Purified hydrogen is an important fuel source for many energy conversion devices. For example, fuel cells use purified hydrogen and an oxidant to produce an electrical potential. A process known as steam reforming produces by chemical reaction hydrogen and certain byproducts or impurities.

A subsequent purification process removes the undesirable impurities to provide hydrogen sufficiently purified for application to a fuel cell.

Under steam reforming, one reacts steam and alcohol, (methanol or ethanol) or a hydrocarbon (such as methane or gasoline or propane), over a catalyst. Steam reforming requires elevated temperature, e. g., between 250 degrees centigrade and 800 degrees centigrade, and produces primarily hydrogen and carbon dioxide. Some trace quantities of unreacted reactants and trace quantities of byproducts such as carbon monoxide also result from steam reforming.

Trace quantities of carbon monoxide, certain concentrations of carbon dioxide, and in some cases unsaturated hydrocarbons and alcohols will poison a fuel cell. Carbon monoxide adsorbs onto the platinum catalyst of the fuel cell and inhibits operation of the fuel cell, i. e., reduces the power output of the fuel cell. To a lesser degree, carbon dioxide and other unsaturated hydrocarbons and alcohols have the same result. All impurities to some extent reduce by dilution the partial pressure of hydrogen in the fuel cell and increase the mass transfer resistance for hydrogen to diffuse to the platinum catalyst, and thereby reduce power output of the fuel cell. Thus, fuel cells require an appropriate fuel input, i. e., purified hydrogen with no additional elements contributing to a loss in fuel cell efficiency.

Traditionally, hydrogen purification attempts to always maximize harvest of hydrogen from the reforming process. To maximize the amount of hydrogen obtained, a relatively expensive device, e. g., a thick and high quality palladium membrane, serves as a hydrogen-permeable and hydrogen-selective membrane Ledjeff-Hey, K., V. Formanski, Th. Kalk, and J. Roes,"Compact Hydrogen Production Systems for Solid Polymer Fuel Cells"presented at the Fifth Grove Fuel Cell Symposium, September 22-25,1997]. Such thick, high quality palladium alloy membranes support maximum harvest of hydrogen with minimal, i. e., acceptable, impurities for use in a fuel cell. Such high level of purification, however, requires significant investment in the thick, high quality palladium membrane.

Traditionally, the process of steam reforming and the subsequent process of hydrogen purification occur in separate apparatus. The advantages of combining steam reforming and hydrogen purification in a single device are known [Oertel, M., et al,"Steam Reforming of Natural Gas with Integrated Hydrogen Separation for Hydrogen Production", Chem. Eng. Technol 10 (1987) 248-255; Marianowski, L. G., and D. K. Fleming,"Hydrogen Forming Rection Process"US Patent No. 4,810,485, March 7,1989]. An integrated steam reforming and hydrogen purification device should provide a more compact device operating at lower temperatures not limited by the normal equilibrium limitations. Unfortunately, such a device has yet to be reduced to practical design. Where theory in this art recognizes the advantage of combining steam reformation and hydrogen purification in a single device, the art has yet to present a practical, i. e., economical, design.

Thus, a practical integrated steam reforming and hydrogen purification device has not yet become available. The subject matter of the present invention provides a practical combined steam reforming and hydrogen purification device.

Summary of the Invention A process for producing hydrogen containing concentrations of carbon monoxide and carbon dioxide below a given level begins by reacting an alcohol vapor (such as methanol) or a hydrocarbon vapor (such as propane) and steam to produce product hydrogen, carbon monoxide, and carbon dioxide.

The reacting step occurs in the vicinity of, or immediately preceding, a hydrogen-permeable and hydrogen-selective membrane and the product hydrogen permeates the membrane. A methanation catalyst bed lies at the permeate side of the membrane and converts any carbon monoxide and carbon dioxide which passes through the membrane to methane, thereby yielding a product hydrogen stream with concentrations of carbon monoxide and carbon dioxide that are below acceptable thresholds. Optionally, reforming catalyst may also lie at the permeate side of the membrane along with the methanation catalyst to convert to product hydrogen any unreacted alcohol or hydrocarbon feed that passes through the membrane. Product hydrogen is then withdrawn from the methanation catalyst bed.

A steam reformer, also referred to as a fuel processor, according to the present invention includes a reforming bed that receives and reacts a mixture of alcohol or hydrocarbon vapor and steam to produce hydrogen and by product gases. The gases are then passed through a hydrogen-permeable and hydrogen selective membrane. On the permeate side of the membrane, a methanation catalyst converts carbon monoxide and carbon dioxide to methane.

Integrated fuel-cell systems including fuel processors, such the disclosed steam reformers, are also disclosed.

Many other features of the present invention will become manifest to those versed in the art upon making reference to the detailed description which follows and the accompanying drawings in which preferred embodiments incorporating the principles of this invention are disclosed as illustrative examples only.

Brief Description of the Drawings For a better understanding of the invention, and to show how the same may be carried into effect, reference will now be made, by way of example, to the accompanying drawings in which: Fig. 1 illustrates generally an energy conversion system including a fuel cell and a steam reformer with internal hydrogen purification according to one form of the present invention.

Fig. 2 illustrates schematically a concentric, cylindrical architecture for the steam reformer with internal hydrogen purification of Fig.

1.

Fig. 3 illustrates in cross section the steam reformer with internal hydrogen purification of Fig. 1.

Fig. 4 illustrates schematically an alternate architecture for the steam reformer under the present invention nesting multiple reformer tubes within a common combustion region.

Fig. 5 illustrates schematically and partially in cross section a steam reformer with internal hydrogen purification according to the present invention including a modified combustion system distributed within the reformation region.

Fig. 6 illustrates schematically and partially in cross section another embodiment of a steam reformer with internal hydrogen purification according to the present invention including an isolated vaporization chamber.

Fig. 7 illustrates schematically a combustion system applicable to the present invention and providing along its length a generally uniform temperature gradient.

Fig. 8 illustrates the temperature gradient of the combustion system of Fig. 7 as compared to a conventional temperature gradient.

Fig. 9 illustrates another form of steam reformer with internal hydrogen purification under the present invention using plate membrane elements.

Fig. 10 illustrates in exploded view a plate membrane module of the steam reformer of Fig. 9 including membrane envelope plates.

Fig. 11 illustrates in exploded view a membrane envelope plate of Fig. 10.

Figs. 12-17 show membrane components for a tubular metal membrane module and assembly steps in the production of a tubular membrane module using manufacturing steps according to the present invention.

Fig. 18 illustrates in perspective, and partially broken away, another embodiment of a steam reformer according to the present invention including an isolated vaporization chamber and a plate-form membrane module.

Fig. 19 illustrates the steam reformer of Fig. 18 in section.

Figs. 20 and 21 show components of the membrane module for the steam reformer of Figs. 18 and 19.

Fig. 22 illustrates a component stack for the membrane module of the steam reformer of Figs. 18 and 19 providing a series feed gas flow arrangement.

Fig. 23 illustrates a component stack for the membrane module of the steam reformer of Figs. 18 and 19 providing a parallel feed gas flow arrangement.

Fig. 24 illustrates a component stack for the membrane module of the steam reformer of Figs. 18 and 19 incorporating an exhaust plate for internal heating of the membrane module.

Fig. 25 illustrates in cross section another embodiment of a steam reformer according to the present invention.

Fig. 26 illustrates in cross section a variation of the reformer of Fig. 25.

Fig. 27 is a process flow diagram of a fuel-cell system in which propane or natural gas is used as the fuel to heat the fuel processor during a cold start-up.

Fig. 28 is a process flow diagram of a fuel-cell system in which a liquid fuel is used to heat the fuel processor during a cold start-up.

Fig. 29 is an embodiment of the invention in which stored hydrogen is used to heat the fuel processor during a cold start-up.

Fig. 30 is a process flow diagram of a fuel-cell system in which hydrogen purged from the anode chamber of the fuel cell is combusted to provide additional water for recovery and use.

Fig. 31 is a process flow diagram of a fuel cell system in which hydrogen purged from the anode chamber of the fuel cell is combusted to provide additional heat and water for recovery and use.

Fig. 32 is an embodiment of the invention in which high-grade heat is recovered from the fuel processor.

Fig. 33 shows another embodiment of the invention comprising a dual pump head in which a single motor is used to simultaneously drive two pump heads that deliver both the feedstock and water to the fuel processor.

Fig. 34 shows yet another embodiment of the invention adapted to preheat either the feedstock or feed water prior to delivery to the fuel processor by heat exchange with hot hydrogen exiting the fuel processor.

Fig. 35 shows yet another embodiment of the invention comprising one or more ion-exchange beds to maintain low electrical conductivity of the process water.

Fig. 36 shows a process flow diagram for a fuel cell system in which ion exchange and activated carbon beds are used to purify feed water prior to injection into the fuel processor.

Detailed Description of the Invention Fig. 1 shows an energy conversion system 10 employing a steam reformer with internal hydrogen purification (reformer) 12 according to a preferred form of the present invention. Reformer 12 provides at its outlet 14 purified hydrogen to a PEM fuel cell 16. Fuel cell 16 receives at its inlet 18 an oxidant from oxidant source 20. Fuel cell 16 produces an electrical potential 22 for application to an electrical load 24, e. g., an electrical motor. Fuel cell 16 also includes outlets 26 and 28 serving as fuel and oxidant outlets, respectively.

For purposes of describing operation of reformer 12, the liquid feedstock will be methanol (MeOH) and water, although other alcohols or hydrocarbons may be used in place of methanol. Reformer 12 receives at its fuel inlet 30 pressurized liquid methanol and water from a pressurized methanol/water source 32. As described more fully hereafter, the pressurized mix of liquid methanol and water vaporizes within reformer 12 and reacts with a reforming catalyst to produce a hydrogen stream and a byproduct stream. A hydrogen-selective membrane separates the hydrogen stream from the byproduct stream. The hydrogen stream passes, by pressure differential, through the membrane and subsequently through a polishing catalyst to appear at the outlet 14 of reformer 12.

While traditional reforming technology allows a high percentage of hydrogen produced to be taken across a selective membrane, the process and apparatus of the present invention takes less than a maximum available amount of hydrogen across the selective membrane. The present invention thereby allows use of a lesser-grade and, therefore, less expensive selective membrane.

In addition, because less than the maximum amount of hydrogen is separated as a product stream, the required membrane area is reduced under this aspect of the present invention. The remaining portion of hydrogen enters the byproduct stream, mixes with air provided at inlet 34 by air blower 36, and reacts with a combustion catalyst within reformer 12 to support elevated temperatures needed for steam reforming within reformer 12. Reformer 12 thereby uses the byproduct stream, including a selected amount of hydrogen remaining therein, as a fuel source for its combustion process. No additional fuel source is applied to reformer 12 to support combustion. Reformer 12 also includes a plurality of combustion exhaust ports 38 releasing combustion byproducts.

The optimum amount of hydrogen to recover as a product stream is calculated from the heating value (enthalpy of combustion) of hydrogen.

Sufficient hydrogen must be supplied in the byproduct stream to the catalytic combustion region so that the heat of combustion exceeds the total heat

requirement of the reformer. The total heat requirement of the reformer (A Total) is given by AHtota) = AHrxn + AHp + AHp + AHbss where AHm, is the enthalpy of the reforming reactions; AHVap is the enthalpy of vaporization of the liquid feed stock; AHCp is the enthalpy required to heat the vaporized feed stock to the reforming temperature; and AH, oss is the heat lost to the surrounding environment. Heat loss from the reformer is minimized (and reduced to a negligible degree) with adequate insulation.

In the case of steam reforming methanol according to the following reaction stoichiometry CH30H + H20 = C02 + 3H2 where 8.4 gmole methanol and 8.4 gmole water are required to yield sufficient hydrogen (21 std. ft3) to generate about 1 kWe. Assuming no heat loss and no heat exchange (between discharged hot streams and the relatively cold feed stock stream) AH,,,., is 300 kcal. Since the heat of combustion for hydrogen is 57.8 kcal/gmole, approximately 5.2 gmoles of hydrogen (4.3 std. ft3) must be combusted to provide the required 300 kcal of heat for steam reforming sufficient methanol to generate lkWe. So, 70% to 80% of the hydrogen produced in the reformer is recovered as a product stream and the remaining 20% to 30% of the hydrogen is passed to the catalytic combustor in the byproduct stream to provide a fuel stream with sufficient heating value to meet the heating requirements (AHtot,) of the reformer.

Fig. 2 illustrates schematically the concentric cylindrical architecture of steam reformer 12. In Fig. 2, reformer 12 includes in concentric relation an outermost metal tube 50, an inner metal tube 52, a hydrogen- selective membrane tube 54, and an innermost metal tube 56. Tubes 50,52,54, and 56 are of successively smaller diameter and arranged in concentric relation to one another. An annular combustion region 60 exists in the space within tube 50 but external of tube 52. An annular reforming region 62 exists within

tube 52 but external of membrane tube 54. An annular hydrogen transport region 64 exists within membrane tube 54, but external of tube 56. A cylindrical polishing region 66 resides within the metal tube 56.

Fig. 3 illustrates in cross section the steam reformer 12. In Fig. 3, outermost metal tube 50, a generally closed-end tubular structure, receives at one end via inlet 34 an air supply and releases at combustion ports 38 combustion byproducts. Within combustion region 60, a combustion catalyst 100 resides near air inlet 34. Alternatively, combustion catalyst 100 may be arranged as a plurality of bands spaced at intervals within combustion region 60. Suitable combustion catalyst materials include platinum supported on alumina or other inert and thermally-stable ceramic. Inlet 30, carrying the pressurized mix of methanol and water, passes through the end wall 50a of tube 50 and forms a coil 30a wrapping about the innermost metal tube 56 within the combustion region 60, although metal tube 56 need not necessarily pass through the axis of coil 30a. The distal end of coil 30a passes through the closed end 52a of tube 52 and opens into the reforming region 62. The pressurized mix of liquid methanol and water entering coil 30a vaporizes at the elevated temperatures of combustion region 60 and enters the reforming region 62 as vapor.

Within reforming region 62 a reforming catalyst 102 (e. g., BASF catalyst K3-110 or ICI catalyst 52-8) reacts with the vaporized mix of methanol and water to produce hydrogen in the vicinity of the membrane tube 54.

Membrane tube 54 is composed of one of a variety of hydrogen-permeable and hydrogen-selective materials including ceramics, carbon, and metals.

