Undersea vehicle and method for operating the same

Abstract

The present invention includes an underwater vehicle power unit and method of operating the same comprising: a fuel and waste stack comprising one or more reactant or fuel storage bladders and one or more waste storage bladders that are volumetrically and gravitationally balanced during operation; a fuel reactor that generates hydrogen; a fuel cell capable of generating an electrical current when exposed to hydrogen; and a controller that controls the flow of fuel into the hydrogen generator, the flow of hydrogen into the fuel cell and the flow of waste from the hydrogen generator, and/or the fuel cell into the one or more waste storage bladders.

Claims

1. An underwater vehicle power unit comprising: a fuel and waste stack comprising one or more reactant or fuel storage bladders and one or more waste storage bladders that are volumetrically and gravitationally balanced during operation; a fuel reactor that generates hydrogen; a fuel cell capable of generating an electrical current when exposed to hydrogen; and a controller that controls the flow of fuel into the fuel reactor, the flow of hydrogen into the fuel cell and the flow of waste from the fuel reactor, and/or the fuel cell into the one or more waste storage bladders.

2. The power unit of claim 1, further comprising one or more heat sinks in communication with the at least one of the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders.

3. The power unit of claim 2, wherein the heat sink surrounds at least one of the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders.

4. The power unit of claim 1, further comprising one or more pumps and valves between the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders controlled by the controller and that manage the flow of fuel, hydrogen, and waste to maintain the underwater vehicle gravimetrically balanced during dive or surfacing operations.

5. The power unit of claim 1, further comprising a water recirculation system connected to the fuel cell, wherein water generated from the fuel cell is used to at least one of cool the fuel reactor or the fuel cell, or dilute a fuel.

6. The power unit of claim 1, further comprising a battery that powers one or more pumps and valves when the fuel cell is not generating an electrical current.

7. The power unit of claim 1, wherein the fuel and waste stack is defined further as comprising interleaved reactant or fuel storage bladders and waste storage bladders.

8. The power unit of claim 1, wherein the reactant or fuel storage bladders and waste storage bladders are cylindrical, ovoidal, pancake shaped, accordion shaped, tubular, polygonal, cubic, spherical, pyramidal, rhomboid, conical, or half-cylinders that sandwich an expandable bladder.

9. The power unit of claim 1, wherein the fuel cell is defined further as comprising one or more membrane electrode assemblies, one or more bipolar plates, one or more seals and structural end plates.

10. The power unit of claim 1, further comprising an oxidizer that provides OX product water to the fuel cell, wherein the oxidizer is further defined as comprising a peroxide pump, a flow meter, a heat exchanger, a back pressure regulator, a phase separator, an accumulator and a forward pressure regulator.

11. The power unit of claim 10, further comprising a back-pressure regulator between the oxidizer and the fuel cell.

12. The power unit of claim 1, further comprising one or more heat sources at one or more locations proximate to an inlet to the fuel reactor between the reactant or fuel storage bladders and waste storage bladders to prevent precipitation of reactants, byproducts, and/or waste in the power unit.

13. The power unit of claim 1, wherein a reactant for use in the fuel cell is a metal-hydride.

14. The power unit of claim 1, wherein a reactant for use with the fuel reactor is selected from at least one of NaBH.sub.4, LiBH.sub.4, KBH.sub.4, Ca(BH.sub.4).sub.2, or Mg(BH.sub.4).sub.2.

15. A method of powering an underwater vehicle with a power unit comprising: providing a fuel and waste stack comprising one or more reactant or fuel storage bladders and one or more waste storage bladders that are volumetrically and gravitationally balanced during operation; connecting the reactant or fuel storage bladders to a fuel reactor that generates hydrogen; connecting the output from the fuel reactor to a fuel cell capable of generating an electrical current when exposed to hydrogen; and connecting a controller that controls the flow of fuel to the fuel reactor, the flow of hydrogen to the fuel cell, and the flow of waste from the fuel reactor and/or the fuel cell to the one or more waste storage bladders.

16. The method of claim 15, further comprising providing one or more heat sinks in communication with the at least one of the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders.

17. The method of claim 16, wherein the heat sink surrounds at least one of the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders.

18. The method of claim 15, further comprising providing one or more pumps and valves between the one or more fuel storage bladders, the fuel reactor, the fuel cell, or the one or more waste bladders controlled by the controller and that manage the flow of fuel, hydrogen, and waste to maintain the underwater vehicle gravimetrically balanced during dive or surfacing operations.

19. The method of claim 15, further comprising connecting a water recirculation system connected to the fuel cell, wherein water generated from the fuel cell is used to at least one of cool the fuel reactor or the fuel cell, or dilute a fuel.

20. The method of claim 15, further comprising providing a battery that powers one or more pumps and valves when the fuel cell is not generating an electrical current.

21. The method of claim 15, wherein the fuel and waste stack is defined further as comprising interleaved reactant or fuel storage bladders and waste storage bladders.

22. The method of claim 15, wherein the reactant or fuel storage bladders and waste storage bladders are cylindrical, ovoidal, pancake shaped, accordion shaped, tubular, polygonal, cubic, spherical, pyramidal, rhomboid, conical, or half-cylinders that sandwich an expandable bladder.

23. The method of claim 15, wherein the fuel cell is defined further as comprising one or more membrane electrode assemblies, one or more bipolar plates, one or more seals and structural end plates.

24. The method of claim 15, further comprising an oxidizer that supplies OX product water to the fuel cell, wherein the oxidizer is further defined as comprising a peroxide pump, a flow meter, a heat exchanger, a back pressure regulator, a phase separator, an accumulator and a forward pressure regulator.

25. The method of claim 24, further comprising providing a back-pressure regulator between the oxidizer and the fuel cell.

26. The method of claim 15, further comprising providing one or more heat sources at one or more locations proximate to an inlet to the fuel reactor between the reactant or fuel storage bladders and waste storage bladders to prevent precipitation of reactants, byproducts, and/or waste in the power unit.

27. The method of claim 15, wherein a reactant for use in the fuel cell is a metal-hydride.

28. The method of claim 15, wherein a reactant for use with the fuel reactor is selected from at least one of NaBH.sub.4, LiBH.sub.4, KBH.sub.4, Ca(BH.sub.4).sub.2, or Mg(BH.sub.4).sub.2.

29. The method of claim 15, further comprising the step of maximizing a fill volume and even distribution of one or more reactants by pre-inflating the two or more reactant or fuel storage bladders with gas.

30. The method of claim 15, further comprising the step of filling the two or more reactant or fuel storage bladders with reactants while the gas is removed from a headspace via a vent in the two or more reactant or fuel storage bladders at the same volumetric rate, to prevent the bladder from sagging.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) For a more complete understanding of the features and advantages of the present invention, reference is now made to the detailed description of the invention along with the accompanying figures and in which:

(2) FIG. 1 is a graph that shows the solubility of aqueous sodium borohydride and sodium borate as a function of temperature.

(3) FIG. 2 is a graph that shows the effective gravimetric and volumetric storage of hydrogen vs. NaBH.sub.4 wt % at 20 C.

(4) FIG. 3 is a graph that shows theoretical NaBH.sub.4 reactor outlet parameters vs. back-pressure assuming inlet conditions of 20 wt % NaBH.sub.4, 20C, 100% hydrolysis reaction conversion and adiabatic conditions.

