US20120195813A1

US20120195813A1 - Catalytic Reactors

Info

Publication number: US20120195813A1
Application number: US13/438,257
Authority: US
Inventors: Michael Joseph Bowe
Original assignee: CompactGTL PLC
Current assignee: CompactGTL PLC
Priority date: 2005-03-05
Filing date: 2012-04-03
Publication date: 2012-08-02
Also published as: CA2597161A1; AU2006221805A1; GB0714314D0; CA2597161C; WO2006095204A1; AU2006221805B2; EA011296B1; TW200640575A; GB0504622D0; BRPI0607501A2; US20080148635A1; CN101137434B; CN101137434A; NO20074479L; GB2436773A; EP1922141A1; DE112006000447T5; US8173083B2; EA200701897A1

Abstract

A compact catalytic reactor defining a multiplicity of alternately arranged first and second flow channels, for carrying first and second fluids, respectively. At least the first fluids undergo a chemical reaction. Each first flow channel contains a removable gas-permeable catalyst structure incorporating a metal foil substrate, said catalyst structure defining flow paths therethrough. The substrate comprises a stack of spaced-apart foils wherein the catalyst structure incorporates a multiplicity of resilient strips which are bent out from the foil substrate so as to project from the substrate and to support said catalyst structure resiliently spaced away from at least one adjacent wall of said channel. Each strip being connected to said catalyst structure only at an end or ends of said strip, and being integral with said foil.

