housing, so that also the first catalyst bed can be further operated, if for example, the second catalyst bed is supposed to be circumvented. The invention is described in detail below on the basis of the drawing. The following are shown:
Fig. l A suitable reactor according to the state-of the-art technology; and Fig.2 A device as per the invention.
The reactor generally denoted by 1 according to the state-of the-art technology consists of a pressure vessel 2 with an inlet stud 3 in the upper dome and an outlet stud 4 in the lower dome, as well as a manhole 5 between an upper catalyst bed 6 and a lower catalyst bed 7. The upper catalyst bed could for example represent the Co-Mo-catalyst for converting organic sulphur compounds into HZS and the lower catalyst bed could be the Zn0-catalyst for absorbing the sulphur from HZS. The upper catalyst bed rests on a carrier grate 8, below this carrier grate 8 there is a catalyst-free space 9 into which the stud of the manhole S leads in, whereby the upper catalyst can be changed through the feed stud 3 and the lower catalyst can be changed through the manhole 5.
In fig. 1 general height data of the catalyst beds of the dead space 9, as well as further measurements are given, whose equivalent are also given in fig. 2; the relevant dimensions are reproduced as an example in a table further below.
As far as possible, in fig. 2, where device as per the invention is depicted, the same reference numbers are chosen as in the case of the description of the state-of the-art technology as mentioned in fig. I.
There the reactor 1 consists of a pressure vessel 2 with an inlet stud 3 and an outlet stud 4 for the fluid to be treated. In the dome of the pressure vessel 2 a manhole 5 is centrically situated, whereby in the inner part of the housing 2 a second cylindrical housing 12 is arranged, which contains centrically a perforated cylinder 9 or an exhaust flow pipe 9 and around it centrically further outwards a perforated pipe 10, whereby the space between the perforated pipes 9 and forms the first catalyst bed 6. The outer wall 12 of the first catalyst vessel forms the inner wall for the second catalyst 7, whereby in the example shown, the first catalyst bed is arranged for flow radially and the second catalyst bed for flow axially, without the invention being restricted only to this.
The dome 13 of the housing of the first catalyst bed 6 is penetrated by the perforated central pipe 9 with a stud 15, whereby the first catalyst housing 12 is closed at the bottom end with a base plate 14 which goes over into the carrying grate for the second catalyst deposit denoted by 20.
The functioning method of the device as per the invention with respect to the flow path of the fluid to be treated is as follows The gas to be treated is fed to the stud 3 and reaches through a pipeline 16 into a first distributor or dome space 17 and subsequently into a feeding gap 1 I in order to then flow through the first catalyst via the perforated wall 10 or the first catalyst bed 6 radially, i.e. here from outside to inside. Through the perforated central pipe 9 via the exhaust stud 15 the gas goes into the second distributor or dome space 18 above the second catalyst deposit 7 in order to penetrate it from there and flow through axially and reach through the carrier grate ring 20 to the exhaust stud 4 which is arranged in the lower floor region 19 of the reactor vessel 2.
In fig. 2, a second feed stud 3' is shown directly in the second distributor space 18. Here the gas can be guided-in in such a way that it only flows to the second catalyst bed in order to simply circumvent the first catalyst deposit 6.
Not shown further is the possibility of guiding the exhaust stud 1 S into the second dome space I 8 outwards as and when required, in order to then be able to continue using the first catalyst, if for example, the second catalyst deposit is supposed to be circumvented.
~
~ CA 02276221 1999-06-25 _ - 5 The possibility of circumventing the first catalyst bed via the second gas inlet stud 3', can be of significant advantage for operators of such devices, if the gas to be treated is relatively clean for some time, e.g. no longer contains any organic sulphur compounds and hence the first catalyst bed need not be flowed through. or in case of using same catalysts for both beds, the first catalyst bed generates high pressure loss or even gets blocked due to impurities or disturbances.
The costs of such device are also greatly reduced, which alone makes a comparison between a reactor as per the state-of the-art technology, i.e. as shown in fig. l, and a reactor as per the invention, i.e. as shown in fig. 2 clear, whereby the dimensions shown in the figures are given in tabular form. The saving in weight which can be seen in the last line of the table is 29,000 Kg, it can be recognised extremely significantly, whereby not only material costs but also transportation and assembly costs can be saved:
Table (Please see original) Gewicht = weight Figur 1 Figur 2 Volumen 6 [m3] 13,6 13,6 Volumen 7 [m3J 66,5 66,5 ho [~,J 11.000 5.500 h [~] ho 7.500 hl [mm] 7.800 __ hz [~nJ 1.600 --h3 [nun] 1.600 --[mmJ 3.300 3.850 __ 1.700 Gewicht kg 109.000 80.000
Claims (4)
1 Device for performing catalytic chemical reactions of a fluid in the gas phase, for example, desulphurization of hydrocarbons like natural gas, by using two catalysts of the same or different types situated in the flow path of the gas within a common housing in two catalyst beds, whereby one catalyst bed arranged centrally in the housing is surrounded by the second catalyst bed, in which a) the first catalyst bed (6) in the flow path has a smaller catalyst volume than the second catalyst bed (7);
b) the first and second catalyst bed (6, 7) are largely designed cylindrically, whereby the cylindrical boundary wall (12) of inner catalyst bed (6) forms the cylindrical inner wall of the second catalyst bed (7); and c) the first catalyst bed (6) can have a flow-through radially and the second catalyst bed (7) axially.
b) the first and second catalyst bed (6, 7) are largely designed cylindrically, whereby the cylindrical boundary wall (12) of inner catalyst bed (6) forms the cylindrical inner wall of the second catalyst bed (7); and c) the first catalyst bed (6) can have a flow-through radially and the second catalyst bed (7) axially.