(5) FIG. 4 is a graph that presents the stoichiometric and thermodynamically compensated relationship between the NaBH.sub.4 feed concentration and NaBO.sub.2 outlet concentration for an adiabatic reactor operating at 60 psig.

(6) FIG. 5 is a diagram that shows the water management between the various sub-systems in terms of moles of water.

(7) FIG. 6 is a graph that shows NaBH.sub.4 and NaBO.sub.2 wt % as a function of moles of water (in reference to Equations 2-8).

(8) FIG. 7 is a graph that shows NaBO.sub.2 concentration at the storage vessel and NaBH.sub.4 diluted concentration at the reactor inlet as a function of NaBH.sub.4 storage concentration.

(9) FIG. 8 is a block diagram that shows a system for level water management of the present invention.

(10) FIG. 9 is a block diagram of the fuel intra-subsystem water recovery technique. Two phase separators and a heat exchanger/condenser are used to separate the un-usable borate byproduct from the usable condensed product water.

(11) FIG. 10 is a block diagram of the H.sub.2O.sub.2 intra-subsystem water recovery technique.

(12) FIG. 11 is a diagram that shows multiple fluid containers with flow restrictors between the multiple fluid containers that dampen fluid movement during pitch and/or roll maneuvers.

(13) FIG. 12 is a diagram which shows that adding relatively large value resistance to parallel flow lines reduces the effect of minor differences.

(14) FIG. 13 is a diagram that shows an asymmetric layout results in horizontal CG shift if reactants are not of similar density and/or volume.

(15) FIG. 14 is a diagram that shows a pancake bladder configuration with alternating reactant/waste pairs

(16) FIG. 15 is a diagram that shows side-by-side bladder configuration with reactant in purple and waste in orange (exploded view). Gray cylinder is for bladder installation and shows conduit passing through center.

(17) FIG. 16 is a cross-sectional side view of a perforated tube vent with internal stiffener can be installed through a small port and configured for best access to high points in the container for gas removal.

(18) FIG. 17 shows a diagram of one embodiment of the hydrogen generator of the present invention.

(19) FIG. 18 shows an example of a reactor design for generating H.sub.2 for use with the present invention.

(20) FIG. 19 shows an example of a fluid management between fuel/water storage and hydrolysis reactor via the conduit system for use with the present invention.

(21) FIG. 20A shows an example of a reactor water recovery by phase separation of the present invention.

(22) FIG. 20B shows an example of a reactor water recovery by phase separation of the present invention.

(23) FIG. 21A shows an example of a water reservoir system for use with the present invention.

(24) FIG. 21B shows an example of a float type continuous level sensor for use with the present invention.

(25) FIGS. 22A and 22B are graphs that show the product as a weight percent wt % of the NaBH.sub.4 and NaBO.sub.2, in relation to: FIG. 22A the wt % of reactant NaBH.sub.4, and in FIG. 22B the wt % of the reactant H.sub.2O.sub.2.

DETAILED DESCRIPTION OF THE INVENTION

(26) While the making and using of various embodiments of the present invention are discussed in detail below, it should be appreciated that the present invention provides many applicable inventive concepts that can be embodied in a wide variety of specific contexts. The specific embodiments discussed herein are merely illustrative of specific ways to make and use the invention and do not delimit the scope of the invention.

(27) To facilitate the understanding of this invention, a number of terms are defined below. Terms defined herein have meanings as commonly understood by a person of ordinary skill in the areas relevant to the present invention. Terms such as a, an and the are not intended to refer to only a singular entity, but include the general class of which a specific example may be used for illustration. The terminology herein is used to describe specific embodiments of the invention, but their usage does not delimit the invention, except as outlined in the claims.

(28) Effective Gravimetric and Volumetric Storage of Aqueous NaBH.sub.4.

(29) Typically, fuel cells are used for low mass and/or low volume applications. This is primarily due to the high relative efficiency of the fuel cell and separation of the reactants from the power generation device (fuel cell). Specifically, proton exchange membrane (PEM) fuel cells require hydrogen gas as a fuel. Effective mass and volume storage of the hydrogen is currently a major barrier for the viability of fuel cells. Chemical hydrides, which store hydrogen in a chemical compound for effective mass and volumetric storage, have become a promising solution. A great deal of investigation has been performed on Sodium Borohydride (NaBH.sub.4) specifically due to its high gravimetric hydrogen wt %, purity, and the high stability and solubility of the compound in an aqueous solution. NaBH.sub.4 reacts with water to form hydrogen gas and Borate while releasing heat (Equation 1).
NaBH.sub.4+(2)H.sub.2O.fwdarw.NaBO.sub.2(4)H.sub.2+212 kJEquation 1

(30) As can be seen by the reaction, the ideal ratio of NaBH.sub.4 to water is 1:2 moles respectively, or 51 wt % of NaBH.sub.4. Since NaBH.sub.4 may be stored with a relatively high stability as an aqueous solution, catalytic reactors are used to generate the hydrogen on demand. FIG. 1 is a graph that shows the solubility of aqueous sodium borohydride and sodium borate as a function of temperature.

(31) However, the solubility of the byproduct, borate, is significantly less soluble than the reactant, NaBH.sub.4 (FIG. 1). To make matters worse, water is consumed during the reaction, reducing the amount of water to solubilize the byproduct. If the maximum solubility is exceeded during the reaction inside the reactor, solid crystals are formed which physically damage the reactor due to clogging and catalyst erosion. Therefore, the maximum solubility of the reactant, NaBH.sub.4, can never be realized in storage as the solubility of the byproduct, Borate, limits the NaBH.sub.4 feed concentration. This is problematic since the goal of using NaBH.sub.4 in the first place is to increase the gravimetric and volumetric storage of hydrogen. FIG. 2 is a graph that shows the effective gravimetric and volumetric storage of hydrogen vs. NaBH.sub.4 wt % at 20 C.

(32) The present inventors have developed specific solutions to increase the effective storage concentration of aqueous NaBH.sub.4 that addresses the issue of reduced NaBO.sub.2 solubility.

(33) Solution ABack Pressure Regulator (Effects all NaBH.sub.4 Reactors).

(34) Even though fully soluble NaBH.sub.4 solutions are fed into the reactor, the byproduct, NaBO.sub.2, can crash out of solution, crystallizing and in the process damaging the reactor due to the limited solubility. Solubility of the byproduct is dependent upon the amount of liquid water available and the temperature of the system (FIG. 1). Although the solubility of the byproduct cannot be changed, the temperature and available liquid water fraction may be somewhat controlled. Most often, the reactor will operate under adiabatic conditions to simplify the reactor design by eliminating the necessity of a cooling system. In this adiabatic case, the outlet temperature of the reactor may be calculated from the inlet temperature and system pressure alone, assuming complete reaction (FIG. 3). Therefore, assuming a room temperature inlet, only the temperature and thus back-pressure of the reactor affects the solubility of the byproduct. During operation, increasing the pressure increases the temperature and the available liquid water, both improving the solubility of the byproduct (NaBO.sub.2). To overcome this problem, which was verified both theoretically (via thermodynamics) and experimentally, the present inventors added a back-pressure regulator downstream of the reactor. This physical addition insures that the reaction takes place at an elevated pressure, regardless of flow rate or H.sub.2 production rate, reducing the concentration of the byproduct, NaBO.sub.2, thus substantially increasing reactor lifetime. FIG. 3 is a graph that shows theoretical NaBH.sub.4 reactor outlet parameters vs. back-pressure assuming inlet conditions of 20 wt % NaBH.sub.4, 20C, 100% hydrolysis reaction conversion and adiabatic conditions.