Description

This invention relates to a catalytic reactor suitable for use in a chemical process to convert natural gas to longer-chain hydrocarbons, and to a plant including such catalytic reactors to perform the process.
A process is described in WO 01/51194 and WO 03/033131 (Accentus plc) 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 overall result is to convert methane to longer chain hydrocarbons of higher molecular weight, which are usually liquids or waxes under ambient conditions. The two stages of the process, steam/methane reforming and Fischer-Tropsch synthesis, require different catalysts, and catalytic reactors are described for each stage. In each case the catalyst may comprise a corrugated foil coated with catalytic material. In each case, the corrugated foils are of height substantially equal to that of the channels: for example the channels might be of width 20 mm and depth 2.5 mm, the foil having corrugations 2.5 mm high.
According to the present invention there is provided a compact catalytic reactor defining a multiplicity of first and second flow channels arranged alternately in the reactor, for carrying first and second fluids, respectively, wherein at least the first fluids undergo a chemical reaction; each first flow channel containing a removable gas-permeable catalyst structure incorporating a metal substrate, the catalyst structure defining a multiplicity of parallel flow paths therethrough; wherein the catalyst structure incorporates a multiplicity of projecting resilient lugs which support the catalyst structure spaced away from at least one adjacent wall of the channel.
Preferably each catalyst structure incorporates resilient lugs projecting in opposite directions, so that the catalyst structure is spaced away from both opposed adjacent walls of the channel. Where chemical reactions are to take place in both the first and second flow channels, then the second flow channels would also contain a removable gas-permeable catalyst structure incorporating such projecting resilient lugs.
The reactor may be made of an aluminium alloy, stainless steel, high-nickel alloys, or other steel alloys, depending on the temperature and pressure required for the reactions, and the nature of the fluids, both reactants and products. The catalyst structures do not provide strength to the reactor, so the reactor itself must be sufficiently strong to resist any pressure forces during operation. It will be appreciated that the reactor may be enclosed within a pressure vessel so as to reduce the pressure forces it experiences, or so that the pressure forces are only compressive.
The reactor must also be provided with headers to supply the fluids to the flow channels, and preferably each first header comprises a chamber attached to the outside of the reactor and communicating with a plurality of the first flow channels, and each second header comprises a chamber attached to the outside of the reactor and communicating with a plurality of the second flow channels, such that after removal of a-header, the corresponding catalyst layers in the flow channels are removable. This ensures that the catalysts can easily be replaced when they become spent.
The catalyst structure preferably incorporates a ceramic coating to carry the catalytic material. Preferably the metal substrate for the catalyst structure is a steel alloy that forms an adherent surface coating of aluminium oxide when heated, for example an aluminium-bearing ferritic steel such as iron with 15% chromium, 4% aluminium, and 0.3% yttrium (e.g. Fecralloy (TM)). When this metal is heated in air it forms an adherent oxide coating of alumina, which protects the alloy against further oxidation and against corrosion. Where the ceramic coating is of alumina, this appears to bond to the oxide coating on the surface. The substrate may be a wire mesh or a felt sheet, but the preferred substrate is a thin metal foil for example of thickness less than 100 μm, and the substrate may be corrugated, pleated or otherwise shaped so as to define the multiplicity of flow paths.
Preferably the substrate of the catalyst structure is a foil corrugated into castellations (rectangular corrugations), and the resilient lugs project above and below the castellations, being integral with the foil and being formed by punching out from the castellated foil. Other shapes of corrugations are also possible.
The metal substrate of the catalyst structure within the flow channels enhances heat transfer within the catalyst structure, preventing hot spots or cold spots, enhances catalyst surface area, and provides mechanical strength. The projecting lugs ensure that the catalyst structure does not become jammed in the channel, for example due to differential thermal expansion, and the lugs also allow for differences in the dimensions of the catalyst structure and the channel that may arise due to manufacturing tolerances. The lugs also allow all the surfaces of the catalyst structure to be effectively contacted by the flowing reactants, as a gap is created between the channel walls and the catalyst structure. The flow paths defined by the catalyst structure may have any suitable cross-sectional shape, but would typically be rectangular; and by virtue of the gaps between projecting lugs adjacent flow paths along the outside of the catalyst structure communicate with each other. Preferably all the surfaces forming the catalyst structure incorporate catalytic material.
Where the channel depth is no more than about 3 mm, then the catalyst structure may for example be a single shaped foil. Alternatively, and particularly where the channel depth is greater than about 2 mm, the catalyst structure may comprise a plurality of such shaped foils separated by substantially flat foils; the shaped foils and flat foils may be linked to each other, for example by similar projecting lugs locating in corresponding slots, or alternatively may be inserted as separate items. To ensure the required good thermal contact, for example with a Fischer-Tropsch reactor, the channels are preferably less than 20 mm deep, and more preferably less than 10 mm deep, and for a steam/methane reforming reactor the channels are preferably less than 5 mm deep. But the channels are preferably at least 1 mm deep, or it becomes difficult to insert the catalyst structures, and engineering tolerances become more critical. Desirably the temperature within the channels is maintained uniformly across the channel width, within about 2-4° C., and this is more difficult to achieve the larger the channel becomes.
The reactor may comprise a stack of plates. For example, first and second flow channels may be defined by grooves in respective plates, the plates being stacked and then bonded together. Alternatively the flow channels may be defined by thin metal sheets that are castellated and stacked alternately with flat sheets; the edges of the flow channels may be defined by sealing strips. The stack of plates forming the reactor is bonded together for example by diffusion bonding, brazing, or hot isostatic pressing.
Hence a plant for processing natural gas to obtain longer chain hydrocarbons may incorporate a steam/methane reforming reactor of the invention, to react methane with steam to form synthesis gas, and a Fischer-Tropsch reactor of the invention to generate longer-chain hydrocarbons.

The invention will now be further and more particularly described, by way of example only, and with reference to the accompanying drawings, in which:

FIG. 1 shows a sectional view of part of a compact catalytic reactor;

FIG. 2 shows a catalyst carrier for use in the reactor of FIG. 1;

FIG. 3 shows a sectional view of the catalyst carrier of FIG. 2, on the line 3-3 of FIG. 2.

