Catalytically heated fuel processor with replaceable structured supports bearing catalyst for fuel cell

Abstract

A highly compact heat integrated fuel processor, which can be used for the production of hydrogen from a fuel source, suitable to feed a fuel cell, is described. The fuel processor assembly comprises a catalytic reforming zone (29) and a catalytic combustion zone (28), separated by a wall (27). Catalyst able to induce the reforming reactions is placed in the reforming zone and catalyst able to induce the combustion reaction is placed in the combustion zone, both in the form of coating on a suitable structured substrate, in the form of a metal monolith. Fe—Cr—Al—Y steel foils, in corrugated form so as to enhance the available area for reaction, can be used as suitable substrates. The reforming and the combustion zones can be either in rectangular shape, forming a stack with alternating combustion/reforming zones or in cylindrical shape forming annular sections with alternating combustion/reforming zones, in close contact to each other. The close placement of the combustion and reforming catalyst facilitate efficient heat transfer through the wall which separates the reforming and combustion chambers.

Claims

1. A reformer for the production of hydrogen from a fuel source, the reformer comprising: a reforming zone configured to receive at least fuel from a source and produce a reformate containing primarily hydrogen and receiving heat from a combustion zone, the reforming zone disposed annularly about the combustion zone and separated by a wall; the combustion zone being configured to receive fuel for combustion from same or separate source as the reforming zone and provide heat to the reformer, wherein the combustion zone includes a tapped tube disposed centrally, wherein the tapped tube includes an open end and a closed end, the closed end configured to reduce a cross sectional flow of the fuel for combustion; the combustion zone having a structured catalyst support coated with a combustion catalyst able to induce fuel combustion reactions; and the reforming zone of the separating wall containing a reforming catalyst able to induce fuel reforming reactions, in the form of a thin film coated on fecralloy sheets.

2. The reformer of claim 1, wherein the structured catalyst support of the combustion and the reforming zones is made of corrugated fecralloy sheets.

3. The reformer of claim 2, wherein the corrugated fecralloy sheets of the combustion zone are coated with a high surface area alumina film containing a dispersed metal phase of palladium or platinum metal and mixtures thereof, or of base metals.

4. The reformer of claim 2, wherein the corrugated fecralloy sheets of the reforming zone are coated with a high surface area alumina film containing a dispersed metal phase of ruthenium, nickel, platinum, rhodium or mixtures thereof.

5. The reformer of claim 1 wherein the fecralloy sheets in the reforming zone are corrugated.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1A is a perspective view of the combustion zone of one embodiment of the invention of the heat integrated reformer with catalytic combustion, which is of the plate type.

(2) FIG. 1B is a perspective view of the reforming zone of one embodiment of the invention of the heat integrated reformer with catalytic combustion, which is of the plate type.

(3) FIG. 1C is a perspective view of another embodiment of the invention of the heat integrated reformer with catalytic combustion, which is of the cylindrical type.

(4) FIG. 1D is another perspective view of one embodiment of the invention of the heat integrated reforming reformer with catalytic combustion, which is of the cylindrical type

(5) FIG. 2A is a perspective view of one embodiment of the invention of the heat integrated reforming reactor with catalytic combustion, comprising of multiple concentric cylindrical sections.

(6) FIG. 2B is a perspective view of another embodiment of the invention of the heat integrated reforming reactor with catalytic combustion, comprising of multiple concentric cylindrical sections.

(7) FIG. 2C is a perspective view of another embodiment of the invention of the heat integrated reforming reactor with catalytic combustion, comprising of a stack of multiple rectangular plates.

DETAILED DESCRIPTION

(8) Although the present disclosure will be described in terms of specific embodiments, it will be readily apparent to those skilled in this art that various modifications, rearrangements, and substitutions may be made without departing from the spirit of the present disclosure.

(9) The present invention is described in detail with reference to a few preferred embodiments illustrated in the accompanying drawings. The description presents numerous specific details included to provide a thorough understanding of the present invention. It will be apparent, however, to one skilled in the art that the present invention can be practiced without some or all of these specific details. On the other hand, well known process steps, procedures and structures are not described in detail as to not unnecessarily obscure the present invention.

