WO2006043111A1 - Hydrogen production - Google Patents
Hydrogen production Download PDFInfo
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- WO2006043111A1 WO2006043111A1 PCT/GB2005/050173 GB2005050173W WO2006043111A1 WO 2006043111 A1 WO2006043111 A1 WO 2006043111A1 GB 2005050173 W GB2005050173 W GB 2005050173W WO 2006043111 A1 WO2006043111 A1 WO 2006043111A1
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- WIPO (PCT)
- Prior art keywords
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- feed gas
- hydrogen
- gas
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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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/249—Plate-type reactors
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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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- 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
- C01B3/48—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 followed by reaction of water vapour with carbon monoxide
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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
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2451—Geometry of the reactor
- B01J2219/2453—Plates arranged in parallel
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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
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2461—Heat exchange aspects
- B01J2219/2465—Two reactions in indirect heat exchange with each other
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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
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2461—Heat exchange aspects
- B01J2219/2466—The same reactant stream undergoing different reactions, endothermic or exothermic
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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
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2469—Feeding means
- B01J2219/2471—Feeding means for the catalyst
- B01J2219/2472—Feeding means for the catalyst the catalyst being exchangeable on inserts other than plates, e.g. in bags
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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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift 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
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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
- C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing 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
- 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
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
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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
- C01B2203/0872—Methods of cooling
- C01B2203/0888—Methods of cooling by evaporation of a fluid
-
- 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
- C01B2203/0872—Methods of cooling
- C01B2203/0888—Methods of cooling by evaporation of a fluid
- C01B2203/0894—Generation of steam
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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
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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
- C01B2203/80—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
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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
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to an apparatus and a process for producing hydrogen from natural gas or methane.
- Natural gas as produced from a gas well consists primarily of methane, but may also contain up to about 10% of ethane and propane. Natural gas as supplied to domestic users has chemical odours added to it to ensure that any gas leak can be detected by smell, and may contain small quantities of higher hydrocarbons such as C2 to C4 compounds. Hydrocarbons up to C4 are referred to herein as short chain hydrocarbons .
- a process is described in WO 01/51194 and WO 03/048034 (Accentus pic) in which methane is reacted with steam, to generate carbon monoxide and hydrogen in a first catalytic reactor; the resulting gas mixture is then used to perform Fischer-Tropsch synthesis in a second catalytic reactor.
- the first stage of this process produces hydrogen, but it is inevitably produced in conjunction with carbon monoxide, and so this is not a satisfactory source of hydrogen, because for example pressure swing absorption materials are deleteriously affected by carbon monoxide if it is present at above about 10%.
- the present invention accordingly provides a plant for producing hydrogen from a feed gas comprising short chain hydrocarbons, the plant comprising reactor means defining channels for treating the feed gas in three successive stages, the channels for treating the feed gas in each case being adjacent to respective heat transfer channels, and the successive treatment stages being as follows :
- the feed gas is heated by heat exchange from the exhaust gases from the catalytic combustion channels.
- the overall process is thermodynamically efficient, in that the heat from the combustion exhaust stream is used to preheat the feed gas, and the heat from the gases produced by reforming is used to generate the steam.
- the reactor means is a single integrated reactor in which all three of the successive treatment stages occur.
- Such a reactor may be formed by a stack of plates between which the treatment channels and heat transfer channels are defined alternately in the stack.
- the hydrogen-producing plant also incorporates other components.
- the feed gas may be natural gas, and if the feed gas contains sulphur-containing compounds, then the plant will incorporate a desulphurising unit, which may for example be a de-sulphurisation bed, and this will typically be arranged to treat the feed gas after it has been preheated in stage (a) but before it is reformed in stage (b) .
- a desulphurising unit which may for example be a de-sulphurisation bed, and this will typically be arranged to treat the feed gas after it has been preheated in stage (a) but before it is reformed in stage (b) .
- this mixing means may either be integral with the integrated reactor, or may be a separate mixing unit .
- the gas stream emerging from stage (c) after the water gas shift reaction contains a high proportion of hydrogen, typically between 60 and 90%, and smaller proportions of carbon monoxide, carbon dioxide, steam and methane.
- This gas stream is subjected to a hydrogen separation treatment. This may require a preliminary cooling step, to a temperature suitable for the hydrogen separation process, and so as to condense some of the steam.
- the hydrogen separation treatment may utilise membrane separation or pressure swing absorption, and preferably removes at least 50% of the hydrogen, more preferably at least 70% but no more than 90%.