Especially preferred materials for fabricating said membrane tube 54 are hydrogen-permeable palladium alloys, e. g., palladium alloyed with 35-45 wt% silver. Each end of membrane tube 54 is sealed by a metal cap 104. A metal gauze 106 within the reforming region 62 surrounds each cap 104 and maintains the catalyst 102 within region 62 and in the vicinity of membrane tube 54. A hydrogen stream 103 migrates by pressure differential through

membrane tube 54 and into hydrogen transport region 64. A thin membrane tube 54 requires support against deformation under the pressure differential between reforming region 62 and hydrogen transport region 64. For this purpose, a tension spring 101 supports membrane tube 54 from within while allowing hydrogen stream 103 to pass by, into and along transport region 64.

Because a thin palladium alloy membrane may be used under the present invention, special construction methods have been developed under the present invention to make use of a delicate structure such as thin membrane tube 54. Under conventional practice, a thick palladium alloy membrane can be brazed because it can withstand the high temperatures and liquid phase aspects of brazing.

A thin palladium alloy membrane, as proposed herein however, cannot be brazed under conventional methods because the elevated temperature and liquid brazing alloy destroy such thin palladium material. A thin membrane tube 54 could, under conventional practice for example, attach to end caps 104 and establish a gas-tight seal by use of gaskets and suitable support structures. As discussed more fully hereafter, under the present invention a thin palladium alloy membrane, e. g., tube 54, attaches to end caps 104 by first attaching a foil (not shown in Fig. 3), e. g., a copper or nickel foil, to the ends of tube 54 by ultrasonic welding and then brazing the foil-wrapped ends of tube 54 to end caps 104.

Hydrogen stream 103 travels within transport region 64 toward and into the open end 56a of tube 56. Hydrogen stream 103 includes some impurities, e. g., carbon monoxide, carbon dioxide and unreacted methanol and water vapor, also traveling along transport region 64 and into innermost tube 56 at its open end 56a. All of hydrogen stream 103 enters the open end 56a of innermost tube 56.

Within tube 56 a polishing catalyst 110 reacts with impurities in the hydrogen stream 103 passing therethrough. Metal gauze 112 downstream from catalyst 110 holds catalyst 110 within tube 56. Polishing catalyst 110 (e. g., BASF catalyst G1-80 or ICI catalyst 23-1) reacts with certain impurities remaining in hydrogen stream 103, e. g., as much as 1% of carbon monoxide

and carbon dioxide, and converts such impurities to innocuous byproducts, e. g., methane. Stream 103 of purified hydrogen and, now innocuous, byproducts passes through metal gauze 112 and exits reformer 12 at the outlet 14, i. e., at the opposite end 56b of tube 56.

Polishing catalyst 110 may be several separate catalysts within tube 56. In order to deal with carbon monoxide and carbon dioxide impurities, one uses a methanation catalyst. The process of methanation, i. e., reacting carbon monoxide or carbon dioxide with hydrogen to yield methane as shown below, is well known.

C02+ 4H2= CH4+ 2H20 CO+3H2=CH4+H20 Methanation provides an acceptable polishing step because methane is considered relatively inert or innocuous to the fuel cell 16 (Fig. 1) whereas carbon dioxide and carbon monoxide are poisonous to the fuel cell.

If reformer 12 uses methanol in the steam reforming step, and leaks in the membrane tube 54 allow carbon monoxide and carbon dioxide to pass into the hydrogen stream 103, some unreacted methanol and water vapor may exist in the hydrogen stream 103. To convert such unreacted methanol into a harmless byproduct prior to entering the fuel cell 16 (Fig. 1), a reforming catalyst which is a low temperature copper/zinc shift catalyst, is placed through a portion (e. g., one-fourth to one-third) of the polishing catalyst bed, i. e., innermost tube 56, followed downstream by a methanation catalyst.

The predominant chemical reaction for steam reforming methanol is shown below.

CH30H+H20 = C02+ 3H2 Returning to reforming region 62, steam reforming byproduct stream 105 moves toward closed end 52b of tube 52 and through critical orifice 120 serving as an outlet for tube 52 and discharging near air inlet 34.

Optionally, deflector 57 directs the flow of byproduct stream 105 and air from inlet 34 toward combustion catalyst 100. Byproduct stream 105 thereby

encounters and mixes with the air inflow 107 of air at inlet 34. Air inflow 107 may be preheated to enhance the catalytic ignition within combustion region 60. For example, an air heater 37 (Fig. 1) may be provided in series along the inlet 34 to reformer 12. Alternatively, inlet 34 may be routed through combustion region 60 as shown schematically in Fig. 3. The resulting mixture travels toward and through combustion catalyst 100 and ignites thereat. The combustion byproducts then travel through combustion region 60 and eventually, after heating coil 30a and thermally supporting the steam reforming process within region 62, exit reformer 12 at the combustion exhaust ports 38.

Reformer 12 operates at a relatively lower temperature than conventional steam reforming devices. Because reformer 12 continually purifies hydrogen as it is produced, the steam reforming reaction may be conducted well away from its equilibrium limitation. Although equilibrium limitations are generally not important in the case of steam reforming methanol, they are very important in the case of steam reforming methane (natural gas).

Unreacted reactants in the relatively lower temperature reforming process tend to be eventually reacted due to the continuous siphoning of hydrogen from the process. Under the present invention, the steam reforming process may be operated at approximately 250 to 600 degrees Celsius. For methanol reforming the operating temperature of the reformer would be approximately 250 to 300 degrees Celsius.

To create an appropriate pressure differential at membrane tube 54, the liquid methanol and water should be pumped, i. e., provided by source 32, at approximately 6 to 20 atmospheres. The polishing step should be conducted at approximately one to three atmospheres within polishing region 66. The pressure within hydrogen transport region 64 is essentially equal to the pressure within polishing region 66. The reforming process should be operated at 6 to 20 atmospheres to provide a substantial pressure differential across membrane tube 54. Critical flow orifice 120 can be sized to provide a pressure drop from the reforming region 62 (6 to 20 atmospheres) to one atmosphere

within the combustion region 60. The byproduct stream 105 thereby enters the combustion region 60 at approximately one atmosphere. This allows operation of the air supply at inlet 34 at approximately one atmosphere, and thereby allows use of an inexpensive air blower 36.

Dimensions for reformer 12 sufficient to feed a typical fuel cell 16 are relatively small. Ten liters per minute (21 cubic feet per hour) of hydrogen is sufficient to generate one kilowatt of electrical energy in fuel cell 16. A steam reformer 12 under the present invention sufficient to support a one kilowatt fuel cell 16 would be roughly three inches in diameter by 15 to 16 inches in length. To increase volumetric production, the length of reformer 12 could be increased or the diameter of reformer 12 could be increased. The volumetric production rate for reformer 12 is limited primarily by the area of membrane 56 exposed to the reforming process. Increasing the length of reformer 12 or the diameter of reformer 12 increases the exposed area of membrane tube 54 and thereby increases hydrogen output for reformer 12.

However, multiple standard-sized reformers 12 may be employed in parallel within a common combustion zone.

Fig. 4 illustrates schematically the architecture of an alternate reformer 12'with an enlarged outermost metal tube 50'defining a common combustion region 60'. Within the relatively larger combustion region 60', a plurality of reformer tubes 51, i. e., each a combination of a tube 52, a tube 54, and a tube 56, are arranged in spaced relation. While not shown in Fig. 4 for purposes of clarity, reformer 12'would include a feedstock inlet, a product hydrogen outlet, and a combustion gas outlet. A common air inlet 34 supplies air to the common combustion region 60'. As may be appreciated, each of reformer tubes 51 provides a byproduct stream 105 (not shown in Fig. 4) to the common combustion region 60'.

Returning to Fig. 3, reformer 12 must be initiated to operate.

Generally, the reforming region 62 must be elevated to approximately 150 to 200 degrees Celsius if methanol is the feedstock, or 300 to 500 degrees Celsius

if hydrocarbons are the feedstock. Once the reforming process begins, the byproduct stream 105, including by design a given amount of hydrogen as combustion fuel, enters the combustion region 60, encounters combustion catalyst 100, and combusts to thermally support the steam reforming process.

The combustion catalyst only needs hydrogen present (mixed with air) to ignite the byproduct stream 105. The goal in starting reformer 12, therefore, is to elevate the reforming region 62 to approximately 150 to 200 degrees Celsius (in the case of methanol reforming).

A simple cartridge-type electric resistance heater 140, either inserted into the reforming catalyst 102 or, as illustrated in Fig. 3, into the center of tube 56 initiates operation of reformer 12. Alternatively, a resistance heater may be used to heat the methanol and water feed provided at inlet 30. In either event, once the reforming catalyst 102 reaches a sufficiently high temperature (150 to 200 degrees Celsius) the reforming reaction begins and the combustion catalyst 100 reacts with hydrogen present in byproduct stream 105.

At this point, the electrical resistance heater 140 can be shut down. A 50 to 100 watt resistance heater 140 should be adequate, based on conventional thermal mass calculations, to sufficiently heat the reforming region 62 in a matter of minutes.

Fig. 5 illustrates, partially and in cross section, an alternate form of the present invention with its combustion system distributed through the reformation region to improve heat transfer from the combustion process to the reformation process. In Fig. 5, reformer 212 is a steam reformer with internal hydrogen purification receiving at its inlet 230 a feed stock, e. g., methanol and water, and providing at its outlet 214 purified hydrogen for application to, for example, a fuel cell (not shown in Fig. 5). As with earlier embodiments of the present invention, reformer 212 leaves a selected portion of hydrogen in its byproduct stream to support the combustion process. Combustion byproducts exit at the exhaust port 238.

Reformer 212 includes an outer metal tube 252 sealed at each end by end plates 253, individually 253a and 253b and gaskets 255, individually 255a and 255b. Bolts 257 secure end plates 253 against the shoulders 252, individually, 252a and 252b, at each end of tube 252. A hydrogen purification module lies within and generally concentric to tube 252 and includes a thin palladium alloy membrane tube 254 sealed by end caps 304a and 304b. Alternatively, membrane tube 254 may be comprised of hydrogen-selective and hydrogen-permeable materials other than palladium alloys, including porous carbon, porous ceramics, hydrogen-permeable metals other than palladium, porous metals, and metal-coated porous carbon and porous ceramics and porous metals. As may be appreciated, tube 254 and caps 304 may be supported in some fashion (not shown) within tube 252. End cap 304b communicates with outlet 214 through plate 253b and the product hydrogen stream 303 emerges from outlet port 214. A polishing catalyst bed, preferably a methanation catalyst, is located at the permeate side of membrane tube 254 (not shown) as discussed earlier and shown in Fig. 3.

Inlet 230 passes through wall 253a and couples to a vaporization coil 230a. Outlet 231 of coil 230a feeds directly into the reformation region 262 defined as being within tube 252 but external of tube 254. Also located within and distributed throughout the reformation region 262 is a combustion coil 250. In the particular embodiment illustrated, coil 250 surrounds in spiral fashion membrane tube 254 and extends substantially throughout the entire reformation region 262. A combustion catalyst 302 lies within and either along the length of coil 250 or localized within coil 250 at or near end 250a. End 250a of coil 250 receives a fuel stock, as described more fully hereafter, and combustion occurs within coil 250 as the fuel stock travels along coil 250 and encounters the combustion catalyst 302 therein. Because coil 250 extends uniformly throughout the reformation region 262 and because coil 250 provides significant surface area, rapid and well distributed heat transfer occurs from the combustion process occurring within coil 250 to the surrounding reformation region 262.

Reformation region 262 couples through wall 253b at its outlet 220 to a conduit 221. Conduit 221 carries the byproduct stream 205, i. e., the byproduct of hydrogen reformation including a selected amount of hydrogen intentionally not taken across the membrane tube 254, to the combustion process. Conduit 221 delivers byproduct stream 205 to a pressure let down valve 223. Byproduct stream 205 then continues, at lowered pressure, into an intake manifold 207. Manifold 207 includes an air inlet 209, e. g., coupled to an air blower or to discharged air from the cathode component of the fuel cell (not shown in Fig. 5), and air passage way 211 carrying combustion air to a mixing region 213 at or near the inlet 250a of combustion coil 250. The combustion fuel stock as provided by the byproduct stream 205, thereby mixes with the incoming combustion air in mixing region 213 and enters end 250a of combustion coil 250. Combustion catalyst 302 within coil 250 ignites the fuel stream 205 and heat transfers efficiently and rapidly in well distributed fashion into and throughout the reformation region 262.

While a coil or spiral form of combustion system has been illustrated, i. e., the coil 250, other shapes may be employed as a combustion system within the reformation region 262. For example, generally tubular structures may assume a variety of forms for distribution throughout reformation region 262. As discussed more fully hereafter, a counter-current combustion system as illustrated in Fig. 7 establishes improved, i. e., uniform, heat distribution throughout reformation region 262. Thus, the advantage of distributing a combustion system throughout the reformation region 262 may be achieved in a variety of specific configurations.

In steam reformer 12 (Fig. 3), the combustion process occurred in a region surrounding the reformation region, i. e., externally of the tube 52 (Fig. 3) thereby requiring heat transfer into and across metal tube 52. From the inner surface of tube 52, heat transfer then occurred by migration across the reformation region. In steam reformer 212, however, heat generated within and distributed throughout the reformation region 262, i. e., within the coil 250, better transfers more rapidly throughout the reformation region 262. In essence, the combustion

process has been brought into and distributed throughout the reformation region 262. Heat transfer improves because the flow of reformation gasses passes directly over and around coil 250. Generally, coil 250 provides significantly greater surface area for heat transfer between combustion and reformation as compared to the surface area provided by tube 52 in reformer 12. Heat energy need not transfer into and migrate across the reformation region, but rather generates within the reformation region and radiates outward throughout the reformation region.

Fig. 6 illustrates another embodiment of the present invention, also distributing combustion heat energy throughout the reformation region, but further providing the advantage of isolating the vaporization process from the reformation process. Generally, a preferred temperature for vaporization of the feed stock, e. g., 400-650 degrees Centigrade, is greater than a preferred temperature, e. g., 250-500 degrees Centigrade, for hydrogen reformation. In Fig. 6, steam reformer 312 includes an outer metal tube 352 defining therein a reformation region 362. Tube 352 includes shoulders 352 at each end, individually 352a and 352b. A vaporization module 340 attaches to shoulders 352a of tube 352. Module 340 defines a vaporization chamber 342 isolated relative to reformation region 362.

