CA1336531C - Apparatus and process suitable for producing hydrogen - Google Patents
Apparatus and process suitable for producing hydrogenInfo
- Publication number
- CA1336531C CA1336531C CA000559441A CA559441A CA1336531C CA 1336531 C CA1336531 C CA 1336531C CA 000559441 A CA000559441 A CA 000559441A CA 559441 A CA559441 A CA 559441A CA 1336531 C CA1336531 C CA 1336531C
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- Prior art keywords
- tubes
- catalyst
- inlet
- process fluid
- outlet means
- Prior art date
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- 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
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- 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
- C01B3/384—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 the catalyst being continuously externally heated
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- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/062—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 in tube reactors; the solid particles being arranged in tubes being installed in a furnace
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00157—Controlling the temperature by means of a burner
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/00777—Baffles attached to the reactor wall horizontal
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- 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
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- 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
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- 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
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
-
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
-
- 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
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
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- 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
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- 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
- C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Apparatus suitable for producing hydrogen comprising a housing containing (i) a convection section having inlet- and outlet means for a heating medium (e.g. combustion gas), and (ii) a reaction section having inlet- and outlet means for process fluid, which reaction section comprises (a) catalyst container(s) extending into the convection section and comprising a plurality of helically wound open-ended tubes wherein the process fluid (e.g. steam and methane) inlet means are in communication with the catalyst container(s) and wherein the process fluid outlet means are in communication with the upper end parts of the tubes.
Description
APPARATUS AND PROCESS SUITABLE FOR
PRODUCING HYDROGEN
The invention relates to an apparatus suitable for producing hydrogen and to a process for producing a hydrogen-containing gas.
It is well known to prepare a hydrogen-containing gas such as synthesis gas (which mainly consists of hydrogen and carbon monoxide, and in addition carbon dioxide, nitrogen and (unconverted) hydro-carbons and steam) by means of endothermic steam reforming of a hydrocarbonaceous feed in an apparatus in which heat is exchanged between flue gas and product gas in order to recover heat which is required to maintain an adequate reaction temperature. However, the heat is not recovered in such an apparatus where it is needed most i.e. in the reaction section wherein a usually highly endothermic reaction is to be carried out.
It is furthermore known to make use of the heat-content of product gas emanating from a reaction zone by employing a reaction section comprising two concentrical tubes forming an annular space which contains catalyst particles and removing product gas through the central tube, thus exchanging heat directly between the hot product gas and the catalyst.
A major problem associated with the use of a reaction section comprising concentrical tubes is the degree of heat exchange which can be attained therewith, in particular when product gas with a temperature of 800 C or even 1000 C is to be cooled.
Surprisingly, it has now been found that helically wound tubes arranged inside catalyst containers provide excellent heat transfer between hot product gas removed via said tubes and surrounding catalyst particles which are further heated by convective heat exchange.
The invention therefore relates to an apparatus suitable for producing hydrogen which comprises ,~., ~
PRODUCING HYDROGEN
The invention relates to an apparatus suitable for producing hydrogen and to a process for producing a hydrogen-containing gas.
It is well known to prepare a hydrogen-containing gas such as synthesis gas (which mainly consists of hydrogen and carbon monoxide, and in addition carbon dioxide, nitrogen and (unconverted) hydro-carbons and steam) by means of endothermic steam reforming of a hydrocarbonaceous feed in an apparatus in which heat is exchanged between flue gas and product gas in order to recover heat which is required to maintain an adequate reaction temperature. However, the heat is not recovered in such an apparatus where it is needed most i.e. in the reaction section wherein a usually highly endothermic reaction is to be carried out.
It is furthermore known to make use of the heat-content of product gas emanating from a reaction zone by employing a reaction section comprising two concentrical tubes forming an annular space which contains catalyst particles and removing product gas through the central tube, thus exchanging heat directly between the hot product gas and the catalyst.
A major problem associated with the use of a reaction section comprising concentrical tubes is the degree of heat exchange which can be attained therewith, in particular when product gas with a temperature of 800 C or even 1000 C is to be cooled.
Surprisingly, it has now been found that helically wound tubes arranged inside catalyst containers provide excellent heat transfer between hot product gas removed via said tubes and surrounding catalyst particles which are further heated by convective heat exchange.
The invention therefore relates to an apparatus suitable for producing hydrogen which comprises ,~., ~
(i) a housing containing a convection section having inlet- and outlet means for a heating medium, and (ii) a reaction section having inlet- and outlet means for process fluid, which reaction section comprises (a) catalyst container(s) extending into the convection section and each catalyst container comprising a plurality of helically wound open-ended tubes wherein the process fluid inlet means are in communication with the catalyst container(s) and wherein the process fluid outlet means are in communication with the upper end parts of the tubes.