(10) FIG. 1A illustrates the “S” shape flow passage of the combustion zone of a plate-type reformer according to one embodiment of the present invention. The combustion flow passage assembly includes a plate 10 that separates the combustion zone 11 from the reforming zone. The steel strips 12 placed suitably in the perimeter of the rectangular plate restrict flow to the desired direction and act as the reactor wall. A fuel and air mixture 13 is supplied through flow passage 14. The flow passage contains a structured combustion catalyst. An example of a structured catalyst is a fecralloy sheet, preferably corrugated, which is coated with a combustion catalyst 15 that induces the desired reaction in the combustor feed. The suitably positioned baffles 16 drive the combustion flow to form an “S” shape. The flue gases 17 exit the tubular section through flow passage 18. The combustion catalyst could be Pt or Pd and combinations thereof or base metals and base metal oxides.

(11) FIG. 1B illustrates the reforming flow passage according to the same embodiment of the present invention. The flow passage assembly includes a plate 10 (of FIG. 1A) that separates the combustion zone 11 (of FIG. 1A) from the reforming zone 20. The steel strips 21 placed suitably in parallel with the rectangular plate, restrict flow to the desired direction and act as the reactor wall. A fuel and steam mixture 22 is supplied through flow passage 23. The flow passage contains a structured reforming catalyst. An example of a structured catalyst is a fecralloy sheet, preferably corrugated, which is coated with a reforming catalyst 24 that induces the desired reaction in the combustor feed. Suitable reforming catalysts include but are not limited to nickel, ruthenium, precious metals and combinations thereof. The reforming products 25 exit the tubular section through flow passage 26.

(12) The fuel to the combustor can be any available and suitable fuel. Such fuels include methane, natural gas, propane, butane, liquefied petroleum gas, biogas, methanol, ethanol, higher alcohols, ethers, gasoline, diesel etc. For the embodiment illustrated in FIGS. 1A and 1B, the fuels normally available in liquid form must be vaporized before entering the combustion zone. The same fuels can be fed to the reforming zone to undergo the hydrogen producing reforming reactions. Another potential fuel to the combustor is the hydrogen depleted off-gas from the anode of a fuel cell when the reformer is used as a part of a fuel processor producing hydrogen for a fuel cell, or the hydrogen depleted gas from hydrogen separation membrane or the hydrogen depleted gas from a Pressure Swing Adsorption (PSA) unit.

(13) The composition of the gas mixture entering the combustor should be such as to ensure complete combustion of the fuel. Although a stoichiometric ratio of air to fuel is sufficient, higher ratios can be employed with the present invention. The composition of the mixture entering the reforming section of the assembly is determined by the stoichiometries of the reforming reactions for the given fuel. It is typical practice to provide a higher than stoichiometric steam-to-fuel ratio to minimize possible side reactions that can cause shoot or carbon formation to the detriment of the catalyst and/or the reactor. All suitable steam-to-carbon ratios in the range from 1 to 25 can be employed with the present invention.

(14) The structured combustion catalyst can preferably be in the form of a corrugated metal foil made of a high temperature resistant metal or metal alloy. A metal alloy such as an alloy with the formula FeCrAlY, commonly referred as fecralloy, can be used for high temperature combustion catalyst support. The wall 10 can be constructed from any material, but materials that offer low resistance to heat transfer such as metals and metallic alloys are preferred. In this configuration, heat is generated by combustion in the catalytic chamber and is transported very easily and efficiently though the wall 10 to the reforming chamber where the heat demanding reforming reactions take place. Heat is generated where it is needed and does not have to overcome significant heat transfer resistances to reach the demand location resulting in high efficiencies. The presence of a catalyst and lower temperatures permit significantly higher space velocities to be used compared to flame based reformers. Space velocity is defined as the ratio of the feed flow at standard conditions to the empty volume of the reactor. For the catalyst section of the heat integrated reformer space velocities of 1000 to 100000 hr.sup.−1, more preferably 5000-50000 hr.sup.−1 and even more preferably 10000 to 30000 hr.sup.−1 can be used. In flame based reformers space velocities are typically below 2000 hr.sup.1.

(15) The catalyst on the reforming side can be a structured catalyst, in which case high space velocities can be used, preferably 10,000-100,000 hr.sup.−1 or, more preferably, 7,500-15,000 hr.sup.−1.