- the resulting tail gas contains hydrogen, methane and some carbon monoxide and carbon dioxide, and may be used as the fuel for the combustion channels.
- the hydrogen separation treatment typically requires the gases to be at an elevated pressure in the range 4 to 14 atmospheres (0.4 to 1.4 MPa), and preferably all the treatment stages for the feed gas are at such an elevated pressure, so that no compression of the gas mixture produced by stage (c) is necessary. If necessary, the feed gas is compressed to such an elevated pressure before being supplied to the reactor means, but in many contexts the feed gas will already be at a suitable elevated pressure.
- the invention also provides a process for producing hydrogen from a feed gas comprising short chain hydrocarbons, and making use of such a plant.
- Figure 1 shows a flow diagram of the plant of the invention
- Figure 2 shows a sectional view of a reactor suitable for use in the plant of figure 1;
- Figure 3 shows a sectional view of a stack of plates, shown separated, for making the reactor of figure 2.
- a plant 10 for generating pure hydrogen is provided with natural gas from a pipeline 12 at a pressure of 1.4 MPa.
- the plant 10 includes a compact reactor 14 in which the natural gas is subjected to three successive treatment stages 16, 18 and 20, these stages being shown separately for clarity in the diagram.
- the reactor 14 is also provided with air, compressed to a sufficient pressure by a compressor 22 and passed through a filter 24.
- the reactor 14 consists of a stack of flat plates separated by plates with rectangular corrugations so as to define flow channels for different fluids between successive flat plates, as described below in relation to figures 2 and 3.
- the first stage 16 is a preheating stage, and this part of the reactor 14 has channels for three different fluids arranged successively in the stack: combustion exhaust gases 16a (flowing axially from top to bottom as shown), natural gas 16b (flowing diagonally), and air 16c (flowing diagonally) such that the natural gas and the air are both preheated by heat exchange with the exhaust gases.
- combustion exhaust gases 16a flowing axially from top to bottom as shown
- natural gas 16b flowing diagonally
- air 16c flowing diagonally
- the flow directions may differ from those shown here, and for example the natural gas and the air might flow along serpentine paths made up as a series of cross-flow passes between appropriate headers.
- the natural gas is then passed through a desulphurisation bed 26 in which any sulphur-containing odours are removed by chemisorption. It is then mixed with steam at the same elevated pressure at a mixer 28 at a controlled mole ratio with respect to the carbon in the feed gas. This ratio is in the range 2 to 4:1 of steam relative to carbon, in order to promote not only steam reforming but also the water gas shift reaction.
- This hot mixture of natural gas and steam is then passed into the second stage 18 in which it exchanges heat with a catalytic combustion reaction in adjacent channels, while contacting a reforming catalyst.
- the combustion channels 18a (extending axially from bottom to top as shown) contain a combustion catalyst, while the reforming channels 18b (extending transversely) contain the reforming catalyst.
- oxidation reaction catalytic combustion
- catalysts for example palladium, platinum or copper on a ceramic support; for example copper or platinum on an alumina support stabilised with lanthanum, cerium or barium, or palladium on zirconia, or palladium on a metal hexaaluminate such as magnesium, calcium, strontium, barium or potassium hexaaluminate.
- metal hexaaluminate such as magnesium, calcium, strontium, barium or potassium hexaaluminate.
- nickel, platinum, palladium, ruthenium or rhodium which may be used on ceramic coatings; the preferred catalyst for the reforming reaction is rhodium or platinum on alumina or stabilised alumina.
- the catalyst is provided in the form of a corrugated metal foil coated with the ceramic coating, typically no more than 100 ⁇ m thick, and impregnated with the catalytic metal, such a corrugated foil being inserted into each flow channel in which a reaction is to occur.
- a corrugated foil being inserted into each flow channel in which a reaction is to occur.
- the reforming channels are at an elevated temperature that may for example be 800 0 C.
- the methane reacts with water vapour, by the reaction:
- the resulting gas mixture which may be referred to as synthesis gas, is then supplied to the third stage 20 in which it loses heat to form the high-temperature steam in the adjacent channels 20a (the steam channels being shown extending axially from bottom to top) , the channels 20b carrying the synthesis gas (extending transversely as shown) containing a catalyst for the water gas shift reaction:
- the effect of the water gas shift reaction is to increase the proportion of hydrogen, and to decrease the proportion of carbon monoxide.