More particularly, module 340 includes a generally cylindrical barrel 344 having an open end 344a and a closed end 344b. An end plate 346 and gasket 348 seal vaporization chamber 342, i. e., close the otherwise open end 344a of barrel 344.

The closed end 344b of barrel 344 couples to shoulders 352a of tube 352. In this manner, closed end 344b together with a gasket 350 seal the end of tube 352 and, thereby, seal reformation chamber 362. By isolating vaporization chamber 342 and reformation chamber 362, vaporization occurs at preferred, i. e., significantly higher, temperatures than temperatures preferred for reformation chamber 362.

Inlet 330 passes through end plate 346 and feeds into coil 230a as located within vaporization chamber 342. The distal end of coil 230a then passes through closed end 344b of barrel 344 and feeds into reformation chamber 362. In this manner, vaporized feed stock, i. e., methanol and water vapor, enter region 362 and chemically interact with reformation catalyst 400 distributed throughout

reformation region 362.

Vaporization chamber 342 includes outlets passing combustion exhaust along corresponding conduits 370 extending through combustion region 362. In this manner, the heat energy of the combustion exhaust transfers through conduits 370 and into the reformation region 362. Again, distributing heat energy throughout and within the reformation region improves heat transfer distribution and rate. For example, vaporization chamber 342 includes outlets 342a and 342b passing combustion gas into corresponding conduits 370a and 370b. The combustion exhaust remains isolated relative to the combustion region 362, but the heat energy of the combustion exhaust migrates through conduits 370 and into the combustion region 362. Conduits 370 pass through an end plate 353b, secured to shoulders 352b, and the combustion exhaust releases to atmosphere. Heat transfer can be improved, and the degree of resistance to flow and turbulence along the exterior conduits 370 can be controlled by use of baffles 371.

As in previously described embodiments, reformation occurring in reformation region 362 supports migration of hydrogen across a tubular palladium alloy membrane 354. Other hydrogen-permeable and hydrogen-selective compositions that may be used in place of palladium alloys for membrane 354 include porous carbon, porous ceramic, hydrogen-permeable metals, porous metals, and metal-coated porous ceramics and porous carbon and porous metal. Tubular membrane 354, sealed at each end by means of end caps 304, feeds the product hydrogen stream 303 at the outlet 314 of reformer 312. A polishing catalyst bed (not shown) is located at the permeate side of membrane 354 as shown in Fig. 3. A preferred polishing catalyst is a methanation catalyst.

By intentionally not recovering all hydrogen available in the reformation region 362, the remaining hydrogen sweeps away in the byproduct stream 305 and provides a fuel stock for the vaporization module 340. More particularly, reformation region 362 couples to a conduit 321 passing through end plate 353b. Conduit 321 carries the byproduct stream 305, including a selected amount of hydrogen remaining therein as fuel stock. Conduit 321 passes through a

pressure let down valve 323 and provides the reduced-pressure fuel stock flow 305' to an inlet manifold 307. Inlet manifold 307 operates in similar fashion to the inlet manifold 207 of Fig. 5, i. e., receiving combustion air and promoting mixing of the combustion air and reduced-pressure byproduct stream 305'. As the combined combustion air and stream 305'intermix at the mixing region 313, an igniter 319 triggers combustion thereof. Igniter 319 may be a variety of devices, e. g., glow plug, spark plug, catalyst, and the like. In the preferred form of the reformer 312, however, a high voltage spark ignition or possibly a glow plug is considered preferred as igniter 319 for long term reliability and ease of replacement.

In addition to isolation of vaporization, reformer 312 also provides the advantage of a preferred low pressure drop between the initiation of combustion and exhaust from the combustion region. The architecture of reformer 312 provides a lower pressure combustion process because conduits 370 are generally straight conduits offering reduced and controlled resistance to the flow of combustion exhaust gasses. With a lower pressure combustion process, combustion air, e. g., such as is provided at inlet 309 of intake manifold 307, may be provided by a relatively lower pressure and relatively less expensive air blower (not shown in Fig. 6).

Fig. 7 illustrates schematically an alternate combustion system applicable to the various embodiments of the present invention. In Fig. 7, a double- walled counter current combustor 450 includes an inlet manifold 452 receiving a byproduct stream 421 and an air stream 423. Byproduct stream 421 is taken from a reformation process as a byproduct, but includes a selected amount of hydrogen intentionally left therein as a fuel stock for combustion. Byproduct stream 421 travels along an inner conduit 425 and exits conduit 425 in a mixing region 413.

Air stream 423 travels along manifold 452, generally surrounding and parallel to inner conduit 425 and encounters byproduct stream 421 in mixing region 413.

Mixing region 413 comprises an inner tube 430 carrying therealong the mixture of combustion air, i. e., air stream 423 and fuel gas, i. e., byproduct stream 421. Tube 430 is closed at one end, i. e., end 430a forming a portion of manifold 452. The

open end 430b of tube 430, however, releases mixed fuel gas and combustion air into an outer mixing region 415. Outer mixing region 415 is defined by an outer tube 432. Tube 432 is closed at each of its ends 432a and 432b with manifold 452 passing through end 432a. A combustion catalyst 440 is distributed throughout regions 413 and 415. Alternately, combustion catalyst 440 may be localized within tube 430 at or near mixing region 413.

The highest temperature combustion occurs when the mixture of fuel gas and combustion air first encounter catalyst 440, i. e., at the outlet of manifold 452. As the gas mixture continues along tube 430 and encounters catalyst 440 therealong, continued combustion occurs but generally at progressively lower temperatures. As the gas mixture continues out of tube 430, at its open end 430b, it reverses direction and travels back along tube 432 and encounters more catalyst 400. As a result, heat energy is produced along the length of tubes 430 and 432 and exhaust gasses exit at the exhaust port 435.

Generally, a significant temperature gradient exists along a combustion catalyst bed, the hottest portion being where the fuel gas and combustion air first encounter the combustion catalyst or igniter device. Such significant temperature gradient can be undesirable, especially when applying the heat energy to a reformation process most desirably conducted at uniform temperature throughout. Under the present invention, combustor 450 provides a more uniform temperature gradient along its length as compared to a conventional combustion bed. The hottest gasses within combustor 450, i. e., near manifold 452, release heat energy through tube 430 and into the coolest gasses within combustor 450, i. e., near exhaust port 435. By thermally coupling the hottest portion of the gasses with the coolest portion of the gasses a more uniform overall temperature gradient exists along combustor 450.

Fig. 8 illustrates a relationship between the length L of a combustion bed (x axis) and temperature T therealong (y axis). Curve 460 in Fig. 8 illustrates substantially higher temperatures at the beginning of a conventional combustion bed and a significant drop in temperature throughout the conventional combustion

bed. Curve 462, however, illustrates the more uniform, i. e., more flat, temperature gradient obtained by use of combustor device 450. More particularly, a shallow and fairly level curve 462 indicates a uniform temperature along the length of combustor 450. Accordingly, combustor 450 provides a more uniform dispersal of heat energy into a reformation region.

While illustrated as a generally straight device in Fig. 7, it will be understood that the double-walled architecture of the combustion device 450 may be formed in alternate shapes, e. g., spiral, and applied to the various embodiments of the present invention as a combustion system.

In addition to alternate combustion and vaporization features, alternative methods of hydrogen purification may be employed in a steam reformer under the present invention. In addition to tubular and concentric-tubular architectures, planar membrane structures may also be employed in a steam reformer with internal hydrogen purification.

Fig. 9 illustrates schematically a further embodiment of a steam reformer with internal hydrogen purification according to the present invention and using planar membrane structures. In Fig. 9, reformer 512 includes an outer metal tube 550 having shoulders 550a and 550b at each open end thereof. Within tube 550, a metal reforming catalyst tube 552 and a metal polishing catalyst tube 556 lie in generally parallel relation along the length of tube 550. As may be appreciated, however, a variety of geometric configurations and relationships between tubes 552 and 556 may be employed. Reforming catalyst tube 552 contains a reforming catalyst 502 and establishes a reformation region 562. Similarly, polishing catalyst tube 556 contains a polishing catalyst 504 and establishes a polishing region 564.

An end plate 590 and gasket 592 couple to shoulder 550a and seal tube 550. Inlet port 530 carries a liquid feed stock, e. g., methanol and water, through end plate 590 and into vaporization coil 530a. In the particular embodiment illustrated, coil 530 wraps about one end of tube 552 and sits near the combustion exhaust port 538 provided in end plate 590. Vaporization coil 530a couples to end 552a of tube 552 whereby vaporized feed stock exits coil 530a and enters reformation region 562.

A plate membrane module 554 couples to shoulder 550b and seals end 550b of tube 550 to complete a combustion region 560 within tube 550, but external of tubes 552 and 556. Plate membrane module 554 couples to tube 552 to receive a reformate-rich gas flow 501, couples to conduit 529 to provide a product or hydrogen stream 503, and couples to conduit 521 to provide a byproduct stream 505 as fuel stock to support combustion in region 560. More than one tube 552 may be used. Byproduct stream 505, as in earlier-described embodiments of the present invention, intentionally includes a given amount of hydrogen not taken from the reformation process and applied to the combustion process. Conduit 521 carries byproduct stream 505 from plate membrane module 554 through a pressure let down valve 523 and into combustion region 560 at the inlet port 525 thereof.

Adjacent fuel inlet port 525, an air inlet port 528 admits air, e. g., forced by blower (not shown), into combustion region 560. Alternatively, a manifold, as in earlier- described embodiments of the present invention, may be used to admit air and byproduct stream 505 into combustion region 560. As the byproduct stream 505 enters region 560, and intermixes with the combustion air at port 528, it continues past an igniter 575. Igniter 575 initiates combustion of the mixture of byproduct stream 505 and combustion air thereby supporting a combustion process within combustion region 560. As may be appreciated, heat developed in this combustion process supports vaporization of feed stock in the vaporization coil 530a and thereby provides vaporized gasses to the reformation region 562. Heat from combustion in region 560 also serves to directly heat the reforming region 562 and to heat the polishing region 564.

Conduit 529 carries the product (hydrogen) stream 503 into end 556b of polishing catalyst tube 556. More than one conduit 529 and more than one tube 556 may be used. Product stream 503 passes through the polishing region 564, where undesirable elements are neutralized, and the final purified hydrogen product passes from the end 556a of tube 556 and out the outlet port 514. For example, when the polishing catalyst 504 is a methanation catalyst, carbon monoxide and carbon dioxide present in product stream 503 are converted to

methane as described previously.

Fig. 10 illustrates in exploded view the plate membrane module 554 and its relationship to tube 552 and to conduits 521 and 529. Plate membrane module 554 includes end plates 554a and 554b. A series of membrane envelope plates 590 stack between end plates 554. In the particular embodiment of the invention illustrated in Fig. 10, three such membrane envelope plates 590, individually 590a-590c, stack between end plates 554. End plates 554a and 554b and membrane envelope plates 590 are all generally rectangular and have corresponding dimensions. Other geometries, such as circular, may be used rather than the rectangular geometry shown. In other words, plates 554a-554b and 590a- 590c stack like a deck of cards and couple together, e. g. by brazing, to form module 554. End plate 554b is a solid planar structure. End plate 554a, however, includes inlet and outlet ports for coupling to other portions of reformer 512. In particular, reformation catalyst tube 552 couples to a reformate-rich inlet port 592a to receive the products of reformation, i. e., to receive the reformate rich flow 501. Conduit 521 couples to a reformate-depleted outlet port 594a to take from module 554 the byproduct stream 505. In the particular embodiment illustrated, module 554 has two product outlet ports, individually 596a and 598a, providing product stream 503. However, only one product outlet port may be used in some embodiments.

Conduit 529, shown twice in Fig. 10, couples to ports 596a and 598a to collect the product stream 503 therefrom. All of the ports 592a, 594a, 596a, and 598a, need not be located on end plate 554a. Rather, one or more of the ports may be located on end plate 554b as desired or necessary in a particular configuration.

Each membrane envelope plate 590 includes ports positioned in locations corresponding to ports 592a, 594a, 596a, and 598a of end plate 554a.

When stacked and operating as the plate membrane module 554, these various ports align and provide conduits to and from the filtration process executed by module 554. Each of plates 590a-590c include a product port 598, individually 598b-598d. Ports 598a-598d align and cooperate to provide a conduit for product stream 503 out of module 554 and into conduit 529. As will be explained more

fully hereafter, the product, i. e., hydrogen, enters ports 598b-598d laterally within the corresponding membrane envelope plate 590. Each of membrane envelope plates 590a-590c include also a port 596, individually 596b-596d, aligned with outlet port 596a of end plate 554a. Ports 596a-596d also carry product stream 503 away from plate membrane envelopes 590 and into conduit 529. As with ports 598b-598d, ports 596b-596d receive the hydrogen stream 503 laterally from within the corresponding membrane envelope plate 590.

Ports 592b-592d align with port 592a of end plate 554 and thereby provide a conduit for introduction of the hydrogen-rich reformate flow 501 from tube 552 and into membrane envelope plates 590. Each of plates 590a-590c include a byproduct port 594b-594d. Ports 594b-594d align with port 594a of end plate 554a to provide a conduit for the byproduct stream 505 away from membrane envelope plates 590. Forcing the hydrogen-rich reformate flow 501 into port 592a produces the byproduct flow 505 at port 594a for application to the combustion process within combustion region 560 and produces the product stream 503 for application to the polishing region 564.

Each of the membrane envelope plates 590 itself includes a stack of individual plate elements. Fig. 11 illustrates in exploded view the set of plate elements found in each of the membrane envelope plates 590. In Fig. 11, each of the plate elements include ports establishing communication through the membrane envelope 590 as described above in connection with Fig. 10. Some of these ports, however, are"open"laterally into the corresponding plate element and thereby provide lateral access to portions of module 554.

Each membrane envelope plate 590 includes a left spacer plate 600 and right spacer plate 602 as the outer most plates in the stack. Generally, each of spacer plates 600 and 602 are"frame"structures defining an inner open region 604.

Each inner open region 604 couples laterally to ports 592 and 594. Port 592 thereby admits flow 501 into open region 604 and port 594 thereby carries byproduct stream 505 out of open region 604. Ports 596 and 598, however, are closed relative to open region 604 thereby isolating the product stream 503.