(35) Solution BPre-Heating Fluid with HX (Effects all NaBH.sub.4 Reactors).

(36) As shown previously in FIG. 3, increasing the pressure will increase the outlet temperature. However, the increased outlet temperature does not directly solve the byproduct solubility issue. The steady state operational reactor will have a thermal gradient from the inlet temperature to the outlet temperature. Therefore, even though the borate at the outlet of the reactor will be fully soluble, some reaction, forming borates, will occur near the colder inlet of the reactor. The existence of borates at these localized cold spots can locally damage the reactor with a cumulative effect. Eventually, the reaction zone will shift from the inlet of the reactor towards the outlet as the cold spots and thus degradation propagates through the reactor. Under these conditions, the reactors life will be quite short. However, this degradation mechanism may be significantly reduced with intelligent control of the inlet feed concentration and temperature. FIG. 4 is a graph that shows the relationship between NaBH.sub.4 feed concentration and NaBO.sub.2 outlet concentration for an adiabatic reactor operating at 60 psig. If the inlet temperature is increased from 20 to 40 C., the limiting feed concentration of NaBH.sub.4 may be increased from 10.8 to 14.6 wt % respectively, while maintaining full solubility of the borate byproduct at inlet cold spots.

(37) FIG. 4 is a graph that shows the stoichiometric and thermodynamically compensated relationship between the NaBH.sub.4 feed concentration and NaBO.sub.2 outlet concentration for an adiabatic reactor operating at 60 psig. Also illustrated is the solubility limit of NaBO.sub.2 at both 20 and 40 C. This gives a surprising insight that the NaBH.sub.4 feed concentration may be increased substantially while maintaining full solubility of the NaBO.sub.2 if the inlet temperature is increased. To overcome this problem, which was verified both theoretically (via thermodynamics) and experimentally, the present inventors insulated and preheated the reactor feed stream with electric heaters on startup and a novel integrated reactor heat exchanger during steady state operation. These physical additions insure that the NaBO.sub.2 byproduct is fully soluble at localized cold spots during startup and steady state operation, thus substantially increasing reactor lifetime.

(38) Solution CSystem Level Water Management.

(39) Storing NaBH.sub.4 at elevated concentrations, or even in the solid form, would result in increased gravimetric and volumetric energy storage. However, above the ideal stoichiometric 51 wt %, not enough water is available for the reaction. Additionally, water limitations may cause the byproduct to crystallize in the reactor or in the waste storage vessel making it difficult to remove, requiring even lower feed concentrations (see FIG. 4). Many others have already investigated the idea of using wastewater from other parts of the system (for example fuel cell product water) for diluting the NaBH.sub.4 either prior to or after the reactor. While the skilled artisan would expect the implementation of this water utilization design to become cumbersome and even dangerous, the present inventors demonstrate herein the advantages of this configuration and overcoming those challenges. The present inventors recognized the need for additional water in the NaBH.sub.4 hydrolysis reaction, determined that a system level water management strategy is necessary. As such, the present inventors evaluated several fuel and oxidizer combinations for a PEM fuel cell and determined that the specific combination of NaBH.sub.4 and H.sub.2O.sub.2 offers an attractive couple based specifically on water management. FIG. 5 is a diagram that shows the water management between the various sub-systems in terms of moles of water. In FIG. 5, the system level water management strategy is shown as flow chart 10, which shows an oxidizer 12 from which the OX product water (4+y) H.sub.2O is combined with the fuel 14. The FC product water is obtained from Fuel Cell 14, with a reactant storage 18, in communication with the fuel 16. The waste return for the fuel 16 is L (x2) H.sub.2O, while the reactant storage 18 provides aqueous sodium borohydride that supplies (x) H.sub.2O. The Reactant storage 18 is also in communication with oxidizer 12, to which is provides an aqueous peroxide supply of (y) H.sub.2O.

(40) Equations 2-4 show the system balanced stoichiometric chemical reactions for each step of the overall system. Equation 2 represents the NaBH.sub.4 fuel hydrolysis reaction, which includes parameter x for water used to solubilize the reactants and products. Specifically, x is used to quantify the amount of water used to solubilize the NaBH.sub.4 during storage and y is used to quantify the water used to dilute the hydrogen peroxide during storage. It should also be noted that 212 kJ of heat is released during this reaction. Equation 3 represents the hydrogen peroxide decomposition reaction. 392 kJ of heat is released during this reaction. Equation 4 represents the PEM fuel cell reaction, which releases a total energy of 1143 kJ. However, it should be noted that approximately half of this energy will be released as heat where as the other half will be transformed into electrical energy by the fuel cell assuming that the fuel cell is 50% efficient based on total available enthalpy.

(41) $\begin{array}{cc}\mathrm{Fuel}\mathrm{Reaction}{\mathrm{NaBH}}_4+\left(x\right)H_2{O}_{\left(l\right)}.fwdarw.{\mathrm{NaBO}}_2+\left(4\right)H_2+\left(x-2\right)H_2{O}_{\left(l\right)}+212{\mathrm{kJ}}_{\mathrm{heat}}.& \mathrm{Equation}2\\ \mathrm{Oxidizer}\mathrm{Reaction}\left(4\right)H_2{O}_{2\left(l\right)}+\left(y\right)H_2{O}_{\left(l\right)}.fwdarw.\left(4+y\right)H_2{O}_{\left(l\right)}+\left(2\right)O_2+392{\mathrm{kJ}}_{\mathrm{heat}}.& \mathrm{Equation}3\\ \mathrm{Fuel}\mathrm{Cell}\mathrm{Reaction}\left(4\right)H_2+\left(2\right)O_2.fwdarw.\left(4\right)H_2{O}_{\left(l\right)}+572{\mathrm{kJ}}_{\mathrm{heat}}+572{\mathrm{kJ}}_{\mathrm{electrical}}.& \mathrm{Equation}4\\ \mathrm{Overall}\mathrm{System}\mathrm{Reaction}{\mathrm{NaBH}}_4+\left(4\right)H_2{O}_{2\left(l\right)}+\left(x+y\right)H_2{O}_{\left(l\right)}.fwdarw.{\mathrm{NaBO}}_2+\left(6+x+y\right)H_2{O}_{\left(l\right)}+1176{\mathrm{kJ}}_{\mathrm{heat}}+572{\mathrm{kJ}}_{\mathrm{electrical}}.& \mathrm{Equation}5\\ \mathrm{Fuel}\mathrm{reaction}\mathrm{with}\mathrm{full}\mathrm{water}\mathrm{utilization}\text{.Math.}\left(\mathrm{from}\mathrm{Oxidizer}\mathrm{and}\mathrm{fuel}\mathrm{cell}\right){\mathrm{NaBH}}_4+\left(8+x+y\right)H_2{O}_{\left(l\right)}.fwdarw.{\mathrm{NaBO}}_2+\left(4\right)H_2+\left(6+x+y\right)H_2{O}_{\left(l\right)}+212{\mathrm{kJ}}_{\mathrm{heat}}.& \mathrm{Equation}6\\ \mathrm{Fuel}\mathrm{byproduct}\mathrm{concentration}\mathrm{assuming}\text{.Math.}\mathrm{full}\mathrm{water}\mathrm{utilization}\mathrm{Wt}\%{\mathrm{NaBO}}_{2\left(\mathrm{aq}.\right)}=\frac{{\mathrm{NaBO}}_2}{{\mathrm{NaBO}}_2+\left(6+x+y\right)H_{2}O}=\frac{65.8}{65.8+\left(6+x+y\right)18}\mathrm{Wt}\%.& \mathrm{Equation}7\\ \mathrm{Fuel}\mathrm{reactor}\mathrm{feed}\mathrm{concentration}\mathrm{assuming}\mathrm{full}\mathrm{water}\mathrm{utilization}\mathrm{Wt}\%{\mathrm{NaBH}}_{4\left(\mathrm{aq}.\right)}=\frac{{\mathrm{NaBH}}_4}{{\mathrm{NaBH}}_4+\left(8+x+y\right)H_{2}O}=\frac{37.8}{37.8+\left(8+x+y\right)18}\mathrm{Wt}\%.& \mathrm{Equation}8\\ \mathrm{Overall}\mathrm{System}\mathrm{Efficiency}\mathrm{based}\mathrm{on}\mathrm{total}\mathrm{Enthalpy}\left(\mathrm{HHV}\right){}_{\mathrm{electrical}}=\frac{{\mathrm{Energy}}_{\mathrm{electrical}}}{{\mathrm{Energy}}_{\mathrm{Total}}}=\frac{572\mathrm{kJ}}{572\mathrm{kJ}+1176\mathrm{kJ}}=33\%.& \mathrm{Equation}9\end{array}$