- the carbon monoxide proportion is reduced to no more than about 5% (by volume) .
- the resulting gas mixture comprises hydrogen, unreacted methane, carbon monoxide and carbon dioxide, and steam. It is first passed through a heat exchanger 30 in which it is cooled by air to the optimal value for the subsequent hydrogen removal. After cooling, the excess steam condenses, and is separated in a separator 32 and may be returned to the steam generating channels 20a. Alternatively this heat exchanger 30 might use water as coolant .
- the cooled gas mixture is then supplied to the hydrogen recovery unit 34. This may utilise pressure swing absorption to separate a pure hydrogen stream 36. This is operated in such a way that about 75% of the hydrogen is removed.
- the remaining tail gases 38 are then fed, via a detonation arrester 40 and a mixer 42 in which they are mixed with the preheated air, into the combustion channels 18a.
- a water supply 44 is required by the plant 10 at least for start-up and for process water make-up and this is supplied through a pressurising pump 45. It must be pure water to ensure the integrity of the steam raising circuit and the reforming catalyst, so this water supply is treated by an absorption column 46. During operation, most of the water for generating steam is actually provided by condensing the steam in the heat exchanger 30. To initiate operation of the plant 10, a proportion of the combustion air may be heated electrically so that when mixed with the natural gas combustion will occur in the presence of the catalyst in the combustion channels 18 a .
- the materials of which the reactor 14 are made are subjected to a severely corrosive atmosphere in use, for example the temperature in the combustion channels 18a may be as high as 900°, although more typically around 85O 0 C.
- the plates forming the reactor 14 may be made of an iron/nickel/chromium alloy for high temperature use, such as Haynes HR-120 or Inconel 800HT (trade marks) .
- the catalyst substrates do not have to resist pressure differences, and may be of an aluminium-bearing ferritic steel such as Fecralloy (trade mark) which is iron with up to 20% chromium, 0.5 - 12% aluminium, and 0.1 - 3% yttrium.
- the metal might comprise iron with 15% chromium, 4% aluminium, and 0.3% yttrium.
- this metal When this metal is heated in air it forms an adherent oxide coating of alumina which protects the alloy against further oxidation; this oxide layer also protects the alloy against corrosion under conditions that prevail within for example a methane oxidation reactor or a steam/methane reforming reactor.
- the corrugated foil for a catalyst substrate, and is coated with a ceramic layer into which a catalyst material is incorporated, the alumina oxide layer on the metal is believed to bind with the oxide coating, so ensuring the catalytic material adheres to the metal substrate.
- the substrate may be a wire mesh or a felt sheet, which may be corrugated, dimpled or pleated, but the preferred substrate is a thin metal foil.
- the metal substrate of the catalyst structure within the flow channels enhances heat transfer and catalyst surface area.
- the catalyst structures are removable from the channels in the stack, so they can be replaced if the catalyst becomes spent; consequently headers or covers must be provided on the stack which can be removed to provide access to the channels, for this removal and replacement.
- the stack of plates forming the reactor 14 are bonded together either by diffusion bonding or by brazing.
- the reactor 14 comprises a stack of rectangular flat plates 50 (see figure 3) each 1 mm thick, spaced apart by corrugated plates. Depending on the scale of the plant 10, these plates 50 might be of length between 100 and 1200 mm, and of width between 75 and 600 mm.
- Axial flow channels 52 (such as the flow channels 16a, 18a or 20a) are defined by plates 54 corrugated with rectangular castellations 5 mm high and 20 mm wide; each such plate 54 is provided with an edge rib 55 of the same height as the overall height of the castellated plate 54 along each side.
- Transverse flow channels 56 are defined by plates 58 with similar rectangular castellations, for example 5 mm high and 20 mm wide, and with similar edge ribs 59, each plate 58 having castellations extending from one side to the other of the stack, but the width of each plate 58 is only a third of the total length of the stack, so that there are three such plates 58 side-by-side.
- appropriate headers 60 are welded onto each end of the stack to communicate with the axial flow channels 52.
- an inlet header 62 is welded to the stack at one end of one side, and an outlet header 63 at the other end of the other side, each being of the same width as one of the castellated plates 58. Headers 64 of twice that width are then welded on to the remainder of each side, so as to communicate with the other pair of castellated plates 58 on that side. Hence the castellated plates 58 and the headers 62, 64 and 63 ensure that the gases flowing in these transverse flow channels 56 follow a generally zigzag path, as shown by the arrows.