Each membrane envelope plate 590 also includes a left membrane plate 606 and a right membrane plate 608, each adjacent and interior to a corresponding one of plates 600 and 602. Membrane plates 606 and 608 each include as a central portion thereof a palladium alloy membrane 610 secured to an outer metal frame 607. In plates 606 and 608, all of the ports 592,594,596, and 598 are closed relative to the palladium alloy membrane 610. Each palladium alloy membrane 610 lies adjacent to a corresponding one of open regions 604, i. e., adjacent to the hydrogen-rich reformate flow 501 arriving by way of port 592. This provides opportunity for hydrogen to pass through the palladium alloy membrane 610 of the adjacent membrane plate 606. The remaining gasses, i. e., the byproduct stream 505, leave open region 604 through port 594.

A screen plate 609 lies intermediate membrane plates 606 and 608, i. e., on the interior or permeate side of each of membranes 610. Screen plate 609 includes an outer frame 611 and carries in a central region thereof a screen 612.

Ports 592 and 594 are closed relative to the central region of screen plate 609, thereby isolating the byproduct stream 505 and the reformate-rich flow 501 from the product stream 503. Ports 596 and 598 are open to the interior region of plate screen 609 carrying screen 612. Hydrogen, having passed through the adjoining membranes 610, travels along and through screen 612 to the ports 596 and 598 and eventually to conduit 529 as the product stream 503.

As the hydrogen-rich reformate flow 501 enters port 592a and forces its flow against membranes 610, hydrogen passes therethrough as the product stream 503 and along ports 596 and 598. The byproduct stream 505 diverts at the membranes 610 and travels along port 594 to conduit 521.

A variety of methods, including brazing, gasketing, and welding, may be used, individually or in combination, to achieve gas-tight seals between plates 600,602,606,608, and 609, as well as between membrane envelopes 590 a- c.

Screen 612 not only provides a flow path for the product flow 503, but also bears the pressure differential applied to membranes 610 to force

hydrogen, i. e., product stream 503, across membranes 610. While illustrated only as a screen structure in Fig. 11, it will be understood that a variety of structures may be used within an open region of screen plate 609 to provide the support function against pressure applied to membranes 610 and to provide a flow path for product stream 503. To the extent that palladium alloy membranes 610 are better supported by an appropriate structure, e. g., screen 612, thinner and less expensive palladium alloy membranes 610 may be employed. Alternative materials to screen 612 include porous ceramics, porous carbon, porous metal, ceramic foam carbon foam, and metal foam.

As discussed throughout this specification, use of thm, less expensive palladium alloy membranes significantly reduces the cost of a steam reformer under the present invention. While it is recognized that use of such thin palladium alloy membranes will result in some contaminants passing into the product stream 503, subsequent purification steps may be taken, e. g., such as illustrated in several embodiments of the present invention.

Manufacturing steps taken in manipulation of the thin palladium alloy membranes, particularly in establishing a gas-tight seal relative to such membranes, must take into account the delicate nature of such thin palladium alloy membranes. In particular, conventional welding or brazing manufacturing steps, i. e., steps including a liquid-phase, cannot by applied to extremely thin (typically <50 microns) palladium alloy membranes. In particular, when liquid phase material contacts the thin palladium alloy membrane it dissolves and melts the membrane and, due to the extremely thin nature of the membrane, cannot serve as an acceptable manufacturing step. There are a variety of ways to establish a gas- tight seal relative to a thin palladium alloy membrane, however, the subject matter of the present invention proposes a particular method of manufacturing to achieve a gas tight seal of a thin palladium alloy membrane without causing significant damage to, i. e., leaks in, the palladium alloy membrane.

Under the present invention, a palladium alloy membrane may be attached and form a gas tight seal relative to an adjoining structure by means of an

intermediate foil attached by ultrasonic welding. The method of manufacture proposed herein may be applied to the tubular form of membrane modules, e. g., such as shown in Fig. 3, or to plate form membrane structures such as shown in Fig. 11. Membrane tube 54 may then be coupled by brazing the foil to end caps 304. In the plate membrane form of the present invention, membranes 610 carrying a foil may be attached by brazing the foil to the surrounding frame 607 of plates 606 and 608. When applied to joining metals, ultrasonic welding strips away and cleans the metal surfaces to such extent that contact between such ultra- clean metals results in joining by solid state intermetallic diffusion. The ultrasonic action scrubbing the mating surfaces of the materials may be done under pressure such as 20 to 60 psi. Once these materials contact, the metal atoms diffuse together and thereby establish a gas tight seal. Important to note, ultrasonic welding does not require a liquid phase and when properly executed does not present opportunity for deterioration of a thin palladium alloy membrane. Because of the relatively low temperature requirements of ultrasonic welding, very little warping of material occurs. Accordingly, ultrasonic welding is particularly well suited for establishing a gas tight seal relative to an ultra thin palladium alloy membrane.

Under the disclosed embodiment of the present invention, ultrasonic welding is used to attach a copper or nickel alloy foil to the surface of the thin palladium alloy membrane. Once this additional copper or nickel alloy layer has been attached it is brazed or welded to an adjoining material, e. g., end caps 304 or frames 607.

Figs. 12-16 show the components and manufacturing steps used in constructing a membrane module, e. g., such as illustrated in Figs. 1,5, and 6 generally described as a tubular palladium alloy structure supported with end caps. Figs. 12 and 13 illustrate a palladium alloy foil 702 and a copper or nickel frame 706 joined, respectively, in preparation for joining by ultrasonic welding as illustrated in Fig. 14. Fig. 15 shows the combined palladium alloy foil and copper or nickel frame assembly 720 rolled into a tubular structure and again joined by ultrasonic welding to maintain the tubular structure. In this

configuration, the end portion of the tubular assembly bears exposed sections of copper or nickel material. The end caps are then brazed directly to this exposed portion of copper or nickel frame to complete the gas-tight structure.

With reference to Figs. 12-16, a tubular hydrogen-permeable metal membrane 700 (Fig. 17) was prepared by the following general method of construction. Both Pd-40Cu and Pd-25Ag foil (nominally 25 micron thick) were used as the hydrogen-permeable membrane 702 (shown individually in Fig. 12). A tension spring 704 (Figs. 15-17), composed of either carbon steel or stainless steel, was used as support within the tubular membrane structure 700.

The first step was to join the palladium-alloy foil 702 to the copper foil frame 706 (nominally 50 microns to 125 microns thick) as shown in Fig. 14. The palladium-alloy foil 702 was typically 8.9 cm wide by 26.4 cm long, and the copper foil frame 706 was typically 10.2 cm wide by 27.9 cm long with a cut out center, equally spaced from all four sides, approximately 7.6 cm wide by 24.1 cm long. This provided a 0.6 cm overlap 710 (Fig. 14) between the palladium-alloy foil 702 and the copper foil frame 706 as foil 702 occupied the cut out center of frame 706.

Ultrasonic welding was used to establish peripheral gas-tight seals 712 between the palladium-alloy foil 702 and the copper foil frame 706 at all four edges of the palladium-alloy foil 702. An Amtech (Shelton, CT) Ultraseam Model 40 welder was used. This welder operates at 40 kHz and delivers up to about 750W of power to the ultrasonic transducer. Both the horn (connected to the ultrasonic transducer) and the anvil rotate at a rate selected by the operator during normal operation of the welder. Welding is accomplished by placing metal between the horn and anvil and applying power to the ultrasonic transducer.

The horn and anvil for the ultrasonic welder are circular, 7.0 cm diameter, with a bearing surface strip about 0.2 cm wide and finished to a surface roughness equivalent to an EDM #3 finish. The horn and anvil were

hard coated with titanium nitride. Typical welding parameters are: 40% full power to the transducer, 40 psig applied pressure between the horn and the anvil, 4 rpm rotation rate for the horn and anvil, and the horn"floating"on the foil pieces to be welded (i. e., no preset separation between the horn and anvil).

To ensure that the metals are bonded during the welding process, the adjoining metal surfaces should be cleaned of residues such as oxidation, grease and oils, dirt, etc. It is also considered beneficial if the palladium-alloy membrane foil 702 and the copper foil frame 706 are annealed prior to welding, since soft metals are more reliably joined by ultrasonic welding than are hard metals.

After welding the palladium-alloy foil 702 to the copper foil frame 706 to establish the membrane assembly 720 as shown in Fig. 14, the welded seals 712 were examined for leaks by a standard dye penetration test. If no leaks were found, membrane assembly 720 was cleaned of excess dye and then wrapped, as illustrated in Fig. 15, lengthwise around a 2.8 cm (outside diameter) tension spring 704,27.9 cm long and made from either stainless steel or carbon steel wire nominally 0.25 cm diameter. The overlap 722 of opposite edges of assembly 720 was then joined by ultrasonic welding to form lap seal 724 along the length of the now tubular structure. Lap seal 724 was established by using the ultrasonic welding parameters specified above. Lap seal 724 was then folded over against the membrane tube to conform to a cylindrical shape.

Copper end caps 730 (Fig. 16) were then fitted to the membrane tube ends and brazed in place at joints 731 (Fig. 17) using standard copper/phosphorous or copper/silver/phosphorous brazing alloys and a hydrogen/air or hydrocarbon/air (e. g., methane, propane, or acetylene) torch. The brazing alloy is applied only to copper end caps 730 and copper foil frame 706. Important to note, establishing braze joints 731 coupling end caps 730 to the cylindrical form of assembly 720 does not expose the delicate palladium alloy membrane foil 702 to liquid phase material, i. e., does not destroy the delicate, thin foil 702.

Because the various ultrasonic welds 712 and 724 establish a gas-tight seal and the braze joints 731 also establish a gas-tight seal, hydrogen passes from a

reformation process external of tube 700 only through foil 702. At least one end cap 730 was fitted with a port 732 and outlet 734 to collect the permeate hydrogen from the inside, or bore, of the membrane tube. Within tube 700, a methanation catalyst 740 may be employed whereby purified hydrogen may be taken from membrane tube 700 as described herein-above. Thus, membranes 700 so constructed are suitable for the high pressure feed gas to be passed over the external surface of the membrane tube, with the permeate collected at the interior surface of the membrane.

Fig. 18 illustrates in perspective and partially broken away, a steam reformer 812 according to another embodiment of the present invention.

Reformer 812 employs an isolated vaporization chamber 820 similar to that of reformer 312 (Fig. 6). More particularly, reformer 812 receives at input conduit 830 a feed stock and conduit 830 delivers this mixture into vaporization chamber 820 at the vaporization coil 830a. Elevated temperatures within chamber 820 vaporize the feed stock provided at input conduit 830. Coil 830a passes into and opens into reformation chamber 862. Vaporized fuel thereby enters the reformation chamber 862. Chamber 862 is filled with a reformation catalyst 863 and steam reformation occurs within steam reformation region 862. A reformation product stream 801 exits reformation region 862 at the outlet conduit 852. Conduit 852 delivers product stream 801 to membrane module 854. Module 854 separates stream 801 into a byproduct stream 805 and a hydrogen-rich stream 803.

The hydrogen-depleted reformate byproduct stream 805 travels along conduit 821 from membrane module 854 to a pressure let down valve 823 (schematically illustrated in Fig. 19) and then to a manifold 807. Manifold 807 operates in similar fashion to manifold 207 of reformer 212 (Fig. 5). More particularly, manifold 807 introduces an air supply taken from inlet 809, e. g., from a forced air supply, and intermixes it with stream 805 at a mixing region 813. An igniter 819 ignites the intermixed air and stream 805 and the resulting combustion elevates temperatures within the vaporization chamber 820. As in

earlier described embodiments of the present invention, stream 805 includes by design a certain amount of hydrogen not taken across the palladium alloy membranes of module 854. Stream 805 thereby serves as a fuel source for combustion within vaporization chamber 820.

Exhaust ports 842 carry the combustion byproducts from chamber 820 through combustion conduits 843 and out exhaust ports 838, shown more clearly in Fig. 19. Conduits 843, however, pass through the reformation chamber 842 and thereby distribute heat throughout reformation region 862 in support of the reformation process therein. Exhaust conduits 843 may take a variety of forms, including finned tubes and spirals, to provide substantial surface area and desirable uniform distribution of heat throughout reformation region 862.

Still referring to Fig. 19, product stream 803 emerging from membrane module 854 travels through a conduit 856 having therein a methanation catalyst 804. Conduit 856 passes through the reformation region 862 and through the vaporization chamber 820 and thereby collects heat energy therefrom in support of the methanation process occurring in conduit 856. The distal end 814 of conduit 856 provides a product outlet, i. e., provides hydrogen in sufficiently purified form for application to, for example, PEM fuel cell 16 (Fig. 1).

Figs. 20 and 21 illustrate a membrane frame and permeate frame, respectively, employed in the membrane module 854 of Figs. 18 and 19. In Fig. 20, the membrane frame 870 includes a circular copper or nickel frame 870a with a rectangular center cut out 870b. A rectangular palladium alloy membrane 870c, oversized relative to center cut out 870b, is joined at seals 870d to the frame 870a. By using ultrasonic welding to establish seals 870d about the periphery of palladium alloy membrane 870c, a gas-tight seal results between membrane 870c and frame 870a. Finally, membrane frame 870 includes a feed manifold aperture 872 and a permeate manifold aperture 874.

In Fig. 21, a permeate frame 876 includes a central cut out 876a.

Cut out 876a includes a first portion generally rectangular and corresponding generally in dimension to membrane 870c. This portion of cut out 876a is occupied by a wire mesh spacer 876b. Other materials that may be used in place of wire mesh spacer 876b include porous and foamed ceramic, porous and foamed carbon, and porous and foamed metal. A second portion of cut out 876a extends peripherally outward to define a permeate manifold 884 and containing therein a wire mesh insert 876c. Frame 876 may be recessed to accommodate face-to-face contact with frame 870, i. e., to accommodate membrane 870c as attached to the face of frame 870b. Finally, permeate frame 876 includes a feed manifold aperture 882.

As may be appreciated, frame 870 and frame 876 correspond in outer dimensions and certain portions align when stacked. For example, feed manifold 872 aligns with feed manifold 882. Also, permeate manifold 874 may be aligned with the substantially larger permeate manifold 884. Thus, when appropriately stacked with other components, described more fully hereafter, a membrane module 854 may be established to separate stream 801 into streams 803 and 805 as described herein-above.

Fig. 22 illustrates use of frames 870 and 876 stacked to form a series flow arrangement for module 854. In Fig. 22, permeate frame 876 occupies a central position with a membrane frame 870 on each side, i. e., above and below as illustrated in Fig. 22. Feed manifold 882 of frame 876 aligns with feed manifolds 872 of frames 870. Permeate manifold 884 of frame 876 aligns with permeate manifolds 874 of frames 870. Feed frames 880 are located at the outward side of each of frames 870, i. e., above and below frames 870 as illustrated in Fig. 22. Each frame 880 is of circular shape corresponding to that of frames 870 and 876. Each frame 880 includes an open central region extending laterally outward to correspond with, i. e., to fluidly couple with, aligned apertures 872 and 882 of frames 870 and 876. Each frame 880 also includes a permeate manifold aperture 887 isolated relative to the center cut out portion.