The invention is applicable to a wide range of different chemical reactions, particularly those involving gaseous reactants and requiring a catalyst. For example it would be applicable in a chemical process for converting natural gas (primarily methane) to longer chain hydrocarbons. This can be achieved by a two-stage process, and each stage might use a reactor of the invention. The first stage is steam reforming, in which steam is mixed with natural gas and heated to an elevated temperature (so as to reach say 800° C.) so that reforming occurs:
H₂O+CH₄→CO+3 H₂
This reaction is endothermic, and may be catalysed by a rhodium or platinum/rhodium catalyst in a flow channel. The heat required to cause this reaction may be provided by combustion of an inflammable gas such as methane or hydrogen, which is exothermic and may be catalysed by a-platinum/palladium catalyst in an adjacent second gas flow channel.
The gas mixture produced by the steam/methane reforming is then used to perform a Fischer-Tropsch synthesis to generate a longer chain hydrocarbon, that is to say:
n CO+2n H₂→(CH₂)_n+H₂O
which is an exothermic reaction, occurring at an elevated temperature, typically between 190° C. and 280° C., and an elevated pressure typically between 1.5 MPa and 2.5 MPa (absolute values), in the presence of a catalyst such as iron, cobalt or fused magnetite. The preferred catalyst for the Fischer-Tropsch synthesis comprises a coating of gamma-alumina of specific surface area 140-230 m²/g with about 10-40% cobalt (by weight compared to the alumina), and with a promoter such as ruthenium, platinum or gadolinium which is less than 10% the weight of the cobalt, and a basicity promoter such as lanthanum oxide.
The stream of high pressure carbon monoxide and hydrogen produced by steam methane reforming is cooled and compressed to the elevated pressure, say 2.0 MPa, and is then fed to a catalytic Fischer-Tropsch reactor, which may be a reactor of the invention; the reactant mixture flows through one set of channels, while a coolant flows through the other set.
The reaction products from the Fischer-Tropsch synthesis, predominantly water and hydrocarbons such as paraffins, are cooled to condense the liquids by passage through a heat exchanger and a cyclone separator followed by a separating chamber in which the three phases water, hydrocarbons and tail gases separate, and the hydrocarbon product is stabilised at atmospheric pressure. The hydrocarbons that remain in the gas phase and excess hydrogen gas (the Fischer-Tropsch tail gases) are collected and split. A proportion may be passed through a pressure reduction valve to provide the fuel for the catalytic combustion process in the reformer (as described above). The remaining tail gases may be fed to a gas turbine arranged to generate electricity. The major plant electrical power needs are the compressors used to raise the pressure to that required for the Fischer-Tropsch reaction; electricity may also be used to operate a vacuum distillation unit to provide process water for steam generation.
Referring now to FIG. 1 there is shown a reactor block 10 suitable for use as a steam reforming reactor, with the components separated for clarity. The reactor block 10 consists of a stack of plates that are rectangular in plan view, each plate being of corrosion resistant high-temperature steel such as Inconel 800HT or Haynes HR-120. Flat plates 12 of thickness 1 mm are arranged alternately with castellated plates 14, 15 in which the castellations are such as to define straight-through channels 16, 17 from one side of the plate to the other. The castellated plates 14 and 15 are arranged in the stack alternately, so the channels 16, 17 are oriented in orthogonal directions in alternate castellated plates 14, 15. The thickness of the castellated plates 14 and 15 (typically in the range between 0.2 and 3.5 mm) is in each case 0.75 mm. The height of the castellations (typically in the range 2-10 mm) is 3 mm in this example, and solid edge strips 18 of the same thickness are provided along the sides. In the castellated plates 15 which define the combustion channels 17 the wavelength of the castellations is such that successive ligaments are 25 mm apart, while in the castellated plates 14 which define the reforming channels 16 successive ligaments are 15 mm apart.
A reactor block similar to that of FIG. 1 would also be suitable for use as a Fischer-Tropsch reactor, in this case defining channels for a coolant fluid alternating with channels for the Fischer-Tropsch synthesis. The channels for coolant might for example be 2 mm high (typically in the range 1 to 4 mm) and channels for the Fischer-Tropsch synthesis might be of height 5 mm (typically in the range 3 to 10 mm). In this case the reactor does not operate at such a high-temperature, so the structural components may be of aluminium alloy, for example 3003 grade (aluminium with about 1.2% manganese and 0.1% copper).