(42) If Equation 2-4 are condensed into one overall system equation, the result is Equation 5 which may be used to calculate the final NaBO.sub.2 storage concentration assuming that all of the product water is mixed with the waste (Equation 7). However, if this product water is mixed with the NaBH4 fuel prior to the reactor feed, Equation 2 turns into Equation 6, which may be used to calculate the reactor feed concentration (Equation 8). Another interesting observation from Equation 5 is that the overall system efficiency based off of total available enthalpy is 33% (Equation 9).

(43) Although pure 100 wt % H.sub.2O.sub.2 is available, shipping and safety regulations can limit the practical concentration of H.sub.2O.sub.2 to 59 wt %. Therefore, 59 wt % H.sub.2O.sub.2 was used for the following calculations as it represents one practical maximum concentration. The skilled artisan will recognize, using the teachings herein, that the wt % of the H.sub.2O.sub.2 can be varied based on the equations above to use any wt % necessary to achieve the required reactant. For example, the wt % of H.sub.2O.sub.2 can be used at 20, 30, 40, 50, 55, 59, 60, 61, 62, 64, 65, 70, 75, 80, 85, 90, 95, or 100 wt % and the moles can be varied accordingly. For these calculations, with 59 wt % H.sub.2O.sub.2, y=1.31 moles, which was used as a constant. This results in the only variable in the relations being x. Therefore, the final NaBO.sub.2 concentration may be plotted as a function of x (or storage NaBH.sub.4 wt %). FIG. 6 is a graph that shows NaBH.sub.4 and NaBO.sub.2 wt % as a function of moles of water (in reference to Equations 2-8), y=1.31. FIG. 7 is a graph that shows NaBO.sub.2 concentration at the storage vessel and NaBH.sub.4 diluted concentration at the reactor inlet as a function of NaBH.sub.4 storage concentration. All the product water from the fuel cell and H.sub.2O.sub.2 reaction can be used for the fuel reaction. Based on this relation, enough water is theoretically available even if solid anhydrous NaBH.sub.4 is stored. At 20 C., the solubility of NaBH.sub.4 is 35 wt %, therefore enough water is available to dissolve all of the solid NaBH.sub.4 into an aqueous solution for fluidic delivery to the fuel reactor. If a fully soluble waste product is desired at 20 C., 21 wt % NaBO.sub.2 must be maintained which limits the NaBH.sub.4 storage to 26 wt %, y=1.31.

(44) Both NaBH.sub.4 and NaBO.sub.2 concentrations may be seen in FIG. 6 as a function of x (Moles of water stored with NaBH.sub.4) and in FIG. 7 as a function of NaBH.sub.4 weight percent (wt %) used for storage. Both FIGS. 6 and 7 assume that all the product water from the fuel cell and H.sub.2O.sub.2 reaction is used for the fuel reaction (full water utilization). Based on this relation, enough water is theoretically available even if solid anhydrous NaBH.sub.4 is stored. At 20 C., the solubility of NaBH.sub.4 is 35 wt %, therefore enough water is available to dissolve all of the solid NaBH.sub.4 into an aqueous solution for fluidic delivery to the fuel reactor. If a fully soluble waste product is desired at 20 C., 21 wt % NaBO.sub.2 must be maintained which limits the NaBH.sub.4 storage to 26 wt %.

(45) FIG. 8 shows a block diagram of the system for level water management 30 of the present invention. The oxidizer 12 that provides OX product water and the fuel cell 14 that provides fuel cell product water, are depicted. These connect to a fuel subsystem 32, which is a common recaptured water reservoir 34, which is used account for delivery transients. This allows for a continuous flow of water to be delivered to the reactor 36, avoiding transient concentration shifts. The rate of water dilution is controlled with a specialized water level feedback loop, which prevents the water reservoir from emptying or overfilling while insuring a minimum threshold fuel dilution and full system level water utilization. A specialized mixing chamber 38 is also used to reduce the possibility of concentrated NaBH.sub.4 solutions from entering the reactor. The reactant, e.g., concentrated NaBH.sub.4, is obtained from the reactant storage containers 40, one of which can provide hydrogen peroxide 42.

(46) The present inventors obtained full water utilization with the NaBH.sub.4/H.sub.2O.sub.2 couple via unique water recapture, storage and subsequent dilution strategies. Custom phase separators are used to capture the liquid product water from the oxidizer reactor, fuel cell anode and fuel cell cathode safely without permitting any entrained gas. This captured water is then delivered to a temporary water storage reservoir to account for system transients. The water is then pumped from the system level water reservoir and mixed with the fuel stream prior to delivery to the fuel reactor. The rate of water dilution is controlled with a specialized feedback loop, which prevents the water reservoir from emptying or overfilling while insuring a minimum threshold fuel dilution and full system level water utilization.

(47) Solution DFuel/Oxidizer Intra-Subsystem Water Recovery.

(48) Although utilizing this unique system level water management approach (discussed previously) theoretically yields enough liquid water to fully solubilize solid anhydrous NaBH.sub.4, this precise water balance is difficult to achieve in practice. These difficulties are a result of system transients, thermal imbalances and practical accuracies/controls of flow meters and pumps (especially at very small volumetric rates).

(49) Any additional water that may be recaptured and used to dilute the feed streams is useful for both the fuel and oxidizer reactors. As discussed previously, reducing the fuel reactor feed concentration reduces the chances of borate (by-product) precipitation, which leads to reactor damage and diminished lifetime. However, the hydrogen peroxide reactor may also benefit from reduced inlet concentrations with increased lifetimes.