Thus, the arrangement illustrated in Fig. 22 offers a series flow configuration directing the feed gas sequentially across successive membranes 870c. For example, consider a feed gas traveling upward through the component stack illustrated in Fig. 22. As the feed gas enters the center open region of the lowest frame 880, hydrogen has opportunity to pass through the membrane 870c of the lowest membrane frame 870. As may be appreciated, any such hydrogen which does cross the lowest membrane frame 870 migrates into the open region of permeate frame 876 and can then migrate by way of permeate manifolds 884,874 and 887 out of the component stack for harvest.

The series flow arrangement of Fig. 22 offers a second opportunity for feed gas to pass through a membrane 870c. More particularly, feed gas travels from the open center region of the lowest frame 880 into the feed manifold 872 of the lowest frame 870, through the feed manifold 882 of the permeate frame 876, through the feed manifold 872 of the upper frame 870, and into the central open region of the upper most feed frame 880. In this open central region, the feed gas is exposed to a second palladium alloy membrane. More particularly, hydrogen remaining in the feed gas as it enters the open region of the upper frame 880 is exposed to the membrane 870c of the upper membrane frame 870.

Any such hydrogen crossing this upper membrane 870c enters the central open region of permeate frame 876 and may then travel along manifolds 884,874 and 887 for harvest.

As may be appreciated, additional similar components may be stacked in the arrangement illustrated in Fig. 22 to provide successive opportunity for feed gas exposure to palladium alloy membranes in series fashion. An actual implementation would include end plates and necessary outlet and inlet ports for harvesting hydrogen gas and forcing feed gas into the component stack as described earlier in connection with the plate form membrane module 554.

In such series flow arrangement as illustrated in Fig. 22, the feed gas stream is directed to flow over a first membrane surface, then a second

membrane surface, and so on as desired. Such series flow arrangement encourages mixing of the feed gas stream components after passage over each membrane in the membrane module component stack.

Fig. 23 illustrates a second arrangement for membrane module components providing a parallel flow configuration, i. e., where the feed stock stream divides and has one opportunity for exposure to a palladium alloy membrane. In Fig. 23, permeate frames 870'correspond generally to the previously described permeate frames 870, but include also a raffinate manifold 875. Similarly, permeate frame 876'corresponds to the previously described permeate frame 876, but includes also a raffinate manifold 885. Raffinate manifolds 885 and 875 align for fluid communication therebetween when frames 870'and 876'stack as illustrated in Fig. 23.

The arrangement illustrated in Fig. 23 establishes a parallel flow of feed gas across the palladium alloy membranes 870c. More particularly, consider a feed gas entering the open central region of the lower feed frame 880. Such feed gas is exposed to the membrane 870c of the lower frame 870'.

Concurrently, some of the feed gas may divert across the lower membrane 870c and then travel along the raffinate channels established by apertures 875 and 885, or along the apertures 872 and 882 and eventually enter the open region of the upper feed frame 880. At this point, the feed gas is exposed to the membrane 870c of the upper frame 870'. Accordingly, hydrogen present therein may migrate across membrane 870c and into the center open region of permeate frame 876'. Thereafter, such hydrogen would pass along manifolds 884 of frame 876'and 874 of frames 870'and eventually through apertures 887 for harvest. In such parallel flow configuration, all of the feed channels over the membrane surfaces are fed from a common feed supply manifold. This favors low pressure drop for the flowing feed gas stream.

The arrangement of membrane component stacking as illustrated in Figs. 22 and 23 allows series or parallel, respectively, flow of the feed gas through the membrane module. Because the feed frames 880 are compatible, it

is possible to combine series flow and parallel flow stacking arrangements in a single membrane module. More particularly, an arrangement such as illustrated in Fig. 22 may be stacked adjacent to an arrangement as illustrated in Fig. 23.

Multiple combinations of such arrangements may be provided in a single membrane module as desired to establish a given first-stage of the hydrogen purifier as illustrated in the present invention.

Fig. 24 illustrates an additional frame component which may be incorporated into a membrane module. In Fig. 24, exhaust frame 890 includes a feed manifold aperture 892, a permeate manifold 894, and a raffinate manifold 895. As may be appreciated, stacking exhaust frame 890 in a membrane module such as illustrated in Figs. 22 and 23 allows passage of feed gas through aperture 892, hydrogen product through aperture 894, and passage of raffinate through aperture 895 without otherwise affecting operation of the membrane modules as described herein above. Exhaust frame 890 includes also an exhaust manifold 897 providing a lateral passage for hot combustion exhaust gas through frame 890. As may be appreciated, exhaust manifold 897 is isolated relative to apertures 892,894, and 895. Hot exhaust gas passing through exhaust frame 890 elevates the temperature of a membrane module including frame 890 and thereby speeds heating of the membrane module during start up. Exhaust frame 890 may be incorporated into the stacked component structure of a membrane module along with the other frame members by conventional brazing, gasketing, or welding techniques as described herein.

Stacking and construction of the planar-type components as illustrated herein may be executed by use of conventional brazing, gasketing, or welding methods to create a stacked component membrane module. To establish seals between the stacked components of the modules, i. e., the membrane assemblies, permeate and feed frames, exhaust frame members, and end plates, brazing, gasketing, or welding methods are appropriate and may be used without deterioration of the delicate palladium alloy membranes 870c.

For example, brazing alloy may be applied between adjoining frame elements and the entire assembly heated to achieve a brazed joint within a controlled- atmosphere brazing furnace. Alternatively, the module may be assembled then welded from the exterior, for example, by using an orbital pipe-welding machine. In yet another proposed method of manufacture of a sealed membrane module, the components are stacked and sufficient pressure applied to the stack such that all joining surfaces are in intimate pressurized contact.

Then, heating the entire assembly to between 500 and 800 degrees Celsius for two hours to eight hours results in intermetallic diffusion between the adjoining surfaces to create a sealed joint. Yet another method for achieving gas-tight seals is to use conventional flexible (compressible) graphite gaskets or composite graphite-metal gaskets.

Thus, a variety of embodiments, configurations and alternatives have been shown for implementing steam reformation under the present invention. Various experiments and testing procedures have been conducted to prove the viability of steam reformation under the present invention and will be described in general terms as follows.

As disclosed earlier in the preferred embodiments of the present invention, the hydrogen-rich reformate stream is purified by means of a two- stage hydrogen purifier that is also the subject of this invention. The two-stage hydrogen purifier utilizes a membrane for the first stage to accomplish a bulk separation of hydrogen from the reformate stream. Then, the permeate hydrogen from the first-stage membrane is subjected to a polishing step (the second stage) to further reduce the concentration of selected impurities, such as CO and CO2, to acceptably low levels as required for the hydrogen to serve as the fuel for PEM fuel cells. For instance, a typical PEM fuel cell using a standard platinum electrocatalyst requires hydrogen containing <10 ppm CO and, preferably, <100 ppm C02 to achieve maximum power output from the fuel cell.

The membrane used in the first stage of the purifier is selected from hydrogen-permeable and hydrogen-selective high-temperature membranes. Thermally-stable membranes allow the purifier to be thermally integrated with the reformer, eliminating the requirement for cooling the hydrogen-rich reformate prior to purification, thereby simplifying the overall system and reducing the cost of the system.

Preferred membranes are microporous ceramic, microporous carbon, microporous metallic, and dense metallic membranes. Especially preferred are thin membranes composed of hydrogen-permeable and hydrogen- selective metals including palladium and palladium alloys, nickel and nickel alloys, and the Group 4 and Group 5 metals and their alloys. Thin membranes composed of Pd-40Cu are especially preferred for high hydrogen permeability and durability. In particular, the Pd-40Cu alloy exhibits highest hydrogen permeability and, therefore, most favorable economics, if the Pd-40Cu alloy contains low concentrations of carbon and oxygen. The following table demonstrates the correlation between high hydrogen permeability (represented as hydrogen flux through the 25 micron thick membrane at 100 psig hydrogen, 400 degrees Celsius) and low carbon content.

Hydrogen Flux Concentration, ppm std. ft3/ft2hr Carbon Oxygen Silicon 240 40 25 10 125 56 29 39 115 146 25 15 56 219 25 27 The hydrogen-permeable membrane does not have to exhibit an exceptionally high selectivity for hydrogen over other gases, since the second stage of the hydrogen purifier serves to further reduce the concentration of selected impurities that remain in the permeate hydrogen after passing through

the membrane. Selectivity is defined as the ratio of the permeation rate of hydrogen divided by the permeation rate of an impurity. The selectivity for hydrogen exhibited by the membrane is at least 20, and preferably at least 50.

Use of such membranes with relatively low selectivity will not yield a permeate hydrogen stream that is of acceptable purity for use in a PEM fuel cell. For example, steam reforming methanol yields a hydrogen-rich reformate stream containing about 25% combined CO and CO2. A membrane with a hydrogen selectivity of 50 will produce a permeate hydrogen stream containing 25%/50 = 0.5% combined CO and CO2. However, this level of impurities is readily treated with the polishing step (the second stage). Thus, the two-stage hydrogen purifier allows the use of membranes that, due to imperfections or otherwise, have relatively low selectivity for hydrogen over other gases. Such membranes are much less expensive than are membranes that have substantially higher hydrogen selectivity (e. g., hydrogen selectivity >1000).

To obtain a very thin metal hydrogen-permeable membrane without sacrificing mechanical strength of the membrane, the thin hydrogen- permeable membrane is supported by a support layer. The support layer must be thermally and chemically stable under the operating condition of the membrane, and the support layer is preferably porous or containing sufficient voids to allow hydrogen that permeates the thin membrane to pass substantially unimpeded through the support layer. Examples of support layer materials include metal, carbon, and ceramic foam, porous and microporous ceramics, porous and microporous metals, metal mesh, perforated metal, and slotted metal. Especially preferred support layers are woven metal mesh (also known as screen) and tubular metal tension springs.

In the event that the membrane is a thin hydrogen-permeable metal (e. g., palladium alloys) and the support layer is composed of a metal, the metal used for the support layer is preferably selected from a corrosion- resistant alloy, such as stainless steels and non-ferrous corrosion-resistant

alloys comprised of one or more of the following metals: chromium, nickel, titanium, niobium, vanadium, zirconium, tantalum, molybdenum, tungsten, silicon, and aluminum. These corrosion-resistant alloys have a native surface oxide layer that is chemically and physically very stable and serves to significantly retard the rate of intermetallic diffusion between the thin metal membrane and the metal support layer. Such intermetallic diffusion, if it were to occur, often results in significant degradation of the hydrogen permeability of the membrane and is undesirable [see Edlund, D. J., and J. McCarthy,"The Relationship Between Intermetallic Diffusion and Flux Decline in Composite- Metal Membranes: Implications for Achieving Long Membrane Lifetimes"J.

Membrane., 107 (1995) 147-153].

The rate of intermetallic diffusion between the thin metal membrane and the metal support layer may also be retarded by applying certain non-porous coatings to the metal support. Suitable coating materials include aluminum oxide; aluminum nitride; silicon oxide; tungsten carbide; tungsten nitride; oxides, nitrides, and carbides of the Group 4 and Group 5 metals; boron nitride; and boron carbide. Many of these coating are employed as hard coatings on tools and dies, and as release agents.

The second stage of the hydrogen purifier is designed to further reduce the concentration of impurities that adversely affect the power output and operation of the PEM fuel cell. Particularly, the second-stage polishing step is designed to remove CO and, to a lesser degree, C02 from the hydrogen that has permeated the first-stage membrane. Furthermore, the second-stage polishing step is conducted at or near the operating temperature of the first- stage membrane and the reformer, thereby eliminating the need to substantially heat or cool the hydrogen stream before passage through the polishing step. By thermally integrating the polishing step, the need for heat exchangers is eliminated and the overall operation of the system is simplified and the cost of the system is reduced.

Suitable chemical operations for the second-stage polishing step include preferential oxidation of CO, a widely practiced method for removing CO from hydrogen fuel streams for PEM fuel cells [Swathirajan, S., and H.

Fronk,"Proton-Exchange-Membrane Fuel Cell for Transportation"Proceedings of the Fuel Cells'94 Contractors Review Meeting, DOE/METC-94/1010, August 17-19 (1994) 105-108. However, selective oxidation only removes CO from the hydrogen stream, it does not reduce the C02 content. In fact, selective oxidation increases the CO2 content of the hydrogen. A preferred chemical operation for the polishing step is methanation, which removes both CO and C02 from the hydrogen stream, as represented by the following chemical rections: CO + 3 H2 = CH4 + H2O C02 + 4 H2 CH4+ 2H20 Methanation occurs rapidly at >300°C in the presence of a catalyst, such as nickel, palladium, ruthenium, rhodium, and platinum. Preferably, methanation is conducted at 400°C to 600°C in the presence of a commercial supported nickel reforming or methanation catalyst such as R1-10 and G1-80 manufactured and sold by BASF.

As the embodiments described earlier have shown, the first stage and second stage of the hydrogen purifier can be integrated so that they are in close proximity, thereby minimizing heat loss as well as reducing the size, weight, and cost of the hydrogen purifier. For example, if a tubular membrane is used as the first stage, the second-stage polishing step may be located within the bore of the membrane tube at the permeate side of the membrane. If a plate-type membrane is selected, the polishing step may be located at the permeate side of the membrane between membrane plates, or it may be located in a tube or other shape that is directly connected to the plate-type membrane at the permeate-hydrogen discharge port. Furthermore, if the membrane is supported for strength, and if the polishing step is methanation, the methanation catalyst may be incorporated within the support for the membrane. For

instance, the membrane support may comprise a nickel or other metal mesh with a high nickel surface area.

While previously disclosed embodiments of the invention have shown the two-stage hydrogen purifier as an integral part of the fuel processor, it will be appreciated that the two-stage hydrogen purifier may function external to a conventional process for hydrogen manufacture (e. g., steam reformer, partial-oxidation reactor, or autothermal reformer).

Concerns over safety call for use of non-flammable fuel feedstocks for use to produce hydrogen by the steam-reforming process. The advantages of using non-flammable fuel feedstocks include elimination of fire or explosion danger due to vapors from the fuel feedstock accumulating in enclosed environments and, for military applications, elimination of fire or explosion risk from hot metal fragments striking and penetrating fuel storage tanks.