In either case the stack is assembled as described above, and bonded together, for example by brazing or hot isostatic pressing. Catalyst carriers 20 (only two are shown) are then inserted into the channels in which reactions are to occur, carrying appropriate catalysts. Appropriate headers can then be attached to the outside of the stack. Each catalyst carrier 20 incorporates a metal foil substrate which assists in dissipating heat uniformly across the surface of the catalyst to reduce or eliminate the development of hot spots, and also provides structural integrity to the catalyst. However it has now been appreciated that in many cases heat conduction from the catalyst to the channel walls is not critical; in the case of the combustion and reforming reactions, this is because heat transfer between the catalyst carrier 20 and the walls of the channel occurs primarily through convection and radiation; and in the case of the Fischer-Tropsch reaction the bulk of the heat transfer occurs through convection between the catalyst carrier 20 and the walls of the channel.
Referring now to FIG. 2, in which the channel walls are shown only by broken lines, each catalyst carrier 20 comprises a 50 μm thick Fecralloy foil corrugated into a castellated shape (with rectangular corrugations), the total height of the corrugations being 1 mm less than the height of the channel. The foil is coated with a ceramic coating (not shown separately in the figures) such as alumina of thickness typically in the range 30-80 μm (for combustion or steam reforming), and the active catalytic material (such as platinum/rhodium, in the case of steam reforming) is incorporated into the ceramic. Resilient lugs 22 are also stamped out from the foil during the corrugation process, these being for example of width 0.5 mm and length 1.5 mm, remaining integral with the foil at one end, and projecting above or below the corrugations. These may for example be provided at 25 mm spacings along the length of the foil, and may (as shown) be provided in every corrugation, or at any rate at least once every two or three corrugations across the width of the foil.
As shown in FIG. 3, the lugs 22 projecting above and below the catalyst carrier 20 are at substantially the same positions along the length of the catalyst carrier 20, and when the catalyst carrier 20 is inserted into the channel the lugs 22 are compressed and pushed into a sloping position. The catalyst carrier 20 is therefore supported resiliently by the lugs 22.
It will be appreciated that the resilience of the lugs 22 can accommodate for any differential thermal expansion of the reactor block and the catalyst carriers 20, and for any bowing of the channel as a result of thermal stress, and also allows for any discrepancy between the height of the catalyst carrier 20 and that of the corresponding channel (as can arise as a result of manufacturing tolerances). However, the lugs 22 require that the catalyst carriers 20 are both installed and removed in the direction of the arrow A in FIG. 3, so that removable headers must be provided at both ends of each channel.
It will be appreciated that the corrugations might have a different shape to that shown here; they may for example have a different ratio of height to width of each corrugation from that shown, for example being square rather than rectangular corrugations. Furthermore the corrugations might be a different shape altogether, for example the vertical parts of the corrugations shown in FIG. 2 might instead be inclined to form a zigzag shape with flat tops; yet again the corrugations might instead be arcuate or sinusoidal. The lugs might be spaced differently from those described above and might be of a different shape or size. There might be lugs on only one side of the catalyst insert, instead of lugs being provided on both the opposed surfaces.
It will also be appreciated that in some cases, for example with a channel that is of height above about 4 mm, it is appropriate to use an assembly of corrugated catalyst carriers separated by substantially flat foils which may also be catalyst carriers. For example in a 6 mm channel there might be two corrugated foil catalyst carriers each of height 2.5 mm, separated by a substantially flat foil. In this case lugs need only be provided on the surfaces of catalyst carriers that are adjacent to a wall of the channel—projecting from the top of the top corrugated foil, and from the bottom of the bottom corrugated foil, in this example. Similar lugs might also be provided for interlocking the foils together, for example lugs projecting from the lower surface of the upper corrugated catalyst carrier and from the upper surface of the lower corrugated catalyst carrier might locate in corresponding slots in the flat foil; such lugs might be inclined in the opposite direction to those adjacent to the channel walls. And alternatively lugs might be provided projecting below and above the flat foil, and locating in corresponding slots in the corrugated foils.
It will be appreciated that this catalyst structure, because it is spaced apart from the wall by the lugs 22, provides an increased cross-sectional area for fluid flow, reducing the local gas velocity and the pressure drop across the reactor block.