(16) The suitable combustion and the reforming catalysts can be prepared by coating a relatively thin (5-1000 μm thick) catalytic film on the fecralloy sheets. Suitable catalysts typically consist of a support and one or multiple metal phases dispersed on the support. The support is typically a metal oxide that may contain oxides of one or multiple elements from the IA, IIA, IIIA, IIIB and IVB groups of the periodic table of elements. The most typical combustion catalysts support is aluminum oxide. The dispersed metal phase may contain one or multiple elements from the IB, IIB, VIB, VIIB and VIII groups of the periodic table of elements. One method to prepare the catalytic film that ensures good adhesion to the fecralloy is to heat the fecralloy sheet to elevated temperatures in air. During the heating, aluminum, which is a component of the fecralloy, is diffusing out of the bulk of the alloy and forms an aluminum oxide surface layer. Upon this surface layer it is easy to coat alumina or other metal oxide supports for the desired dispersed metal phase which may be a precious or non-precious metal. Typical supports for reforming and combustion catalysts consist of oxides of aluminum, silicon, lanthanum, cerium, zirconium, calcium, potassium and sodium. The metal phase of reforming catalysts may contain nickel, cobalt, copper, platinum, rhodium and ruthenium. The metal phase of the combustion catalyst may contain platinum, palladium, rhodium nickel or any other metal that is active in catalytic combustion.

(17) Coating of the catalysts support on the fecralloy sheets can be accomplished by many techniques. After heating up so as to form the aluminum oxide layer at the surface, techniques such as dip coating from a solution of dispersed metal oxide particles or from a slurry which contains the metal oxide particles can be employed. Alternatively, catalyst can be deposited on the fecralloy sheets by spraying the catalytic components onto their surface, or by plasma deposition, etc. The catalyst support is then dried by calcination at elevated temperatures. The dispersed metal phase can be added to the support forming solution or slurry of the metal oxide particles or it can be added in a separate step from a solution of the desirable metal salt after the calcination step.

(18) The temperatures and pressures of the two streams entering the combustion zone and the reforming zone, respectively, need not to be the same. Typically, combustion takes place at low or near-atmospheric pressure, although high pressure combustion is practiced. Reforming can take place at pressures somewhat above atmospheric up to 30 barg. The wall of the flow passages should be of sufficient strength to allow for the pressure differential between the two streams.

(19) The major advantage of the present invention is the heat integration between the combustion 11 and the reforming 20 zones. Combustion takes place on the catalytic film which is coated on the structured catalyst 15 placed on one side of the plate 10 separating the two zones. The heat that is generated on the combustion side is quickly transferred and used on the reforming side. This rapid heat transfer is critical in maintaining the combustion side catalyst at temperatures below 1200 C and more preferably below 1000 C. These temperatures ensure acceptable catalyst life and permit the use of a very compact combustion zone which allows the reactor assembly to be dramatically smaller compared with a flame based reformer which needs to maintain a significant distance between the flame generation and the reforming sections. The lower temperatures also allow the use of less expensive alloys for the construction of the reactor. The lower temperatures also mean that there are no nitrogen oxide emissions as their formation require much higher temperatures.

(20) FIG. 1C illustrates a lateral cross-section of an integrated reformer according to another embodiment of the present invention. The integrated combustor/steam reformer assembly includes a tubular section defined by a cylindrical wall 27 which separates the combustion zone 28 from the reforming zone 29. The assembly housing 30 acts as the reactor wall and define an axially extending concentric annular passage in heat transfer relation with the tubular section. In the center of the combustion zone a tapped tube 31 is inserted so as to reduce the combustion flow cross section area.

(21) FIG. 1D illustrates an axial cross section of the same integrated reformer as illustrated in FIG. 1C. The integrated combustor/steam reformer assembly includes a tubular section defined by a cylindrical wall 27 that separates the combustion zone 28 from the reforming zone 29. The assembly housing 30 acts as the reactor wall and defines an axially extending concentric annular passage in heat transfer relation with the tubular section. In the center of the combustion zone a tapped tube 31 is inserted so as to reduce the combustion flow cross section area.

(22) A fuel and air mixture 32 is supplied to the tubular section through flow passage 33. In this embodiment the flow passage of the tubular section contains the combustion catalyst 34 deposited on a corrugated fecralloy sheet that induces the desired reaction in the combustor feed. Similarly, the outside of the tubular section contains fecralloy sheets coated with reforming catalyst 35 that induces the desired reaction in the reformer feed. The products of the combustion reactions 36 exit the tubular section through flow passage 37. A fuel and steam mixture 38 is supplied to the annular passage through flow passage 39 counter-current or co-current to the combustion gases. The products of the reforming reactions 40 exit the annular passage through flow passage 41.