(50) One of the primary H.sub.2O.sub.2 reactor degradation mechanisms is contamination from the stabilizers used in the H.sub.2O.sub.2 itself. Lack of available liquid water throughout the H.sub.2O.sub.2 reaction can lead to precipitation of the stabilizer (commonly Potassium or Sodium Stannate) onto the catalyst, thus reducing catalytic activity. Similar to the fuel reaction, more liquid water is available when utilizing lower concentrations of H.sub.2O.sub.2 and when running at higher pressures with a BPR. Additionally, the H.sub.2O.sub.2 reaction can see localized and transient water shortages (caused by flow pulsations) again leading to stagnation and precipitation of the stabilizer. For these reasons, adding additional water to the inlet of the H.sub.2O.sub.2 reactor and diluting the H.sub.2O.sub.2 concentration results in longer lifetimes.

(51) However, due to the need for additional water by both the fuel and oxidizer subsystems, a decision must be made on which subsystem needs what allocations of water. This decision primarily depends on the relative storage concentrations of the NaBH.sub.4 and H.sub.2O.sub.2 solutions. However, two unique intra-subsystem water recovery techniques may be used by both subsystems simultaneously without affecting the overall system level water balance.

(52) For the fuel subsystem, additional product water was obtained by implementing a two-stage phase separation (see FIG. 9). The first stage of phase separation occurs at high temperature (>100 C.). As used herein, high temperature in the hydrogen/liquid separator is >100 C., for example 105, 110, 115, 120, 125 C. This removes the solubilized byproduct (borate solution) for subsequent waste storage. Saturated hydrogen gas then travels out of the top of the high temperature phase separator through a heat exchanger, cooling and condensing the saturated vapor down to 60 C. As used herein, low temperature in the hydrogen/liquid separator is 50 to 90 C., for example 55, 60, 65, 70, 75, 80, 85, or 90 C. The two phase liquid/gas mixture then enters the low temperature phase separator where the liquid water may be captured and drained into a common liquid water storage tank (common to the other sources of recaptured water previously discussed). From there the water can be feed continuously back into the fuel reactor, thus further reducing the reactor inlet concentration. FIG. 9 is a block diagram 50 of the fuel intra-subsystem water recovery technique. Two phase separators and a heat exchanger/condenser are used to separate the un-usable borate byproduct from the usable condensed product water. A reactant, depicted in this example as concentrated NaBH.sub.4 is provided via a delivery pump 52, which reactant enters reactor 54. Water produced at the reactor 54 enters a high temperature phase separator 56, which is saturated with hydrogen and enters a heat exchanger/condenser 58. The saturated hydrogen and condensed water then enters a low temperature phase separator 60, which separates the product hydrogen gas 62 from the recovered condensed water. The recovered condensed water enters the recovered liquid water storage reservoir 64, which can be pumped back into the reactor at recovered water delivery pump 66. The high temperature phase separator 56, separates the saturated hydrogen from the liquid waste, which is stored in liquid waste storage 68.

(53) Within the oxidizer subsystem, a unique water recirculation loop was used that is fundamentally different than the fuel subsystems (see FIG. 10). Since the H.sub.2O.sub.2 decomposition reaction has no products other than oxygen gas and water, the two-phase separator approach is not needed. The product stream from the reactor is fed directly into the heat exchanger where additional water vapor is condensed at 60 C. Subsequently the two phase mixture is separated so that the liquid water may be both delivered to the fuel subsystem (as previously described) and re-circulated to the H.sub.2O.sub.2 reactor for additional dilution. Although the fuel intra-subsystem water recovery rate is limited by the enthalpy released by the hydrolysis reaction (this limits the amount of condensate recovered), the H.sub.2O.sub.2 re-circulation rate is theoretically unlimited and has no net effect on the rate of product water delivered to the fuel subsystem. This is realized since any liquid water removed from the phase separator and delivered to the reactor eventually ends up back in the phase separator. This allows the system to accurately control the H.sub.2O.sub.2 concentration at the reactor inlet without affecting the overall system level water balance. FIG. 10 is a block diagram 70 of the H.sub.2O.sub.2 intra-subsystem water recovery technique. A concentrated H.sub.2O.sub.2 is delivered by H.sub.2O.sub.2 pump 72, which concentrated H.sub.2O.sub.2 enters reactor 54. The reactor 54 generates a saturated oxygen and liquid water mixture, which enter heat exchanger/condenser 74. A saturated oxygen and additional condensed water exits the heat exchanger/condenser 74 and enters a low temperature phase separator 76. A product oxygen gas 78 is produced by the low temperature phase separator 76 with the net product liquid water delivered to the fuel subsystem 80. The recovered condensed water can be re-circulated liquid water that enters the re-circulated liquid water delivery pump 82, which fees the reactor 54. In one non-limiting example, the present inventors used the two aforementioned intra-subsystem water recovery techniques to further reduce both the NaBH.sub.4 and H.sub.2O.sub.2 reactor inlet concentrations, significantly increasing reactor lifetime.

(54) Bladder Manifold Management.

(55) When aqueous NaBH.sub.4 is selected as the hydrogen source of fuel for a power system, there are typically constraints on system mass and/or volume that lead to this selection because of its high gravimetric hydrogen wt %. In such an application, the oxygen source may be concentrated hydrogen peroxide (H.sub.2O.sub.2). NaBH.sub.4 produces NaBO.sub.2 as waste, and H.sub.2O.sub.2 produces water. In some cases, it is advantageous to retain the waste within the system until it is refueled, and to do so while limiting any shifts in center of gravity (CG) of the system.

(56) In the case of case of underwater vehicles, for example, maintaining constant system buoyancy may be critical to vehicles without active ballast control, and retaining all waste products in a closed system is the most straightforward method of doing so. Additionally, CG shifts can result in unacceptable changes in vehicle attitude, leading to reduced navigation control. In this case, it is important to have confidence that the power system CG will stay within a narrow range as reactants are converted to waste.

(57) Collapsible bladders for reactant and waste storage allow generated waste to fill the void left by consumed reactants. Their flexibility allows for adaptation to unique spaces and volumetric reactant-to-waste conversion ratios that deviate from 1:1. If the waste is more dense than the reactants consumed, it will simply fill its bladder more slowly than the reactant bladders collapse, or vice-versa. A rigid separation between the two volumes would not allow this expansion/contraction differential without additional compensating mechanisms. Although their flexibility is advantageous, collapsible bladders can result in unacceptable CG shifts if they do not fill or drain in a uniform or symmetric manner. Solutions to control or influence bladder filling/expansion and draining/collapse are discussed below.

(58) Solution ARestricted Fluid Movement Using Multiple Bladders as Baffles.

(59) When the energy system changes pitch or roll attitude, gravity will tend to cause the fluids to shift to lower space if any room is available. Additionally, differences in densities between the fluids (reactants and waste) can cause them to shift during system pitch roll so that less dense fluids move toward the new high point and more dense fluids move toward the new low point. In a vehicle, this means the CG shifts along the length of the vehicle, exaggerating pitch control inputs.