Non-flammable fuel feedstocks for generating hydrogen by steam reforming and as disclosed in this invention include polyhydroxy alcohols and polyethers that are miscible with water. As used herein, non-flammable means that combustion in normal air at about 1 atm. pressure is not self-sustaining.

Preferred fuels include ethylene glycol, propylene glycol, and the glycol ethers of ethylene glycol and propylene glycol (e. g., diethylene glycol). These fuels are collectively called glycols. When mixed with a stoichiometric amount of water for steam reforming (e. g., two molar equivalents water to one molar equivalent ethylene glycol ; and four molar equivalents water to one molar equivalent propylene glycol), these fuel feedstocks are not flammable even when subjected to a propane/air flame from a torch. The flame merely heats the glycol/water mixture until the water in the mixture boils. Provided substantial water is still present in the glycol/water mixture, combustion is not supported.

The non-flammable nature of the glycol/water mixtures is due to the very low vapor pressure of the glycol component (e. g., ethylene glycol and

propylene glycol). For instance, the vapor pressure of ethylene glycol is only 20 torr at 100°C. Furthermore, the water component of these mixtures, in addition to being a necessary reactant for steam reforming, serves two functions that contribute to the non-flammable nature of these glycol/water mixtures.

First, water in the mixture serves, by evaporative cooling, to reduce the maximum temperature to which the mixture can be heated thereby limiting the maximum vapor pressure of the glycol. Second, as water evaporates at the surface of the mixture, the water vapor dilutes oxygen (from air) at the surface of the glycol/water mixture. Since oxygen is necessary for combustion, and combustion is generally favored by high oxygen concentrations, substantial dilution of oxygen from air by evaporating water serves to reduce the flammability of the glycol/water mixture.

Thus, certain feedstock mixtures are non-flammable. Simply stated, to be non-flammable the vapor pressure of the combustible component, i. e., organic component, of the fuel feedstock must remain below the lower flammability limit at 100°C; the approximate temperature at which water in the mixture will boil. Generally, this requires that the organic component have a vapor pressure <100 torr at 100°C.

In addition to being non-flammable, glycol/water mixtures, best known for their use as heat exchange fluids in internal combustion engines, are converted to a hydrogen-rich reformate stream in the presence of nickel-based steam-reforming catalysts at temperatures in the range of 400°C to 700°C.

Glycol/water mixtures also offer the advantage of forming stable solutions over a wide range of water concentration, so that the proper water to glycol steam reforming ratio can be obtained by appropriately mixing the glycol/water fuel feedstock and then dispensing this fuel feedstock into a supply tank (or reservoir) from which the fuel feedstock is delivered at the proper rate to the reformer. Yet another advantage of the glycol/water mixtures is that they remain liquid over a large temperature range, and they are generally viscous

liquids. Glycol/water mixtures, sold commercially as antifreeze coolants, remain liquid even at temperatures well below 0°C and at temperatures greater than 100°C. Being liquid, glycol/water mixtures are efficiently pumped to elevated pressure for delivery to the reformer so that steam reforming can be conducted at elevated pressure (up to 500 psig, but preferably 100 psig to 300 psig). The high viscosity of glycol/water mixtures leads to greater pumping efficiency, particularly if a gear pump, piston pump, or centrifugal pump is used to deliver the high-pressure fuel feedstock to the reformer. The high viscosity reduces slippage past the wetted surfaces of the pump, which often limits the maximum pressure differential at which a pump may be used.

To demonstrate the integrated fuel processor of this invention, the fuel processor depicted generally in Fig. 5 was constructed and operated. The tubular metal membrane (first stage of the hydrogen purifier) was made using the method generally described in connection with Figs. 12-17. The hydrogen- permeable metal foil 702 consisted of Pd-40Cu nominally 25 microns thick, and the membrane was about 15 cm long (2.8 cm outside diameter). The second stage of the hydrogen purifier, a catalytic methanizer, was contained in a copper tube, 1.8 cm outside diameter, that was inserted inside the bore of the tubular membrane 700. One end of the copper methanation tube was sealed to one of the tubular-membrane end caps 730. The other end of the copper methanation tube was terminated about 0.3 cm from the end of the membrane tube whereby hydrogen permeating to the inside of the membrane tube 700 would freely flow into the open end of the methanation tube such as shown generally in Figure 3. The methanation tube was filled with catalyst G1-80 (BASF), a supported nickel composition that is active for methanation of CO and CO2.

The reforming region of the fuel processor was filled with catalyst K3-110, a copper/zinc supported catalyst sold by BASF generally for conducting the water-gas shift reaction at <350°C. The shell of the fuel processor, the spiral combustion tube, and the end plates were all constructed

from stainless steel. Insulation was placed around the exterior of the shell and end plates to reduce heat loss.

The fuel processor was operated using methanol/water mix as the feed. The methanol/water solution was prepared by mixing 405 mL methanol (histological grade, Fisher Scientific) with 180 mL deionized water. The fuel processor was heated to 200°C to 300°C using an externally placed electric resistance heater. Once the fuel processor was hot, the electric heaters were turned off and methanol/water solution was pumped into the fuel processor at 200 psig. The methanol/water feed was first vaporized then the vapors passed over the K3-110 reforming catalyst to produce hydrogen-rich reformate. The two-stage hydrogen purifier then extracted product hydrogen at ambient pressure from the hydrogen-rich reformate. The hydrogen-depleted raffinate was directed to the combustor as described above. Combustion of this raffinate gas inside the fuel processor heated the fuel processor to 300°C. to 350°C and provided all required heat once operation of the fuel processor commenced.

The purity of the product hydrogen was determined by gas chromatography and the flow rate of the product hydrogen was measured using a calibrated gas flow meter. Analysis of the product hydrogen confirmed <10 ppm CO and <10 ppm C02. The flow rate of product hydrogen was 2 L/min.

The reformer was operated in this mode, without any external source of heating, for 6 hours at which time the experiment was concluded.

According to a second example, tubular Pd-25Ag membranes with a 2.2 cm outside diameter were made using the general method described in connection with Figs. 12-17. The Pd-25Ag foil was 25 micron thick and 7.0 cm wide by 16 cm long and the copper foil frame was 125 micron thick and 8.3 cm wide by 17.8 cm long. The dimensions of the center cut out in the copper foil frame was 5.7 cm wide by 14 cm long. The welding equipment and methods described in connection with Figs. 12-17 were used to join the palladium-alloy foil to the copper foil frame. The support for the membrane was a carbon steel tension spring, 2.2 cm outside diameter. The spring was

made using wire nominally 0.25 cm diameter. End caps were brazed to the ends of the membrane tube using the method given above or, in some cases, end caps were sealed to the ends of the membrane tube using graphite seals.

The graphite seals were achieved using flexible graphite tape (1.3 cm wide) wrapped around the membrane tube and then compressed against the membrane in a standard compression fitting.

In another example, plate-type membrane modules were made using the following general method. Hydrogen-permeable Pd-40Cu foil, nominally 25 micron thick and 5.1 cm by 5.1 cm square, were welded to a copper foil frame (nominally 125 micron thick) using the ultrasonic welder and welding parameters discussed above. The copper foil frame was circular in shape (8.9 cm diameter) with cut outs for feed and permeate as shown in Fig.

20. After welding the Pd-40Cu membrane to the copper foil frame to make the membrane assembly, the weld was checked for leaks by a standard dye penetration test.

The copper permeate plate (Fig. 21) was 0.3 cm thick and 8.9 cm diameter. A recessed was machined in the permeate plate to accept the support layer for the membrane. This recess, as shown in Fig. 21, was of the same dimensions as the membrane and connected to the permeate manifold channel.

The support layer consisted of a first layer of stainless steel screen (70x70 mesh), placed against the permeate plate, then a second layer of stainless steel screen (200x200 mesh) that the thin Pd-40Cu foil rested against. This combination of coarse mesh and fine mesh was determined to both adequately support the thin membrane without excessively damaging the membrane, and provide acceptably low resistance to the lateral flow of permeate hydrogen.

The stainless steel screen was fixed to the permeate plate with a single drop of cyanoacrylate glue, and the glue allowed to dry. Then, two membrane assemblies were brazed to a single permeate plate, one membrane assembly at each major surface of the permeate plate. Brazing was achieved using a standard brazing alloy (nominally 80% copper, 15% silver, and 5%

phosphorous) in either ribbon form or as a paste (powdered brazing alloy mixed with a paste binder). This brazing alloy was purchased from Lucas-Milhaupt, Inc. (Cudahy, WI). To prevent unwanted creep of the brazing alloy over the surface of the Pd-40Cu membrane, Nicrobraz Red Stop-Off Type II (Wall Colmonoy Corp., Madison Hts., MI) was applied around the edge of the Pd- 40Cu membrane. This assembly was then placed on a flat surface beneath a steel weight (approximately 1.5 kg) and heated to 750°C in a brazing furnace.

A coating of boron nitride, a release agent, was applied to the steel surfaces in contact with the membrane assembly during brazing to prevent sticking between the membrane assembly and the steel surfaces. Brazing was done under vacuum, a nitrogen atmosphere, or a nitrogen stream containing a low concentration of methanol or hydrogen to serve as a reducing gas (to prevent oxidation). The brazing temperature of 750°C was held for 15 minutes prior to cooling.

To demonstrate the non-flammability of ethylene glycol/water mixtures, the following experiment was conducted. Ethylene glycol (1.0 mL) was mixed with two molar equivalents water (0.65 mL). The resulting homogeneous solution is of the proper stoichiometry for steam reforming, as shown by the following ideal reaction equation: HOCH2CH20H + 2 H2O = 2 CO2 + 5 H2 This solution of ethylene glycol and water was directly exposed to the flame from a propane/air torch. The ethylene glycol/water solution did not burn or support combustion.

In yet another example, a 2: 1 molar ratio of water-to-ethylene glycol was prepared by mixing 65 mL deionized water and 100 mL purified reagent grade (Fisher Scientific) to form a homogeneous solution. This ethylene glycol/water solution was reformed to produce hydrogen in a laboratory-scale packed-bed catalytic reactor as described below.

The catalytic reactor consisted of a cylindrical stainless steel shell 2.5 cm inside diameter and 22.9 cm long. The reactor contained a fixed bed of

the commercial catalyst G1-80 (BASF), which is a supported nickel steam reforming catalyst. A length of stainless steel tubing (0.3 cm diameter by about 25 cm long) was coiled around one end of the catalytic reactor to serve as a preheater and vaporizer for the ethylene glycol/water feed. One end of this vaporization coil was connected to the inlet of the catalytic reactor, the other end of the coil was connected to a reservoir containing the ethylene glycol/water feed. The temperature within the catalytic reactor was measured and controlled via a thermocouple inserted within the catalyst bed.

The catalytic reactor was heated to 500°C by means of an external electric furnace. The G1-80 catalyst was then reduced in situ by first flowing ethylene glycol/water feed into the catalytic reactor at a rate of 2.5 mL/min (liquid flow rate) for 2 hrs, then flowing pure hydrogen at ambient pressure through the catalytic reactor for another 4 hrs. Following reduction of the steam reforming catalyst, ethylene glycol/water feed was admitted into the catalytic reactor at ambient pressure. The temperature of the catalytic reactor was varied between 400°C and 500°C. The product gas was shown to be predominantly C02 and H2 by gas chromatography analysis, unreacted ethylene glycol/water was collected in a cold trap and quantified by gravimetric analysis, and the product flow rate was measured using a calibrated gas flow meter to determine the degree of conversion to products. The results of these experiments are summarized in the following table. Temperature (°C) Product Flow Rate (L/min) Conversion to Products (%) 500 +/-50 3-5 90-95 465 +/-25 4-5 90-95 400 +/-25 4-5 93-98 To demonstrate the utility of the two-stage hydrogen purifier when utilized as a stand-alone hydrogen purifier, the following experiment was

conducted.

A tubular hydrogen-permeable metal membrane was made using the method described in Figs. 12-17. The membrane consisted of Pd-25Ag foil nominally 25 micron thick and was 2.2 cm outside diameter by 15 cm long, the overall length of the membrane tube (including end caps) was approximately 21 cm. This tubular membrane serves as the first stage of the purifier. The second stage of the purifier, a catalytic methanizer, was contained in a copper tube, 1.58 cm outside diameter, that was inserted inside the bore of the tubular membrane. One end of the copper methanation tube was sealed to one of the tubular-membrane end caps. The other end of the copper methanation tube was terminated about 0.3 cm from the end of the membrane tube so that hydrogen permeating to the inside of the membrane tube would freely flow into the open end of the methanation tube (this arrangement is shown in Figure 3). The methanation tube was filled with catalyst G1-80 (BASF), a supported nickel composition that is active for methanation of CO and CO2.

This two-stage hydrogen purifier was placed in a stainless steel shell equipped with electric resistance heaters. The hydrogen purifier was heated to 300°C to 350°C, and methanol/water reformate (approximately 70- 75% hydrogen, balance CO and CO2) at 50 psig was passed into the stainless steel shell and over the exterior surface of the Pd-25Ag membrane tube.

Product hydrogen at ambient pressure, after permeation through the Pd-25Ag membrane and then passage over the methanation catalyst, was collected and analyzed by gas chromatography. Analysis confirmed that the product hydrogen contained <2 ppm CO and <50 ppm CO2.

Thus, a steam reformer with internal hydrogen purification has been shown and described. The reformer of the present invention utilizes a single feed, e. g., a methanol and water or hydrocarbon and water mix, as both the chemical feed stock to support hydrogen reforming and also as a combustion fuel source to provide sufficient temperature to support steam reforming. The present invention recovers by design less than a maximum

amount of hydrogen available in a reforming step to leave in the byproduct stream sufficient hydrogen as fuel to support the combustion process. The present invention uses two distinct hydrogen purification processes. First, a membrane produces a hydrogen stream as a bulk filtration step, but the product hydrogen stream may still contain some undesirable impurities. Second, a polishing process converts the undesirable impurities in the hydrogen stream to innocuous components not affecting operation of, for example, a fuel cell.

Advantageously, this allows use of a relatively less expensive, thin palladium- alloy membrane in the steam reforming process.