2. Device as per claim 1, in which the measurement of the receivers for the smaller first catalyst bed (6) and the larger second catalyst bed (7) are tuned to one another in such a way that the filling heights of both catalyst beds in the total housing (2) of the catalyst are equal to a large extent.
3. Device as per claim 1 or 2 in which also the second catalyst bed (7) is designed for flow-through axially.
4. Device as per one of the precious claims, in which in the dome of the total catalyst housing (2), apart from the feed stud (3) to the dome (13) of the inner first catalyst bed (6), a second feed stud (3') is provided for circumventing the first catalyst bed (6).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19828777.1 | 1998-06-27 | ||
| DE19828777A DE19828777A1 (en) | 1998-06-27 | 1998-06-27 | Device for carrying out catalytic chemical reactions of a fluid in the gas phase |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2276221A1 true CA2276221A1 (en) | 1999-12-27 |
Family
ID=7872262
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002276221A Abandoned CA2276221A1 (en) | 1998-06-27 | 1999-06-25 | Device for performing catalytic chemical reactions of a fluid in the gas phase |
Country Status (7)
| Country | Link |
|---|---|
| EP (1) | EP0967006B1 (en) |
| JP (1) | JP2000033258A (en) |
| AT (1) | ATE246038T1 (en) |
| CA (1) | CA2276221A1 (en) |
| DE (2) | DE19828777A1 (en) |
| DK (1) | DK0967006T3 (en) |
| ES (1) | ES2201596T3 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10206132A1 (en) * | 2002-02-14 | 2003-08-21 | Basf Ag | First and second stage series reactor system, internally cascaded within a common containment shell |
| DE10226461A1 (en) * | 2002-06-13 | 2004-01-22 | Uhde Gmbh | Method and apparatus for reducing the content of NOx and N2O in gases |
| DE102011121188A1 (en) | 2011-12-16 | 2013-06-20 | Thyssen Krupp Uhde Gmbh | Apparatus and method for removing NOx and N20 |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1959219A (en) * | 1932-09-08 | 1934-05-15 | Forrest C Reed | Process of producing compounds containing carbon, hydrogen, and oxygen |
| US3544264A (en) * | 1968-09-25 | 1970-12-01 | Universal Oil Prod Co | Method and means for two-stage catalytic treating of engine exhaust gases |
| US3620685A (en) * | 1969-07-30 | 1971-11-16 | Phillips Petroleum Co | Radial flow catalyst reactor |
| US3902856A (en) * | 1971-10-05 | 1975-09-02 | Texaco Inc | Hydrogenation reactor with improved flow distribution |
| US3817716A (en) * | 1971-11-18 | 1974-06-18 | E Betz | Catalytic incineration apparatus |
| JPS61171530A (en) * | 1985-01-23 | 1986-08-02 | Hitachi Ltd | Fuel reforming device |
| DK165946C (en) * | 1985-03-21 | 1993-07-05 | Haldor Topsoe As | REFORMING PROCESS DURING HEAT EXCHANGE AND REACTOR THEREOF |
| DE3607118A1 (en) * | 1986-03-05 | 1987-09-10 | Linde Ag | Method and reactor for carrying out a catalytic reaction |
| DE3917325A1 (en) * | 1989-05-27 | 1990-11-29 | Metallgesellschaft Ag | CONVERTER FOR THE CATALYTIC IMPLEMENTATION OF GASEOUS INGREDIENTS IN GASES |
| DE19600549A1 (en) * | 1996-01-09 | 1997-07-10 | Linde Ag | Air cleaning reactor vessel |
-
1998
- 1998-06-27 DE DE19828777A patent/DE19828777A1/en not_active Ceased
-
1999
- 1999-06-11 EP EP99111405A patent/EP0967006B1/en not_active Expired - Lifetime
- 1999-06-11 DK DK99111405T patent/DK0967006T3/en active
- 1999-06-11 DE DE59906415T patent/DE59906415D1/en not_active Expired - Fee Related
- 1999-06-11 ES ES99111405T patent/ES2201596T3/en not_active Expired - Lifetime
- 1999-06-11 AT AT99111405T patent/ATE246038T1/en not_active IP Right Cessation
- 1999-06-25 CA CA002276221A patent/CA2276221A1/en not_active Abandoned
- 1999-06-25 JP JP11180577A patent/JP2000033258A/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| EP0967006B1 (en) | 2003-07-30 |
| DE19828777A1 (en) | 1999-12-30 |
| EP0967006A3 (en) | 2000-05-24 |
| ES2201596T3 (en) | 2004-03-16 |
| DK0967006T3 (en) | 2003-11-03 |
| EP0967006A2 (en) | 1999-12-29 |
| JP2000033258A (en) | 2000-02-02 |
| ATE246038T1 (en) | 2003-08-15 |
| DE59906415D1 (en) | 2003-09-04 |
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