- Diagonal flow channels such as the flow channels 16b and 16c may be defined by similar castellated plates whose castellations extend in an appropriate diagonal direction between respective inlet headers and outlet headers attached to the sides of the stack.
- the axial flow channels 18a contain catalyst foils as described earlier, as do the transverse flow channels 18b and 20b. When it is necessary to replace the catalyst, this may be done by cutting off one of the headers 60, or both the headers 64, extracting the foils on which the catalyst is spent, and replacing with fresh catalyst-carrying foils. The headers 60 or 64 can then be re-welded into position.
- the reactor 14 shown in figures 2 and 3 is by way of example only, and that a hydrogen production plant of the invention might utilise a different design of compact catalytic reactor.
- the channels, or at least some of the channels might be defined by grooves in thick plates, rather than by castellations in thin plates.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP05791679A EP1812338A1 (en) | 2004-10-18 | 2005-10-05 | Apparatus and process for the production of hydrogen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB0423081.9 | 2004-10-18 | ||
GBGB0423081.9A GB0423081D0 (en) | 2004-10-18 | 2004-10-18 | Hydrogen production |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006043111A1 true WO2006043111A1 (en) | 2006-04-27 |
Family
ID=33462899
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB2005/050173 WO2006043111A1 (en) | 2004-10-18 | 2005-10-05 | Hydrogen production |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1812338A1 (en) |
GB (1) | GB0423081D0 (en) |
WO (1) | WO2006043111A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7829602B2 (en) | 2007-01-19 | 2010-11-09 | Velocys, Inc. | Process and apparatus for converting natural gas to higher molecular weight hydrocarbons using microchannel process technology |
US8100996B2 (en) | 2008-04-09 | 2012-01-24 | Velocys, Inc. | Process for upgrading a carbonaceous material using microchannel process technology |
US8747656B2 (en) | 2008-10-10 | 2014-06-10 | Velocys, Inc. | Process and apparatus employing microchannel process technology |
US9676623B2 (en) | 2013-03-14 | 2017-06-13 | Velocys, Inc. | Process and apparatus for conducting simultaneous endothermic and exothermic reactions |
US9908093B2 (en) | 2008-04-09 | 2018-03-06 | Velocys, Inc. | Process for converting a carbonaceous material to methane, methanol and/or dimethyl ether using microchannel process technology |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0600621A1 (en) * | 1992-12-02 | 1994-06-08 | Rolls-Royce And Associates Limited | A combined reformer and shift reactor |
EP0861802A2 (en) * | 1997-02-28 | 1998-09-02 | Mitsubishi Denki Kabushiki Kaisha | Fuel reforming apparatus |
US6203587B1 (en) * | 1999-01-19 | 2001-03-20 | International Fuel Cells Llc | Compact fuel gas reformer assemblage |
EP1142632A1 (en) * | 1998-12-15 | 2001-10-10 | Osaka Gas Company Limited | Fluid treating device |
US20020131919A1 (en) * | 2001-03-15 | 2002-09-19 | Debellis Crispin L. | Modular fuel processing system for plate reforming type units |
WO2004013258A1 (en) * | 2002-08-02 | 2004-02-12 | Catacel Corporation | Autothermal catalytic stem reformer |
-
2004
- 2004-10-18 GB GBGB0423081.9A patent/GB0423081D0/en not_active Ceased
-
2005
- 2005-10-05 EP EP05791679A patent/EP1812338A1/en not_active Withdrawn
- 2005-10-05 WO PCT/GB2005/050173 patent/WO2006043111A1/en active Application Filing
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0600621A1 (en) * | 1992-12-02 | 1994-06-08 | Rolls-Royce And Associates Limited | A combined reformer and shift reactor |
EP0861802A2 (en) * | 1997-02-28 | 1998-09-02 | Mitsubishi Denki Kabushiki Kaisha | Fuel reforming apparatus |
EP1142632A1 (en) * | 1998-12-15 | 2001-10-10 | Osaka Gas Company Limited | Fluid treating device |
US6203587B1 (en) * | 1999-01-19 | 2001-03-20 | International Fuel Cells Llc | Compact fuel gas reformer assemblage |
US20020131919A1 (en) * | 2001-03-15 | 2002-09-19 | Debellis Crispin L. | Modular fuel processing system for plate reforming type units |
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GB0423081D0 (en) | 2004-11-17 |
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