Claims

1-10. (canceled)

11. A compact catalytic reactor defining a multiplicity of first and second flow channels arranged alternately in said reactor, for carrying first and second fluids, respectively, wherein at least said first fluids undergo a chemical reaction; wherein each first flow channel contains a removable gas-permeable catalyst structure incorporating a metal foil substrate, said catalyst structure defining flow paths therethrough; wherein said substrate comprises a stack of spaced-apart foils; wherein said catalyst structure incorporates a multiplicity of resilient strips which are bent out from the foil substrate so as to project from the substrate and to support said catalyst structure resiliently spaced away from at least one adjacent wall of said channel, each strip being connected to said catalyst structure only at an end or ends of said strip, and being integral with said foil; and

wherein said catalyst structure, excluding said projecting strips, is of height less than a corresponding height of said channel by between 0.1 mm and about 1 mm.

12. A catalytic reactor as claimed in claim 11 wherein chemical reactions occur in both said first and said second flow channels, and wherein second flow channels contain removable gas-permeable catalyst structures that incorporate a metal foil substrate, and which define flow paths therethrough, wherein said catalyst structure incorporates a multiplicity of projecting resilient strips which support said catalyst structure spaced away from at least one adjacent wall of said channel, each strip being connected to said catalyst structure only at ends of said strip, and being integral with said foil.

13. A catalytic reactor as claimed in claim 11 wherein said catalyst structure comprises resilient strips projecting in opposite directions, so that said catalyst structure is spaced away from both opposed adjacent walls of said channel.

14. A catalytic reactor as claimed in claim 11 wherein said resilient strips comprise projecting lugs, attached to said foil at one end.

15. A catalytic reactor as claimed in claim 11 wherein said resilient strips comprise projecting curves, each being attached to said foil at both ends.

16. A catalytic reactor as claimed in claim 11 wherein the said substrate comprises a stack of spaced-apart foils in which at least some of the foils in the stack are spaced apart by resilient strips which are bent out from the foil substrate so as to project from the substrate.

17. A catalytic reactor as claimed in claim 11 wherein said first fluids undergo steam reforming.

18. A catalytic reactor as claimed in claim 11 wherein said first fluids undergo Fischer-Tropsch synthesis.

19. A plant for processing natural gas for obtaining longer chain hydrocarbons, said plant comprising:

a first reactor as defined by claim 11, wherein said first fluids undergo steam reforming, for reacting methane with steam for forming synthesis gas, and

a second reactor as defined by claim 11, wherein the second reactor is configured to be fed a stream from the first reactor;

wherein said first fluids undergo Fischer-Tropsch synthesis for generating longer-chain hydrocarbons;

wherein the first reactor is a reforming reactor; and

wherein the second reactor is a synthesis reactor.

20. A compact catalytic reactor defining a multiplicity of first and second flow channels arranged alternately in the reactor, for carrying first and second fluids, respectively, wherein at least said first fluids undergo a chemical reaction; wherein each first flow channel contains a removable gas-permeable catalyst structure incorporating a metal foil substrate, said catalyst structure defining flow paths therethrough; wherein said substrate comprises a stack of spaced-apart foils; wherein said catalyst structure incorporates a multiplicity of resilient strips which are bent out from the foil substrate so as to project from the substrate and to support said catalyst structure resiliently spaced away from at least one adjacent wall of said channel, each strip being connected to the catalyst structure only at an end or ends of the strip, and being integral with a said foil.

21. A compact catalytic reactor as claimed in claim 20 wherein the said substrate comprises a stack of spaced-apart foils in which at least some of the foils in the stack are spaced apart by resilient strips which are bent out from the foil substrate so as to project from the substrate.

22. A compact catalytic reactor as claimed in claim 21 wherein adjacent foils in the stack are spaced apart by resilient strips which are bent out from each adjacent foil, wherein said adjacent foils are secured to each other by means that interlock said resilient strips bent out from the adjacent foils.