(60) Baffles spaced along the direction of attitude (i.e., along the length of the vehicle for pitched maneuvers) within the storage volume will slow down fluid shifting during short-term pitch or roll maneuvers, dampening the resultant CG shift. One implementation of storage containers that effectively baffles fluid flow is to divide the volume into multiple containers with flow restrictors between them. One example is to use multiple bladders connected in parallel to permit the contents to move between bladders, but with orifices or long lengths of small diameter tubing to slow that movement down to acceptable levels. FIG. 11 is a diagram that shows a restricted fluid movement using multiple bladders as baffles system 100, that shows multiple fluid containers 102a-c, with flow restrictors 104a,b between them to dampen fluid movement during pitch and/or roll maneuvers.

(61) Solution BEven Distribution of Flow Through a Manifold Using Flow Restrictions.

(62) Flow from a single source through parallel lines in a system will be inversely proportional to the relative resistance to flow in each line. In order to fill multiple containers evenly, the flow resistance from the source to each container must be identical. Any variations will result in uneven filling. With open containers or rigid containers having fluid communication between containers at the head and drain (top and bottom), levels will even out over time after filling is complete. With collapsible containers having fluid communication at the head and drain, the fluid level will tend to seek its own, but the container size will not necessarily adjust, so that one container may remain expanded more than another if it receives more flow during filling.

(63) Perfectly identical flow resistance in parallel is impossible to achieve, and differences may be significant in the case of collapsible containers because of constrictions or differences in resistance to expansion. Since the differences in flow are inversely proportional to flow resistance, one method to minimize differences is to place a large value of identical flow restriction in each parallel path. This reduces the relative impact of minor differences in resistance. For example, if two parallel lines had relative resistance of 1 and 1.5, the first line would receive 60% of flow and the other would receive 40%, a 20% difference. By adding resistance of 10 to each line, the lines would receive 51% and 49% each, only a 2% difference. For collapsible containers, minor resistances are difficult to avoid if the containers wrinkle or are constricted by adjacent components, so implementing a relatively large flow resistance reduces differences in filling or draining. This added resistance can also serve to limit flow between bladders as in Solution A. FIG. 12 is a diagram that shows an even distribution of flow through a manifold using flow restrictions system 110 and multiple fluid containers 102a-c, which shows that adding relatively large value resistance to parallel flow lines reduces the effect of minor differences using variable innate flow resistance 112a-c and added identical flow restrictors 114a-c in series, respectively.

(64) Solution CBalanced Reactant-to-Waste Transfer by Interleaved Bladders.

(65) When each reactant solution is stored in its own separate space, the CG of each section is in the centroid of the fluid volume. Depending on the relative densities and volumes of each reactant, the combined CG of the reactants may not be in the centroid of the combined fluid volume. Once all the reactants are consumed and converted to waste, if the waste is evenly distributed in the volume vacated by the consumed reactants, the CG of the waste will be at the centroid of the fluid volume because only a single fluid exists at that point. This movement in CG may exceed the operational limits of the vehicle or other system using the power system.

(66) To avoid CG movement from the beginning of power production until all reactants are consumed, the layout of reactants should be symmetrical. This can be accomplished by dividing the reactants into multiple containers and alternating them in the layout. Waste containers situated between the reactant bladders allow waste to fill the space vacated by the reactants and keeps a constant horizontal CG location regardless of waste density. FIG. 13 is a diagram that shows an asymmetric layout results in horizontal CG shift if reactants are not of similar density and/or volume. Subdividing containers for a symmetric layout maintains a constant horizontal CG location.

(67) Solution DPancake and Side-by-Side Bladder Configurations.

(68) Specifically in reference to cylindrical reactant/waste container volumes, two different collapsible container (bladder) layouts each offer unique features to address implementation concerns.

(69) The first configuration is composed of pancake bladders, stacked back-to-back along the axis of the cylinder. This layout permits small deflection of each individual bladder, resulting in predictable collapse and inflation geometry. It also permits implementation of Solution A (multiple bladders as baffles) and Solution C (symmetric layout) to minimize movement of the reactant/waste CG. The narrow aspect ratio also helps collect any offgas in the top of each bladder for ventilation purposes. The pancake design is amenable to other profiles, as well, since the overall shape can be fabricated to fit the geometry of the available space. Fabrication is straightforward since the bladders can be formed from two flat panels, sealed together around the perimeter. FIG. 14 is a diagram that shows a pancake bladder configuration 120 with alternating reactant/waste pairs 122. Suspension eyelets 124 are depicted that permit the bladders to be aligned on a frame (not depicted). Also shown are vent port(s) 126 and fill/drain ports 128. For example, the pancake bladder configuration 120 is depicted with alternating reactant/waste pairs 122, which alternate as follows: NaBH.sub.4 storage, Waste Storage, H.sub.2O.sub.2 storage, and waste storage, thereby providing gravity balance during operation of the pancake bladder configuration 120 system and the overall system, and the reactants are expended at about the relatively the same rate as the waste is generated.

(70) The second configuration is useful when fluid densities and volumes are similar enough that CG shifting along the cylinder axis is not a concern. This layout places bladders side-by-side along the axis of the cylinder. The orientation of the bladders parallel to the cylinder wall is conducive to the bladder filling the available volume. The reason for this is when a two-panel flat container is inflated, it tends to assume a round shape due to the even pressure of the contents applied to the container wall. For a rectangular bladder in a cylindrical space, this means the bladder will naturally conform to the inside diameter of the cylinder. The two primary benefits of this approach are 1) more efficient use of space for reactant storage, and 2) the cylinder supports the bladder, reducing stress on the bladder wall. Since the shape readily fills the volume, the number of containers required to use the space effectively is reduced. A single bladder could fill the cylindrical volume, but lateral symmetry is lost by having a single reactant container and a single waste container side-by-side. To maintain symmetry, two reactant containers and two waste containers can be situated on either side of the middle dividing line. A secondary benefit of this approach is it allows objects to extend through the middle of the reactant storage space, such as reinforcing tie-rods for the ends of the cylinder, or for cables, tubing, or a conduit. FIG. 15 is a diagram that shows side-by-side bladder configuration with reactant in purple and waste in orange (exploded view). Gray cylinder is for bladder installation and shows conduit passing through center.

(71) Filling process optimization. Aside from physical configuration of the bladders and tanks, taking specific process steps can help with balancing and maximizing fill volumes.

(72) The first step to maximize fill volume and even distribution is to pre-inflate the bladders with gas. The chief advantage of the gas pre-fill is that the weight of the gas does not restrict the motion of the bladders as they expand. When filling an empty bladder (gas removed by vacuum) the liquid tends to run to the bottom. As the liquid weight builds, it causes the bladder to sag and may trap bladder material at the bottom of the tank, limiting its ability to expand upward and outward. Pre-filling with gas expands the bag without sagging. Subsequently, the reactants can be filled while gas is removed from the headspace via a vent at the same volumetric rate, thereby maintaining the optimum form of the bladder.

(73) With the side-by-side bladder configuration, filling the interior bladders with reactants produces the most desirable result for space utilization. During the gas prefill, then interior bladders expand and flatten the exterior bladders against the outer wall of the tank. The collapsed bladders are designed to fit against the tank wall, so wrinkling and bunching are minimized. If the outer bladders are filled first, the inner bladders must crumple due to their excess material in the middle. This can result in voids and reduced tank volume utilization.

(74) Bladder Gas Head Management.