The invention further relates to a process for producing a hydrogen-containing gas which comprises contacting a hydrocarbonaceous feed in the presence of steam at elevated temperature and pressure with a reforming catalyst which is heated by means of convective heat transfer and removing hydrogen-containing product gas through helically wound tubes extending in the reforming catalyst.
The apparatus and process according to the invention will be elucidated hereinafter with the use of the Figures in which various preferred embodiments have been incorporated without having the intent of limiting the invention to those particular embodiments as depicted in the Figures. Reference numerals relating to corresponding parts are the same for Figures 1-3.
Figure 1 relates to a longitudinal section of an apparatus according to the invention.
In Figure 2 a cross section is shown at AA' of the apparatus depicted in Figure 1.
Figure 3 represents a longitudinal section of an apparatus which contains additional heat exchange means, compared _ 2a 1 3 3 6 5 31 63293-2911 with the apparatus depicted in Figure 1.
The apparatus depicted in Figure 1 comprises a housing (1) containing a convection section (2) having inlet means (3) for a heating medium e.g. a hot liquid or gas or even particulate solids, preferably combustion gas, and outlet means (4) therefor.
The housing furthermore contains a reaction section comprising one or more catalyst containers (8) and a distribution section (5) 1 33653 t having inlet means (6) for process fluid such as a feed mixture of steam and a hydrocarbons-containing gas (preferably natural gas or methane) and outlet means (7) for process fluid such as a mixture of hydrogen-containing product gas and unconverted feed gas.
The catalyst containers (8) are preferably tubular shaped and enclose at least the major part of a plurality of at least partly helically wound open-ended tubes (9).
Preferably, a plurality of tubular catalyst containers (8), which are suitably arranged in one (as depicted in Figure 2) or more (concentrical) circular patterns in the housing (1), extend downwardly into the convection section (2).
The distribution section (5) is preferably separated from the convection section (2) by means of a tube sheet (10) in order to avoid contamination of product gas emanating through outlet means (11) with heating gas. Moreover, by suspending the tubular catalyst containers by means of tube sheet (10) the containers can expand freely during start up of the apparatus according to the invention, without causing problems such as cracking of the tubes or tube connections which can easily occur when the tubes are connected at both ends to in- or outlets means.
In order to ensure as uniform heating of the catalyst containers as possible, the convection section preferably contains means (12) for preventing radiant heat transfer, such as the disc-shaped insulation means e.g. containing refractory material depicted in Figures 1 and 3.
Process feed gas can enter a catalyst container only through inlet opening (13) in the upper end part thereof and proceeds downwardly through the particulate catalyst which is preferably used in order to be able to operate at a relatively low temperature from 400 to 1200 C at a pressure from 2 to 200 bar in the reaction section (5).
Preferably, the catalyst containers (8) are provided with catalyst support means (14) in their closed lower end parts in order to avoid entrainment of catalyst particles into the open lower end parts (15) of the two helical coil tubes which are preferably present in each catalyst container. The catalyst support means (14) may additionally serve as positioning means for said lower end parts (15) of the helical coil tubes.
During operation hot process gas centers tubes (9) through end parts (15) as depicted in Figures 1 and 3 and flows upwardly, thus ensuring optimal heat exchange with the surrounding catalyst.
Heat exchanged process gas (which still may have a temperature of e.g. 500-1000 C) enters the annular-shaped channel (16) present in the upper end part (29) of catalyst container (8) and communi-cating with a pair of helically wound tubes. The annular channels(16) are in open communication with product outlet means (7) via manifold tubes (17).
In the above-described manner the upper parts of each pair of helically wound tubes (9) are connected to a single outlet manifold (7) for process fluid arranged substantially centrally in the upper part of the housing (1). Such an arrangement is very advantageous from a constructional point of view because the use of a plurality of individual outlet means for each catalyst tube, with the associated sealing and expansion problems, can thus be avoided; moreover, the pressure in all manifold tubes (17) will be substantially equal, thus ensuring optimal distribution of process gas over all catalyst containers.
In the bottom section (18) of housing (1) one or more combustor outlet means may be present as depicted in Figures 1 and 3 which function as inlet means (3) for heating medium. In a preferred embodiment of the apparatus according to the invention a plurality (e.g. three) of combustor outlet means are (e.g. tangentially) arranged in the housing in a rotation-symmetrical manner (not depicted in the Figures) in order to ensure optimal distribution of combustion gas throughout the combustion section (2).