In Fig. 25, another embodiment of the fuel processor, or reformer, is shown and generally indicated at 900. Similar to the previously described embodiments, reformer 900 includes a shell 902 that houses steam reforming 904 and combustion 906 regions, as well as at least one steam reforming tube 908. Three such tubes are shown in Fig. 25, and each contains steam reforming catalyst 910. It should be understood that, like the rest of the reformers disclosed herein, reformer 900 may include as few as one tube and preferably includes multiple tubes. Between six and ten reforming tubes have proven effective, both in hydrogen production rate and compactness of the overall reformer. However, the number of tubes in any particular embodiment may vary, depending upon such factors as the size of the reformer's shell, the desired rate of hydrogen production, and the number of additional elements within the shell. For example, when a plate-type membrane module is used, there is more available space adjacent the side walls of the reforming tubes.

As shown in Fig. 25, a portion 911 of each reforming tube 908 extends external shell 902. This enables the tubes (and the reforming catalyst contained therein) to be accessed without having to open the shell. In this configuration each end portion 911 includes a removable cap or other closure which may be selectively removed to permit access to the interior of the tube, and thereafter replaced. This configuration for the reforming tubes may be

used with any of the other reformers disclosed herein, just as reformer 900 may include reforming tubes which are completely housed within shell 902.

Tubes 908 are heated by hot combustion gasses passing from internal combustion manifold 912 to internal exhaust manifold 914, and ultimately exiting reformer 900 through outlet 916. In Fig. 25, a plurality of passages 918 are shown which permit the hot combustion gasses to pass between manifolds 912 and 914, and thereby heat tubes 908 as the gasses flow around the tubes.

Hot combustion gasses are produced by burner 920. Upon initial startup, burner 920 is ignited by a suitable ignition source, such as spark plug 922, or any of the other ignition sources disclosed herein. Combustion air, preferably at or near ambient pressure, is brought into burner 920 through combustion port 924.

Feedstock for the steam reforming process is admitted into the fuel processor through inlet tube 926 and passes into the hot combustion region 906 of fuel processor 900, wherein the feedstock is vaporized. A single inlet tube 926 may be used to admit a feedstock comprising alcohol and water, or multiple separate inlet tubes may be used (such as disclosed herein) if the feedstock consists of separate streams of water and a hydrocarbon or alcohol.

As shown in Fig. 25, inlet tube 926 forms a coil 927 that extends around tubes 908 multiple times before entering a distribution manifold 928. Coil 927 should be of sufficient length that the feedstock is vaporized prior to reaching distribution manifold 928. It should be understood that the circuitous path of coil 927 is shown in Fig. 25 for purposes of illustrating one possible path. The important concern is that the coil is of sufficient length that the feedstock passing there through is vaporized by heat transmitted to it as it travels to distribution manifold 928. To aid with the vaporization of the feedstock, multiple coils of tubing may be used to effectively increase the heat transfer surface area of the tubing, and thereby aid in the vaporization of the feedstock.

Vaporization of the feedstock may also be accomplished using plate-type vaporizers.

From distribution manifold 928, the vaporized feedstock is distributed to steam reforming tubes 908. When tubes 908 are of similar size or are adapted to process generally equal volumes of feeds, the feedstock is evenly distributed between the tubes by manifold 928. However, the feedstock may be otherwise proportioned if the tubes are adapted to receive and process different flows of the feedstock.

Within reforming tubes 908, the feedstock undergoes a catalytic reaction to yield a hydrogen-rich reformate gas stream which contains carbon monoxide and carbon dioxide in addition to hydrogen. To purify the produced hydrogen, fuel processor 900 includes a purification module (or membrane module) 930, through which the reformate gas stream is passed. One or more hydrogen-selective inorganic membranes, such as any of the hydrogen-selective metal (and preferably palladium alloy) membranes disclosed herein, are contained within module 930. Membrane module 930 may include any suitable configuration, including those previously described herein. The hydrogen that permeates the hydrogen-selective membranes passes from the module through an outlet port 932 and into a polishing catalyst bed 934. Preferably, the polishing catalyst bed contains a methanation catalyst (not shown) to convert carbon monoxide and carbon dioxide in the permeate stream into methane.

As shown in Fig. 25, polishing catalyst bed 934 is located external shell 902, where it is heated by radiant heat and thermal conduction from hot shell 902. As shown, bed 934 lies against the exterior surface 936 of shell 902. However, it is within the scope of the invention that bed 934 may be at least partially or completely spaced away from shell 902, so long as it still receives sufficient heat for the polishing reaction. Polishing catalyst bed 934 is further heated by the hot hydrogen that flows into the bed from the methanation module 930. Finally, purified hydrogen exits reformer 900 via tube 938. By locating the polishing catalyst bed external shell 902, reformer 900 may either

include additional reforming tubes within its shell, or the shell may be smaller because it no longer needs to house the polishing catalyst bed.

It should be understood that as used herein, purified hydrogen refers to a stream that is at least substantially comprised of hydrogen gas. The stream may include other components, such as methane produced in the polishing catalyst bed, but the stream contains less than defined minimum amounts (i. e. trace concentrations) of impurities (such as carbon monoxide and carbon dioxide) which would harm or lessen the effectiveness of a fuel cell.

Waste gasses, including some of the produced hydrogen gas, that do not pass through the hydrogen-selective membrane within module 930 are used as fuel to heat fuel processor 900. Therefore, the hydrogen-depleted raffinate stream (which exits module 930 through conduit 940) is directed into burner 920. As discussed previously, the concentration of hydrogen within the raffinate stream may be selectively controlled so that there is sufficient fuel gas to maintain reformer 900 within desired temperature ranges.

Fig. 25 illustrates other non-essential elements that may be used within any of the reformers disclosed herein. For example, in Fig. 25, reformer 900 further includes a pressure gauge 942 for monitoring the pressure of the fuel gas in conduit 940, a pressure relief valve 944, and a vent valve 946. Also illustrated are a valve 948, which controls the flow of fuel gas in conduit 940 to the burner and applies back pressure on the reforming region, and a valve 949, which controls the flow of start-up fuel gas (previously produced and stored or supplied from an external source), such as hydrogen, propane or natural gas, during a cold start-up of the reformer.

In Fig. 26, a variation of the reformer of Fig. 25 is shown and generally indicated at 950. Unless otherwise indicated, reformers 900 and 950 contain the same components and subcomponents. To provide more space within shell 902, and thereby permit additional reforming tubes 908 to be housed therein, reformer 950 includes vaporization coils 952 which are located external shell 902. As shown, coils 952 are wrapped around the external

surface 936 of shell 902 and are in contact therewith. Similar to the polishing catalyst bed described with respect to Fig. 25, coils 952 may be at least partially or completely spaced apart from shell 902. In this case, the important factor is that sufficient heat is transmitted to the feedstock within the coils to vaporize the feedstock before it reaches distribution manifold 928. In the position shown in Fig. 26, the coils are heated by radiation and thermal conduction from the hot surface of shell 902.

The reformer shown in Fig. 26 also demonstrates structure for admitting immiscible feedstocks to the reformer. As shown, reformer 950 includes an inlet tube 954 through which a water feed is received and delivered to vaporization coils 952. A hydrocarbon or alcohol feed is admitted through inlet tube 956, and it is mixed with the hot steam before passing into the reformer through a reformer inlet tube 958. The combined feedstock stream passes into one end of a mixing chamber 960, which contains an optional static mixer or a packing (not shown) to promote turbulent flow and thereby encourage mixing of the vaporized feedstocks. The mixed, vaporized feedstock exit the mixing chamber and are delivered to distribution manifold 961, which in turn distributes the feedstock to the reforming tubes.

To increase the energy efficiency and to increase the combustion chamber temperature within reformer 950, reformer 950 includes a quenching chamber 962 adapted to partially quench the reformate gas stream prior to its entrance into membrane module 930. As shown, the reformate gas stream must pass through chamber 962 after exiting reforming tubes 908 and prior to entering membrane module 930. Chamber 962 includes a pair of ports 964 and 966 through which combustion air respectively enters and exits the chamber.

The air is cooler than the reformate gas stream, and therefore cools the reformate gas stream prior to its entry into the membrane module. During this exchange, the combustion air is heated prior to its entry to burner 920.

The quenching chamber and external vaporization coils described with respect to reformer 950 may be used with any of the reformers (or fuel

processors) described herein. Similarly, the external polishing catalyst bed may be used with any of the reformers described herein, such as to increase the number of reforming tubes within the reformer's shells or to decrease the size of the shell. It should be understood that the reformers described herein have been shown and described to illustrate particular features of the invention, and that particular elements or configurations may be selectively used with any of the reformers described herein.

In many of the previously described embodiments, the end plates and/or membrane modules of the reformers (or fuel processors) are secured to the rest of the reformers with bolts and gaskets. It should be understood that any other suitable form of fastening mechanism and seal may be used so long as the shell is sealed against leaks and secured together so that it does not unintentionally open, such as during operation. Although welding and other more permanent fasteners are within the scope of suitable fastening mechanisms, fastening mechanisms which may be selectively removed and resecured, such as the bolts and nuts shown for example in Figs. 25 and 26, are preferred.

In Fig. 27, a fuel-cell system is schematically shown. The system includes a fuel cell 1010 that produces electrical power from air (oxygen) and hydrogen, and a fuel processor (such as any of the previously described steam reformers) 1012 that produces hydrogen from a variety of feedstocks.

Generally, said fuel cell is a net producer of water, and said fuel processor 1012 is a net consumer of water.

Fuel cell 1010 is preferably a proton exchange membrane fuel cell (PEMFC) and may utilize internal humidification of air and/or hydrogen, including so called self-humidification, or external humidification of air and/or hydrogen. Fuel cell 1010 produces byproduct water and byproduct heat in addition to electrical power.

Many feedstocks are suitable for producing hydrogen using fuel processor 1012 including, but not limited to, carbon-containing compounds

such as hydrocarbons, alcohols, and ethers. Ammonia is also a suitable feedstock. Fuel processor 1012 preferably produces hydrogen by reacting the carbon-containing feedstock with water by a process commonly known as steam reforming. In this case fuel processor 1012 consumes water in addition to consuming feedstock. It is within the scope of the present invention that other chemical methods for making hydrogen from a feedstock, such as partial oxidation and autothermal reforming, may also be used as well as steam reforming.

Fig. 27 illustrates a process flow diagram for a fuel cell system of this invention. The fuel cell, or fuel cell stack, 1010 receives hydrogen produced by the fuel processor 1012. The fuel processor produces hydrogen by reacting, at high temperature, a feedstock from storage reservoir 1014 and water from storage reservoir 1016. Pump 1020 moves feedstock from reservoir 1014 and delivers the feedstock to fuel processor 1012. Likewise, pump 1021 moves water from reservoir 1016 and delivers the water as stream 1022 to the fuel processor 1012. Pumps 1020 and 1021 deliver the feedstock and water to the fuel processor at a pressure ranging from ambient pressure to approximately 300 psig.

Hydrogen produced by the fuel processor is initially hot because the fuel processor must operate at elevated temperatures of 250 °C to 1300 °C.

The product hydrogen stream 1023 from the fuel processor is cooled using heat exchanger 1024 and fan 1026 to blow cool ambient air over the hot heat exchanger surfaces. Once cooled to a temperature near to or lower than the operating temperature of the fuel cell, which typically is between approximately 0 °C and approximately 80 °C, product hydrogen is passed into the anode chamber 1028 of the fuel cell stack.

An air stream 1029 is delivered to the cathode chamber 1030 of fuel cell 1010 by a blower 1032. Alternatively, a compressor could also be used in place of blower 1032. An example of suitable blowers are centrifugal blowers because of their low noise during operation and low power

requirements. However, centrifugal blowers are generally limited to relatively low delivery pressure, typically <2 psig. For higher delivery pressures, a linear compressor may be used. Linear compressors are based on an electromechanical (solenoid) drive that is characterized by relatively low power consumption and low noise. An example of a suitable linear compressor is Model Series 5200 sold by Thomas Compressors & Vacuum Pumps (Sheboygan, WI).

A coolant circulating loop is used to maintain the temperature of the fuel cell stack within acceptable limits, such as those described above. The coolant serves the purpose of cooling both the cathode and anode chambers of the fuel cell stack. To this end, coolant circulating pump 1034 circulates hot coolant from the fuel cell stack into heat exchanger 1036. Fan 1038 blows cool air over the hot surfaces of heat exchanger 1036, thereby reducing the temperature of the coolant. The coolant may be de-ionized water, distilled water, or other non-conducting and non-corrosive liquids including ethylene glycol and propylene glycol.

A pressure regulator 1040 ensures that the pressure of the hydrogen supplied to the anode chamber 1028 of said fuel cell 1010 remains at an acceptable value. For most PEM fuel cells, this range of pressures is between ambient pressure to 4 atmospheres, with a pressure range between ambient pressure and approximately 1.5 atmospheres being preferred. Within the anode chamber of the fuel cell hydrogen is consumed and, at the same time, diluted with water vapor. Thus, a periodic purge of hydrogen-rich gas from the anode chamber is required. Purge valve 1042 serves this purpose. The purge hydrogen represents a small amount of the total hydrogen supplied to the fuel cell, typically only about 1% to 10% of the total. The purge hydrogen stream 1044 may be vented directly to the surroundings, as shown in Fig. 27, or it may be used for the purpose of producing heat, or for other purposes. In some embodiments of this system, hydrogen stream 1023 may be flowed continuously in excess through anode chamber 1028, eliminating the need for

said purge valve 1042. Since some liquid water may be entrained in said purge hydrogen stream 1044, an optional water knock-out may be placed in purge stream 44 for the purpose of separating and collecting said entrained liquid water.

Excess air is continuously flowed through the cathode chamber 1030. Typically the air flow rate is 200% to 300% of the stoichiometric requirement of oxygen to support the magnitude of electrical current produced by the fuel cell, although flow rates outside of this range may be used as well.

Oxygen-depleted air is discharged from cathode chamber 1030 as stream 1052.

Stream 1052 contains substantial water, as both liquid and vapor, available for recovery. Stream 1052 is typically saturated with water vapor, and as an example, approximately one third or more of the total water may be freely condensed to liquid water. In an embodiment of this system, stream 1052 is first passed through a knock-out 1054 that separates liquid water from the oxygen-depleted air and water vapor. Liquid water stream 1056 flows out of said knock-out 1054 and the liquid water is collected within water reservoir 1016. The gas-phase stream 1058 exiting knock-out 1054 comprises the oxygen-depleted air and water vapor.