(75) As reactants and waste decompose, they generate gas. As this gas accumulates in the top of the bladders, it begins to pressurize the bladders and may lead to leaks or bursting. To relieve the gas build-up, vents are located high in the bladders. These vents are protected by hydrophobic, gas-permeable membranes to allow gas to escape while retaining liquids in the bladders. One embodiment of the vent is a small circular port mounted in the side of the bladder. This port functions effectively when the container volume is sufficiently oversized to allow a gas head to build up before significant pressure accumulates. If the liquid level rises above the vent, gas cannot escape, so any volume above the vent is not available for reactant storage. Additionally, the vent must be above the liquid level in all orientations experienced by the container for extended periods. Depending on the bladder design, it may not be desirable or possible to locate this port at the very top of the bladder. Finally, the vent area is limited by the size of the port, which can cause undesired gas flow restriction, prevent off-gas from escaping fast enough, or extend refueling times.

(76) An improved gas vent is formed by locating a perforated tube in the top of the bladder and covering this tube in hydrophobic, gas-permeable membrane. This vent is superior to a single port because it can be located in the extremes of the bladder and service multiple positions, so that the high points in multiple orientations always have access to the vent. Since it can access the high points more effectively, more volume can be used for liquid storage rather than wasted as gas headspace. Additionally, the vent area is no longer limited to the port size, so a larger vent area can be provided to reduce gas flow restriction. This vent can be mounted internally in the bladder during fabrication using loops, clips or other standard means, but installation may be desired after the bladder is formed. Placing a wire inside the perforated tube allows it to be shaped and held in the proper location after inserting it through a small port, permitting installation, removal, and replacement without cutting or replacing the bladder. FIG. 16 is a cross-sectional side view of a perforated tube vent system 150 with internal stiffener can be installed through a small port and configured for best access to high points in the container for gas removal. The bladder wall is depicted into which a pass-through fit 152 is attached that connects to the outside of the bladder. Inside the bladder the perforated tube vent system 150 includes a perforated tube 154 into which a wire 156 is inserted. A gas permeable film 158 surrounds the perforated tube 154 through which gas can flow.

(77) The reaction of alkali and alkali-earth metal hydrides with water can be used for the generation of hydrogen. A non-limiting list of hydrides (in an aqueous solution) for use with the present invention are the ternary hydrides including LiAlH.sub.4, NaAlH.sub.4, LiBH.sub.4 and NaBH.sub.4. Other ternary hydrides, such as Mg(AlH4).sub.2 and liquid Al(BH.sub.4).sub.3, can also be used with the present invention. Lithium, sodium and magnesium react directly with hydrogen, under commercially convenient pressures and temperature conditions, to form the binary metal hydrides LiH, NaH, and MgH.sub.2.

(78) Hydrogen Generation System. Sodium borohydride has high gravimetric hydrogen storage (amount of H.sub.2 produced per unit weight of materials). Borate is formed as a byproduct when sodium borohydride undergoes hydrolysis to release hydrogen. Depending on conditions such as temperature and pressure, the borate's solubility can lead to the formation of undesirable solids unless due consideration is given. These solids can produce inefficiencies in reactor function, which negatively affects hydrogen generation. The present invention includes a continuous H.sub.2 generator system to produce maximum hydrogen output using the highest effective storage concentration of sodium borohydride and, avoiding conditions where borate becomes insoluble. FIG. 17 is an embodiment of the hydrogen generator invention 901. The aqueous NaBH.sub.4 is kept in one or more storage reservoirs 902. The preferred hydride storage concentration is between 10 and 30 wt %, preferably between 20 and 25% wt % for storage temperatures as low as 0 C. The expanded range is still viable for storage temperatures down to 5 C. However, below this temperature, the upper limit of 30% has converged with the solubility limit, thus dramatically increasing the likelihood of precipitate formation within the stored NaBH.sub.4. The NaBH.sub.4 catalytic hydrolysis reactor 903 contains specialized catalysts with a high surface area that favor the hydrolysis of NaBH.sub.4. The reactor allows flow of NaBH.sub.4 solution through the reactor while retaining catalyst within the reactor beds. Additional water for the reaction (Eq 1) comes from a water reservoir 904. Water in the reservoir is supplied from several sources including (1) oxidizer water 905 from the oxidant production subsystem (Eq 3) (2) water 906 from a fuel cell (Eq 4) and (3) from water recovered from the output stream 907 of the catalytic hydrolysis reactor. Water is supplied from these sources to the water reservoir via fluid conduits. As the water in the reservoir is depleted, from use in the hydrogen generation system, the water is replenished at an equivalent rate with water from the aforementioned sources.

(79) Transfer of water and fuel from the storage reservoirs and into the hydrolysis reactor is via two separate pumps and conduit system that manages the reactant mixing flow regime into the catalytic reactor 910. In addition to pumps, conduit system 910 can contain, flow meters, pressure sensing devices, mixing zones, and check valves, as described later. The transfer pumps for water and fuel into the hydrolysis reactor are under variable control and are critical elements of the hydrogen generator control architecture. Fluid transfer conduits between the fuel and water reservoirs and the reactor incorporate bypass loops 911, 912. The bypass loops contains valves which divert flow away from the reactor and back into the original storage containers in short duration pulses in order to clear the pumps of stalls in flow rate. The fuel solution tends to have micro bubbles entrained in the liquid due to the relatively small rate of natural, unassisted hydrogen generation. Sodium hydroxide is added to the NaBH.sub.4 solution to stabilize the natural rate of NaBH.sub.4 breakdown and hydrogen off gassing but gas production is not eliminated completely. The pump is appropriately sized to accommodate flow with only liquid against the expected reactor pressure at the required flow rates. However, as the fuel pump encounters solution with bubbles, there is a risk of a stall in flow rate. Because the reactor is kept at a high pressure relative to the storage container, the pump has to work harder to pump at a certain flow rate and the risk of experiencing stalls due to bubbles is increased. Once a stall is detected by the flow meters, the bypass valves open momentarily to clear bubbles. By exposing the outlet of the pump to a lower pressure (storage containers), the pump is able to clear bubbles out of the pump head easily so that when the outlet returns to the high pressure line there is only liquid in the pump head and it can operate normally. While bubbles are more of a concern with the fuel solution, a bypass valve was also added to the water loop so that both pumps are protected from stalls due to bubbles.

(80) A high temperature phase separator is used to separate H.sub.2 gas from a liquid 913. The residual liquid product contains dissolved NaBO.sub.2 914. The gas and liquid exiting the catalytic hydrolysis reactor is 915 at a temperature of 60 to 180 C. The separated liquid is recovered via a drain mechanism 916 and is sent to waste bladder storage as described elsewhere in this application 917. Separated gas subsequently flows to a heat exchanger 918 where it is cooled to 60 C. At this point in the scheme a back pressure regulator is used 919. Condensed water is recovered by the low temperature phase separator 920 via a drain mechanism and is then delivered to the water reservoir. Stored H.sub.2 is delivered to a fuel cell as needed from a H.sub.2 accumulator 921. A forward pressure regulator 922 is included to adjust the H.sub.2 to the desired pressure for the fuel cell 923. Product water from the fuel cell can be supplied via a conduit to the water reservoir 904.

(81) The hydrogen generation system in FIG. 17 contains multiple pressure controlled zones. One pressure zone comprises the conduits between the water reactor 904, fuel reactor 902 and the hydrolysis reactor 903. These zone is maintained typically at 55 psia.