The combustion means depicted in Figures 1 and 3 comprise inlet means (19) for (e.g. oxygen-enriched) air, inlet means (20) for a combustible fluid (e.g. hydrocarbonaceous gas, llquid and/or coal) and, optionally, inlet means (21) for recycled gas such as _ 5 _ 1 33653 1 carbon monoxide-containing gas separated off from hydrogen- and carbon monoxide containing product gas e.g. by means of pressure swing adsorption (not shown in the Figures), or recycled flue gas.
In Figure 3 a more complex, even more heat-efficient embodiment of the apparatus according to the invention is depicted wherein the outlet manifold (7) comprises a plurality of concentrically arranged tubes forming at least one annular space (22) which is in open communication with inlet means (23) and outlet means (24) for heat exchange fluid (e.g. relatively cold expanded and/or heat-exchanged flue gas) extending outside the housing (1).
Product outlet means (7) now comprise a tubular housing (24) extending through tube sheet (10) into convection zone (2). The closed bottom end part (25) of housing (24) is connected to heat exchange fluid inlet means (23), preferably by means of expansion bellows (not shown in Figure 3). Product manifold tubes (17) are in open communication with tubular heat exchange means (26) having a closed lower end part (27) in order to reverse the downward flow of product gas during operation through the annular space (28) into the open-ended tubular product outlet means (11) which extend through manifold (17) into said tubular means (26).
With the above-described product outlet means a substantial part of the thermal energy still present in the product gas emanating from manifold tubes (17) can be recovered.
The invention further relates to a process for producing a hydrogen-containing gas which comprises contacting a hydrocarbonaceous feed in the presence of steam at elevated temperature and pressure with a reforming catalyst which is heated by means of convective heat transfer and removing hydrogen-containing product gas through helically wound tubes extending in the reforming catalyst.
The apparatus and process according to the invention will be elucidated hereinafter with the use of the Figures in which various preferred embodiments have been incorporated without having the intent of limiting the invention to those particular embodiments as depicted in the Figures. Reference numerals relating to corresponding parts are the same for Figures 1-3.
Figure 1 relates to a longitudinal section of an apparatus according to the invention.
In Figure 2 a cross section is shown at AA' of the apparatus depicted in Figure 1.
Figure 3 represents a longitudinal section of an apparatus which contains additional heat exchange means, compared _ 2a 1 3 3 6 5 31 63293-2911 with the apparatus depicted in Figure 1.
The apparatus depicted in Figure 1 comprises a housing (1) containing a convection section (2) having inlet means (3) for a heating medium e.g. a hot liquid or gas or even particulate solids, preferably combustion gas, and outlet means (4) therefor.
The housing furthermore contains a reaction section comprising one or more catalyst containers (8) and a distribution section (5) 1 33653 t having inlet means (6) for process fluid such as a feed mixture of steam and a hydrocarbons-containing gas (preferably natural gas or methane) and outlet means (7) for process fluid such as a mixture of hydrogen-containing product gas and unconverted feed gas.
The catalyst containers (8) are preferably tubular shaped and enclose at least the major part of a plurality of at least partly helically wound open-ended tubes (9).
Preferably, a plurality of tubular catalyst containers (8), which are suitably arranged in one (as depicted in Figure 2) or more (concentrical) circular patterns in the housing (1), extend downwardly into the convection section (2).
The distribution section (5) is preferably separated from the convection section (2) by means of a tube sheet (10) in order to avoid contamination of product gas emanating through outlet means (11) with heating gas. Moreover, by suspending the tubular catalyst containers by means of tube sheet (10) the containers can expand freely during start up of the apparatus according to the invention, without causing problems such as cracking of the tubes or tube connections which can easily occur when the tubes are connected at both ends to in- or outlets means.
In order to ensure as uniform heating of the catalyst containers as possible, the convection section preferably contains means (12) for preventing radiant heat transfer, such as the disc-shaped insulation means e.g. containing refractory material depicted in Figures 1 and 3.
Process feed gas can enter a catalyst container only through inlet opening (13) in the upper end part thereof and proceeds downwardly through the particulate catalyst which is preferably used in order to be able to operate at a relatively low temperature from 400 to 1200 C at a pressure from 2 to 200 bar in the reaction section (5).
Preferably, the catalyst containers (8) are provided with catalyst support means (14) in their closed lower end parts in order to avoid entrainment of catalyst particles into the open lower end parts (15) of the two helical coil tubes which are preferably present in each catalyst container. The catalyst support means (14) may additionally serve as positioning means for said lower end parts (15) of the helical coil tubes.