(23) The reactor assembly includes a flow distributor 16 as to allow for uniform feeding of the annular combustion zone 28. The flow distributor consists of a cylindrical cross section 42 and multiple perforated sheets 43 placed against the combustion feed flow passage. The perforated steel sheet 43 has holes of 0.5-1 mm diameter with a density of 20-50 holes per cm2 and subsequently a flow area which is 5-20% of the flow area of the cylindrical cross section 42. Due to the pressure drop created on the perforated sheet, the flow of the gas is distributed evenly in the cylindrical cross section 42. In a way, the holes of the perforated sheet act as spraying nozzles and the flow distributor as a static mixer with a pressure drop of 15-250 mbar, which is much lower than the commonly used static mixers. The size and the density of the perforated sheet holes as well as the distance between the perforated sheets is of critical importance and depends on various reformer sizing parameters such as capacity, type of fuel, desired pressure drop etc. The preferable distance between perforated sheets is 15-50 mm.

(24) FIG. 2A and FIG. 2B illustrate one embodiment of a complete heat integrated reforming reactor, which is of the cylindrical form. The reactor consist of multiple cylindrical cross sections 44 placed concentrically forming combustion flow passages 45 in contact with reforming flow passages 46. Reforming flow passages communicate through radially placed cylindrical channels 47. A fuel and air mixture 48 is supplied to the annular sections through flow passage 45. The combustion flow passages 45 contain the combustion catalyst 50 deposited on a corrugated fecralloy sheet that induces the desired reaction in the combustion zone. Similarly, the reforming flow passages 46 contain fecralloy sheets coated with reforming catalyst 51 that induces the desired reaction in the reforming zone. The products of the combustion reactions 52 exit the reactor through flow passage 49. A fuel and steam mixture 53 is supplied to the annular passages through flow passage 46 and cylindrical channels 47 counter-current or co-current to the combustion gases. The products of the reforming reactions 54 exit the annular passage through radial channels 47 and flow passage 46.

(25) This embodiment may contain also a flow distributor for uniform feeding of the combustion flow passage as described in FIG. 1D.

(26) FIG. 2C illustrates another embodiment of a complete heat integrated reforming reactor with catalytic combustion, which is of the plate form. The reactor consists of multiple rectangular steel sheets 55 placed one on top of the other forming combustion flow passages 56 in contact with reforming flow passages 57. Reforming flow is restricted in reforming flow passage with steel rectangular strips 58 placed accordingly. Combustion flow is restricted in combustion flow passage with steel rectangular strips 59 placed accordingly. Combustion flow may have an “S” type flow shape as briefly described in FIG. 1A. A fuel and air mixture 60 is supplied to the combustion passage 56. The combustion flow passages 56 contain the combustion catalyst 62 deposited on a corrugated fecralloy sheet that induces the desired reaction in the combustor feed. Similarly, the reforming flow passages 57 contain fecralloy sheets coated with reforming catalyst 63 that induces the desired reaction in the reformer feed. The products of the combustion reaction 64 exit the reactor through rectangular combustion flow passages 56. A fuel and steam mixture 65 is supplied to the reforming catalyst 63 through reforming flow passages 57 and cross flow to the combustion gases. The products of the reforming reactions 66 exit the reactor through reforming passage 57.

(27) The heat integrated reforming reactor configurations described above offer several advantages over the conventional flame-based reforming reactors. The catalytic combustion takes place at lower temperatures, which permits close coupling of the combustion and reforming zones. In a flame based reformer, the flame must be at a significant distance from the tube containing the reforming catalyst to prevent the tube from melting. As a result, the integrated reforming reactor is several times smaller than a flame-based reforming reactor and, consequently, has a much lower capital and installation cost. The flame-based reformers can consist of hundreds of tubes and burners and a sophisticated feed flow distribution system is required to distribute the combustion feed and reforming feed to all burners and tubes evenly. The heat integrated reformer has a single inlet for the reforming and single inlet for the combustion feed gases which results in simple and inexpensive feed flow system. The flame reformers, even with the use of low NOx burners, still produce significant quantities of NOx in the combustion gases, which have to be controlled with a separate selective catalytic reduction (SCR) catalyst and ammonia injection. The heat integrated reformer described within operates at low temperatures on the combustion side at which NOx formation is negligible.

(28) The fuel feed to the reformer can be natural gas, liquefied petroleum gas (LPG), propane, naphtha, diesel, ethanol or other biofuels, or combinations of these fuels.

(29) While this invention has been described in terms of several preferred embodiments, there are alterations, permutations and equivalents that fall within the scope of the present invention and have been omitted for brevity. It is therefore intended that the scope of the present invention should be determined with reference to appended claims.