Stream 1058 is directed into fuel processor 1012 for the purpose of supporting combustion within the fuel processor to generate the required heat for satisfactory operation of the fuel processor (if the fuel processor is based on steam reforming), or to supply oxidant (oxygen) for partial-oxidation of the feedstock (if the fuel processor is based on partial oxidation or autothermal reforming). Since stream 1058 is to be used for combustion, there is no primary reason to cool stream 1058 or stream 1052, other than to assist with separation of liquid water within knock-out 1054.

Still referring to Fig. 27, fuel processor 1012 is preferably a steam reformer, such as any of the reformers discussed above. To initially heat fuel processor 1012 during a cold start-up, a suitable fuel such as propane or natural gas is fed from a supply source 1060 to the fuel processor. The fuel is

combusted within the fuel processor 1012 until the fuel processor is hot enough to begin steam reforming the feedstock. A throttle valve 1062 regulates the flow of propane or natural gas fuel to the fuel processor during this cold start- up.

Combustion exhaust stream 1064 exits the fuel processor as a hot gas stream laden with water vapor. The water vapor in combustion exhaust stream 1064 has essentially two sources: as a byproduct of burning the fuel, and as a component of air stream 1058. It is desirable to recover the water from combustion exhaust stream 1064 and to recover heat from exhaust stream 1064. Condenser 1066 serves this purpose. Hot, moist exhaust stream 1064 passes into condenser 1066 and is chilled using a cold fluid stream 1068.

Streams with temperatures near or less than 20 °C have proven effective.

Liquid water condenses and flows out of condenser 1066 as liquid stream 1069, and is collected in water reservoir 1016.

Cold fluid stream 1068 is warmed by the process of passing hot exhaust stream 1064 through condenser 1066. For example, cold outside air may serve as stream 1068 and be heated for the purpose of space heating in a residential, commercial, or industrial application. Alternatively, cold water may serve as stream 1068 and be heated for use as domestic or process hot water, or the hot water may be used for space heating or other heating applications. Yet another embodiment is that a cold fluid other than air or water including, but not limited to ethylene glycol and propylene glycol, serves as stream 1068.

Once fuel processor 1012 has reached a suitable temperature for steam reforming the feedstock, feed water and feedstock are pumped into said fuel processor. For methanol, this temperature should be at least 250 °C, with temperatures of at least 450 °C and preferably at least 600 °C being used for most hydrocarbon feedstocks. The steam reforming reaction produces a hydrogen-rich reformate gas mixture that is preferably purified within the fuel processor, such as discussed above. The pure product hydrogen stream 1023 is

passed to the fuel cell as previously described. The hydrogen-depleted stream 1075 that is rejected by the hydrogen purifier is passed through throttle valve 1078 to be used as fuel for combustion to heat said fuel processor 1012. At this time during the operation of fuel processor 1012 there is no longer a need to supply propane or natural gas fuel that was used for the cold start-up, and that fuel supply is shut off.

Fig. 28 illustrates another embodiment of an integrated fuel-cell system in which the fuel processor 1012 is heated during a cold start-up by combustion of a liquid fuel, rather than propane or natural gas. The liquid fuel may be diesel, gasoline, kerosene, ethanol, methanol, jet fuel, or other combustible liquids. During a cold start-up, liquid fuel is removed from storage supply 1100 using pump 1102. The discharged liquid fuel from pump 1102 is admitted through a suitable nozzle or jet into the combustion region in fuel processor 1012 where the fuel is mixed with air and burned to heat said fuel processor. The liquid fuel may be vaporized or atomized prior to injection into fuel processor 1012 to facilitate combustion.

Another embodiment of the fuel-cell system that is directed to cold start-up of fuel processor 1012 is shown in Fig. 29. In this case cold start- up is accomplished by combustion of hydrogen fuel within fuel processor 1012.

Hydrogen fuel is stored by within hydrogen storage vessel 1150 by any known method. An example of a particularly well-suited method for storing hydrogen fuel is as a metal hydride. The metal hydride then comprises a metal hydride storage bed serving as storage vessel 1150.

Metal hydrides exist in equilibrium with gaseous hydrogen (see F. A. Lewis,"The Palladium Hydrogen System"Academic Press, 1967; and "Hydrogen in Metals 1: Basic Properties"edited by G. Alefeld and J Völkl, Springer-Verlag, 1978, the disclosures of which are hereby incorporated by reference). The equilibrium pressure of hydrogen gas over a given metal hydride is a function of the chemical composition of the metal hydride and the temperature of the system. Thus, it is possible to select a metal hydride

chemical composition such that the equilibrium pressure of hydrogen over the metal hydride is between 0 psig (ambient pressure) and 10 psig at a temperature of about 15 °C to 22 °C. Increasing the temperature of the metal hydride system increases the equilibrium pressure of hydrogen over the metal hydride.

Returning to Fig. 29 and for purposes of illustration, it is assumed that storage reservoir 1150 contains a suitable quantity of a metal hydride, and is called a metal hydride bed. During a cold start-up, fuel hydrogen stream 1152 is withdrawn from hydride storage bed 1150 and, after passing through isolation valve 1154, is admitted into fuel processor 1012 where said hydrogen fuel is combusted to heat the fuel processor. As fuel hydrogen is withdrawn from storage bed 1150, the pressure of gaseous hydrogen in said storage bed will begin to decrease and the bed will begin to cool in temperature (phenomena well known to those skilled in the art of hydrogen storage in metal hydride beds). To counteract these trends, warm combustion exhaust stream 1064 is flowed through metal hydride storage bed 1150 to heat said metal hydride bed. Then, the now cool exhaust exits the warmed metal hydride bed 1150 as cool exhaust stream 1158. This allows the pressure of gaseous hydrogen to remain sufficiently high to discharge most of, to nearly all of, the hydrogen from storage bed 1150.

Alternative embodiments of this system may utilize other suitable sources to heat metal hydride bed 1150 including electrical resistance heaters and combustion of hydrogen or other fuel to directly heat storage bed 1150.

After completing cold start-up of fuel processor 1012 and hydrogen is being produced by the fuel processor, isolation valve 1154 is closed and hydride storage bed 1150 is recharged with hydrogen so that it will be ready for the next cold start-up. Recharging of storage bed 1150 is accomplished by taking a hydrogen slip stream 1160 from purified product hydrogen stream 1023 after said product hydrogen stream has been cooled by passing through heat exchanger 1024. During this hydrogen recharging operation, byproduct heat should be removed from hydride storage bed 1150,

such as through any known mechanism. An optional isolation valve 1162 is placed in hydrogen slip stream 1160 to facilitate maintenance.

An advantage of this embodiment of the invention is that the fuel required for cold start-up of fuel processor 1012 is clean burning hydrogen, acquired from a previous period of operating the system. Thus, it is not necessary to periodically resupply an auxiliary fuel such as propane or diesel for start-up purposes, nor is it necessary to have a large external storage reservoir for said auxiliary fuels.

Fig. 30 presents another embodiment of a fuel-cell system. In this embodiment, purge hydrogen stream 1044 is passed into combustor 1200 for the purpose of generating additional water to be recovered ultimately by knock-out 1054 and condenser 1066. Combustor 1200 may be catalytic or non- catalytic. Air to support combustion of purge hydrogen stream 1044 is supplied by the cathode exhaust stream 1052 which is depleted, but not devoid, of oxygen as described previously. The single outlet from combustor 1200 is exhaust stream 1202 that is enriched in water (vapor and liquid) as a result of burning purge hydrogen stream 1044.

In another embodiment of the present system, heat is recovered in addition to water recovery from combustion of purge hydrogen 1044. As shown in Fig. 31, combustor 1200 is coupled to heat exchanger 1250 for the purpose of recovering and using heat generated by combustion of purge hydrogen stream 1044 within combustor 1200. Heat exchanger 1250 may include heat-conductive fins on the exterior of combustor 1200, or a heat exchange fluid may be passed between combustor 1200 and heat exchanger 1250. The heat exchange fluid may be circulated based on natural convection currents, or it may be forcibly circulated by a circulation pump. To utilize the recovered heat a suitable cold fluid stream is passed over hot heat exchanger 1250. One such suitable cold fluid stream is air, in which case fan 1252 blows a cold air stream over heat exchanger 1250 resulting in an increase in the temperature of the air stream. Other suitable cold fluids include, but are not

limited to, water, ethylene glycol, propylene glycol, and both the feedstock and feed water to be fed to fuel processor 1012.

Useful heat can also be recovered from fuel processor 1012.

Fig. 32 illustrates an embodiment of the fuel-cell system which demonstrates this recovery of heat. Heat exchanger 1300 extracts heat from the high- temperature combustion regions of fuel processor 1012. Pump 1302 may be used to circulate a heat transfer fluid between fuel processor 1012 and heat exchanger 1300, as shown in Fig. 32, or circulation of said heat transfer fluid may be based on naturally occurring convection currents. Alternatively, heat exchanger 1300 may comprise a series of heat-conductive fins placed on the hot regions of the fuel processor. For purposes of heat recovery and use, a suitable cold fluid is passed over the hot heat exchanger 1300. Such a suitable cold fluid may be an air stream supplied by fan 1305. In this case said air stream is heated by passing over hot heat exchanger 1300. Other suitable cold fluid streams include, but are not limited to, water, ethylene glycol, and propylene glycol.

Another embodiment of the system is shown in Fig. 33. Dual- head pump 1350 supplies both feedstock from reservoir 1014 and feed water from reservoir 1016 to fuel processor 1012. Dual-head pump 1350 comprises two pump heads driven by a single drive motor such that both pump heads are driven at the same speed over the entire operating speed range of the pump motor. The pumping rate of each feedstock and feed water is determined by the displacement of each respective cavity in dual-head pump 1350. For example, to preserve a fixed ratio of feed water to feedstock, as is desirable for steam reforming, the dual-head pump may be a gear pump with a ratio of displacement volume of the two pump heads being 3: 1. Thus, if the larger displacement pump head supplied feed water to the fuel processor, and the smaller displacement pump head supplied feedstock (e. g., a liquid hydrocarbon), then the flow rate of feed water would be three times greater than the flow rate of feedstock into the fuel processor. This ratio would be

essentially constant over the entire range of delivery rates achievable with the dual-head pump since this ratio is fixed by the displacement volumes of each of the two pump heads and both pump heads are driven at the same speed by the same drive motor. Suitable types of dual-head pumps include, but are not limited to, gear pumps, piston pumps, diaphragm pumps, and peristaltic pumps.

Another embodiment of the fuel-cell system utilizes the hot product hydrogen stream 1023 as it exits fuel processor 1012 to pre-heat feed water stream 1022 prior to introduction of the feed water into the fuel processor. As shown in Fig. 34, feed water stream 1022 enters a counter- current heat exchanger 1400. Hot product hydrogen stream 1023 also flows into counter-current heat exchanger 1400. The feed water stream and the hydrogen stream are isolated from each other, but are in thermal contact such that the hot hydrogen stream is cooled during passage through heat exchanger 1400 and the feed water stream is warmed during its passage through heat exchanger 1400. When the invented system of Fig. 34 is used, it is preferable that product hydrogen stream 1023 is cooled to a temperature at or near the operating temperature of the fuel cell (typically between approximately 40 °C and approximately 60 °C).

Maintaining acceptable water purity in the cooling loop for fuel cell 1028 is an important aspect of the successful operation of a PEMFC system. Often, to achieve this objective, fuel cell manufacturers specify stainless steel for all wetted surfaces of the PEMFC cooling loop. This leads to considerable expense, especially since stainless steel radiators (heat exchangers) are expensive and, by virtue of the relatively poor thermal conductivity of stainless steel, large in size.

Fig. 35 shows an embodiment of this system that overcomes the need to use stainless steel components throughout the cool loop of the fuel cell, thereby improving the performance of said cooling loop and decreasing its cost.

This objective is achieved by placing an ion exchange bed 1450 in the cooling loop so that cooling water passes through the ion exchange bed during

operation of the system. Either all of the cooling water or a portion of the cooling water is passed through the ion exchange bed. Since the objective is to maintain low ionic (both cationic and anionic) concentrations in the cooling water, ion exchange bed 1450 should comprise both cation-exchange resins and anion-exchange resins.

If a slip stream of cooling water is passed through ion exchange bed 1450, the flow rate of said slip stream is sized to maintain sufficiently low ionic concentration in the cooling water. Because the cooling water typically passes over electrically charged surfaces within the PEMFC, it is important that the cooling water have a high electrical resistance, but it is not essential that the cooling water be of ultra-high purity with respect to ionic and non-ionic content.

It is also important to maintain acceptable levels of purity in the feed water that is to be used within fuel processor 1012 so that the steam- reforming catalysts within the fuel processor are not poisoned and rendered non-effective. Fig. 36 shows activated carbon bed 1500 and ion exchange bed 1502 placed in feed water stream 1022 for the purpose of purifying the feed water of ionic and organic contaminants. The now purified feed water stream 1510 is then admitted into fuel processor 1012. Activated carbon bed 1500 removes organic impurities from feed water stream 1022. Such organic impurities may originate from a variety of sources including, but not limited to, combustion byproducts that are exhausted from fuel processor 1012 and carried in exhaust stream 1064 to condenser 1066, and from there into condensed liquid water stream 1069. Ion exchange bed 1502 comprises both cation- exchange resins and anion-exchange resins, thereby removing both cations and anions from feed water stream 1022. Ionic contamination of feed water stream 1022 may originate from a variety of sources including, but not limited to, corrosion of metallic wetted surfaces in the combustion exhaust line carrying exhaust stream 1064, condenser 1066, the line carrying condensed liquid water stream 1069 to water reservoir 1016, and water reservoir 1016. The

incorporation of ion exchange bed 1502 allows the use of materials that are not especially corrosion resistant, but exhibit good thermal conductivity and relatively low cost, for the aforementioned wetted parts of the system, thereby improving the performance of condenser 1066 and reducing the cost of the system.

While the invention has been disclosed in its preferred form, the specific embodiments thereof as disclosed and illustrated herein are not to be considered in a limiting sense as numerous variations are possible. Applicants regard the subject matter of the invention to include all novel and non-obvious combinations and subcombinations of the various elements, features, functions and/or properties disclosed herein. No single feature, function, element or property of the disclosed embodiments is essential. The following claims define certain combinations and subcombinations which are regarded as novel and non-obvious. Other combinations and subcombinations of features, functions, elements and/or properties may be claimed through amendment of the present claims or presentation of new claims in this or a related application.

Such claims, whether they are broader, narrower or equal in scope to the original claims, are also regarded as included within the subject matter of applicants'invention.