During operation hot process gas centers tubes (9) through end parts (15) as depicted in Figures 1 and 3 and flows upwardly, thus ensuring optimal heat exchange with the surrounding catalyst.
Heat exchanged process gas (which still may have a temperature of e.g. 500-1000 C) enters the annular-shaped channel (16) present in the upper end part (29) of catalyst container (8) and communi-cating with a pair of helically wound tubes. The annular channels(16) are in open communication with product outlet means (7) via manifold tubes (17).
In the above-described manner the upper parts of each pair of helically wound tubes (9) are connected to a single outlet manifold (7) for process fluid arranged substantially centrally in the upper part of the housing (1). Such an arrangement is very advantageous from a constructional point of view because the use of a plurality of individual outlet means for each catalyst tube, with the associated sealing and expansion problems, can thus be avoided; moreover, the pressure in all manifold tubes (17) will be substantially equal, thus ensuring optimal distribution of process gas over all catalyst containers.
In the bottom section (18) of housing (1) one or more combustor outlet means may be present as depicted in Figures 1 and 3 which function as inlet means (3) for heating medium. In a preferred embodiment of the apparatus according to the invention a plurality (e.g. three) of combustor outlet means are (e.g. tangentially) arranged in the housing in a rotation-symmetrical manner (not depicted in the Figures) in order to ensure optimal distribution of combustion gas throughout the combustion section (2).
The combustion means depicted in Figures 1 and 3 comprise inlet means (19) for (e.g. oxygen-enriched) air, inlet means (20) for a combustible fluid (e.g. hydrocarbonaceous gas, llquid and/or coal) and, optionally, inlet means (21) for recycled gas such as _ 5 _ 1 33653 1 carbon monoxide-containing gas separated off from hydrogen- and carbon monoxide containing product gas e.g. by means of pressure swing adsorption (not shown in the Figures), or recycled flue gas.
In Figure 3 a more complex, even more heat-efficient embodiment of the apparatus according to the invention is depicted wherein the outlet manifold (7) comprises a plurality of concentrically arranged tubes forming at least one annular space (22) which is in open communication with inlet means (23) and outlet means (24) for heat exchange fluid (e.g. relatively cold expanded and/or heat-exchanged flue gas) extending outside the housing (1).
Product outlet means (7) now comprise a tubular housing (24) extending through tube sheet (10) into convection zone (2). The closed bottom end part (25) of housing (24) is connected to heat exchange fluid inlet means (23), preferably by means of expansion bellows (not shown in Figure 3). Product manifold tubes (17) are in open communication with tubular heat exchange means (26) having a closed lower end part (27) in order to reverse the downward flow of product gas during operation through the annular space (28) into the open-ended tubular product outlet means (11) which extend through manifold (17) into said tubular means (26).
With the above-described product outlet means a substantial part of the thermal energy still present in the product gas emanating from manifold tubes (17) can be recovered.
Claims (7)
1. Apparatus suitable for producing hydrogen which comprises (i) a housing containing a convection section having inlet-and outlet means for a heating medium, and (ii) a reaction section having inlet-and outlet means for process fluid, which reaction section comprises (a) catalyst container(s) extending into the convection section and each catalyst container comprising a plurality of helically wound open-ended tubes wherein the process fluid inlet means are in communication with the catalyst container(s) and wherein the process fluid outlet means are in communication with the upper end parts of the tubes.
2. Apparatus according to claim 1 wherein the convection section contains means for preventing radiant heat transfer to the catalyst containers.
3. Apparatus according to claim 1 wherein the convection-and the reaction sections are separated by a tube sheet.
4. Apparatus according to claim 3 wherein a plurality of tubular catalyst containers extend downwardly through the tube sheet into the convection section.
5. Apparatus according to any one of claim 1 to 4 wherein the upper end parts of the helically wound tubes are connected to a single outlet manifold for process fluid arranged substantially centrally in the upper part of the housing.
6. Apparatus according to claim 5 wherein the outlet manifold comprises a plurality of concentrically arranged tubes forming at least one annular space which is in communication with inlet- and outlet means for heat exchange fluid extending outside the housing.
7. Process for producing a hydrogen-containing gas using the apparatus as claimed in claim 1, comprising the steps of contacting a hydrocarbonaceous feed in the presence of steam at elevated temperature and pressure with a reforming catalyst which is heated by means of convective heat transfer and removing hydrogen-containing product gas through helically wound tubes extending in the reforming catalyst.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8704959 | 1987-03-03 | ||
| GB8704959A GB2201903B (en) | 1987-03-03 | 1987-03-03 | Apparatus and process suitable for producing hydrogen |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1336531C true CA1336531C (en) | 1995-08-08 |
Family
ID=10613252
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000559441A Expired - Fee Related CA1336531C (en) | 1987-03-03 | 1988-02-22 | Apparatus and process suitable for producing hydrogen |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JP2787773B2 (en) |
| KR (1) | KR960005505B1 (en) |
| CA (1) | CA1336531C (en) |
| DE (1) | DE3806536C2 (en) |
| GB (1) | GB2201903B (en) |
| MY (1) | MY103066A (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2835851B2 (en) * | 1989-06-23 | 1998-12-14 | ヤマハ発動機株式会社 | Reformer for fuel cell |
| GB2238487A (en) * | 1989-11-25 | 1991-06-05 | Methan Limited | Reforming apparatus |
| DE19512945A1 (en) * | 1995-03-28 | 1996-10-24 | Mannesmann Ag | Catalyst tube |
| IT1283877B1 (en) * | 1996-01-12 | 1998-05-07 | Kinetics Technology | ISOTHERMAL CATALYTIC REACTOR FOR HIGH TEMPERATURE ENDOTHERMIC REACTIONS |
| EP0911076A1 (en) * | 1997-10-23 | 1999-04-28 | Haldor Topsoe A/S | Reformer furnace with internal recirculation |
| CA2357960C (en) * | 2000-10-10 | 2007-01-30 | Tokyo Gas Co., Ltd. | Single-pipe cylinder type reformer |
| BRPI0814196A2 (en) | 2007-07-05 | 2015-01-27 | Saudi Basic Ind Corp | Process to perform an endothermic reaction |
| DE102011118217A1 (en) * | 2011-11-11 | 2013-05-16 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Reformer tube with internal heat exchange |
| EP3266739B1 (en) * | 2016-07-07 | 2018-12-05 | L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude | Corrosion protected reformer tube with internal heat exchanger |
| EP3296255A1 (en) * | 2016-09-14 | 2018-03-21 | L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude | Reformer tube with structured catalyst and improved temperature control |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3442618A (en) * | 1965-08-04 | 1969-05-06 | United Aircraft Corp | Method for producing hydrogen from hydrogen-containing feedstocks |
| ES183753Y (en) * | 1969-01-15 | 1974-08-16 | A REACTOR ELEMENT FOR THE CONSERVATION OF HYDROCARBONS. | |
| DE2412840C2 (en) * | 1974-03-18 | 1982-11-11 | Metallgesellschaft Ag, 6000 Frankfurt | Tube reactor for the catalytic cracking of hydrocarbons |
| NL187622C (en) * | 1975-04-14 | 1991-12-02 | Stone & Webster Eng Corp | REFORM OVEN WITH CONVECTION HEATING OF PROCESS TUBES. |
| MX168335B (en) * | 1982-08-12 | 1993-05-17 | Mitsubishi Heavy Ind Ltd | IMPROVED APPARATUS FOR REFORMING FUEL |
| JPS60248230A (en) * | 1984-05-25 | 1985-12-07 | Babcock Hitachi Kk | Catalytic combustion type reactor |
-
1987
- 1987-03-03 GB GB8704959A patent/GB2201903B/en not_active Expired - Fee Related
-
1988
- 1988-02-22 CA CA000559441A patent/CA1336531C/en not_active Expired - Fee Related
- 1988-02-29 KR KR1019880002136A patent/KR960005505B1/en not_active IP Right Cessation
- 1988-03-01 MY MYPI88000205A patent/MY103066A/en unknown
- 1988-03-01 DE DE3806536A patent/DE3806536C2/en not_active Expired - Fee Related
- 1988-03-01 JP JP63045997A patent/JP2787773B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| GB2201903A (en) | 1988-09-14 |
| JP2787773B2 (en) | 1998-08-20 |
| KR960005505B1 (en) | 1996-04-25 |
| GB2201903B (en) | 1990-11-28 |
| DE3806536C2 (en) | 1997-01-30 |
| GB8704959D0 (en) | 1987-04-08 |
| JPS63230502A (en) | 1988-09-27 |
| KR880011009A (en) | 1988-10-25 |
| DE3806536A1 (en) | 1988-09-15 |
| MY103066A (en) | 1993-04-30 |
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Legal Events
| Date | Code | Title | Description |
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| MKLA | Lapsed |