(82) A second pressure controlled zone is achieved through back pressure regulator 919. The pressurized zone extends from the hydrolysis reactor outlet to the HT phase separator 913, through conduits 915, and heat exchanger conduits within 918. The pressure in this zone is controlled between 0 psig and 200 psig depending on the reaction conditions. For example, setting this zone to a higher pressure improves borate solubility. Pressure in this zone settings may be varied via 919 in relation to the reactor preheat temperature to achieve optimal hydrolysis reactor conditions.

(83) Another pressure controlled zone comprises the LT phase separator 920 and the hydrogen accumulator 921 and associated conduits. The pressure is controlled in a suitable range for delivery to the fuel cell 923.

(84) Catalytic Reactor. The H.sub.2 production reactor 903 is a flow-through single pass design with unidirectional internal fluid flow, achieving continuous hydrogen output. The reactor design is given in FIG. 18. Light-weight design features are included. The middle screens hold the hydrolysis catalyst material 925. The number of screens can vary from 6 to 60. Cartridge heaters allow temperature management and contribute to rapid start up 924. There are 4 heaters (50 W capacity) total, with 2 heaters inside each end plate. The reactor can be heated to 60 C. in <2 minutes. The reactor's operation conditions require precise parameter control as described herein especially with regard to preheating of the reactor and reactor pressure.

(85) The hydrolysis catalysts include a high surface area coating of cobalt-boride on the expanded metal screen packages. The screen coating procedure first requires sonication for 30 minutes to remove any dirt and oil. After rinse the screens with large amounts of DI water, they are soaked in a Woods Nickel Bath for at least 15 minutes. While the packages are soaking, prepare the cobalt chloride solution. Move the Woods Nickel Bath to the 2 L beaker and add a counter electrode connected to a cathode power supply clip. Nickel plate the packages at 2.0V for 8 seconds on each face. Thoroughly rinse off the plating solution from. Once the Cobalt Chloride solution has sat for 10 minutes, pour enough solution over the packages to half cover the top package with the plastic container tilted to keep the solution in the package corner. Slosh the solution to ensure that there are no pockets of DI water with no cobalt in it. Pour to as much of the NaBH.sub.4 solution onto the screens as the Cobalt Chloride Solution. Slosh the solution around, making sure to keep the packages covered with the solution, until bubble formation stops. Rinse with DI water. Repeat several times in such a way that the packages have been plated with the following sequence: nickel, cobalt, cobalt, nickel, cobalt, cobalt, nickel. The two later nickel coats improve the adhesion of the cobalt and keep it from being torn off during use. The packages should now be black and slightly fuzzy. Dry, wrap each package with a chem-wipe and store them in a plastic bag until they are used. Rough handling can break off the coating.

(86) The reactor is designed and operated to achieve 100% hydrogen conversion. Conversion percentages are calculated by comparing the total amount of H.sub.2 produced through the duration of a test (according to a mass flow meter) against the theoretical amount of hydrogen available from the volume of NaBH.sub.4 which was supplied to the reactor during a defined operation time, using Eq 1. for stoichiometry values required for the calculation. The reactor as described herein provides a means for >95% and preferably 99.0 to 100.0% conversion, which means the reactor can achieve zero NaBH.sub.4 or near zero NaBH.sub.4 in the reactor output stream. Another feature of the reactor is operation without formation of crystal (insoluble) NaBH.sub.4 or NaBO.sub.2 within the hydrogen production catalytic reactor or adjacent fluid conduits. Included in the design are pressure sensing and pressure control at designated points in the flow system. Cooling of the catalytic reactor is achieved through the control architecture, by adjusting fluid flow rate through the reactor. Temperature sensing and control equipment items are included in the catalytic reactor design. Pressure and sensor controls are used in conjunction with the variables described above to achieve conditions of temperature and pressure, affecting water availability, and improving the solubility of NaBO.sub.2 in the reactor and associated fluid conduits.

(87) Fuel Management. Details of fluid management between fuel/water storage and hydrolysis reactor via the conduit system 910 are given in FIG. 19. A mixing zone 940 allows adequate dilution of the fuel from its storage concentration to its use concentration. As the fuel and water pumps ramp up and down during operation, the ratio of fuel to water will vary. The purpose of the mixing chamber is to provide a buffer for any abrupt changes in concentration that may occur. The system is preferably controlled at a concentration less than 12% NaBH.sub.4. Assuming that all points in the reactor are at temperatures greater than 23 C., 12% can be a safe upper limit to prevent formation of NaBO.sub.2 solids in the reactor. Because the flow rates can change abruptly during pressure on demand operation of the system, having this buffer volume to dilute any momentary or periodic changes in concentration protects the reactor from conditions, which could affect solubility. Fuel flow rate is controlled by the feedback from a pressure transducer 941. Pressure transducer can be located at any position between the fuel solution reservoir 902 and reactor 903. The pressure transducer may be in close proximity to the mixing zone 940. Goal is to maintain an accumulated pressure of 55 psia at pressure transducer 941. The conduit between the fuel reservoir and the mixing zone 940 can include a bypass valve 912, pump 942, flow meter 943, check valve 944. The conduit between the water reservoir 904 and the mixing zone 940 can include a bypass valve 911, pump 945, flow meter 946, and a check valve 947.

(88) Because this is a pressure on demand system, but there is a slight delay between the fuel flow rate and hydrogen generation, an accumulator volume 921 was added after the low temperature phase separator 920. As the demand for hydrogen fluctuates up and down, the accumulated volume provides a consistent supply of hydrogen pressure for the fuel cell. The pressure in the accumulator 921 is monitored by pressure transducer 926 and maintained in the range of 35-75 psia by increasing or decreasing the flow rate of the fuel solution into the reactor 903 via fuel pump 924. Pressure transducer 926 is in communication with accumulator volume 921. The lower pressure limit (35 psia) ensures that the pressure always stays above the pressure required by the fuel cell 923. A typical pressure required by the hydrogen feed to the fuel cell is 25 psi. The accumulator helps to ensure the fuel cell is never starved of sufficient hydrogen. The upper limit of 75 psia prevents excessive production of hydrogen and risk of over pressurization of the system.

(89) The control scheme ramps the fuel pump 942 up if pressure monitored by 926 falls below 55 psia so that hydrogen generation can keep up with the fuel cell's hydrogen demand. The fuel pump ramps down when the demand decreases and the 926 pressure rises above 55 psia, eventually shutting off the fuel pump if 75 psia is reached. The fuel pump 942 is controlled by the fuel flow rate and closed loop feedback from the fuel flow meter 943. The goal is to maintain the required fuel flow rate as indicated by the flow meter. For the optimum operation of 10% NaBH.sub.4 and water balance (made up from: H.sub.2O.sub.2 product water; fuel cell water and reactor recovered water) for a 900 W fuel cell output, the fuel solution feed rate should be preferably at 13 ml/min. During normal pressure on demand operation, the flow rate range will be as low as 0 ml/min (zero) when the hydrogen production should slow down or stop, and as high as 20 ml/min when the fuel cell is at higher power, needing a high rate of hydrogen feed.

(90) The water flow rate between reservoir 904 and mixing zone 940, is directly correlated to the fuel flow rate in order to maintain a NaBH.sub.4 concentration entering reactor 903 at <12% for solubility protection and >8% so that water balance is maintained in a desirable range, such that the level of water in 904 is neither depleted or accumulated to excess. To achieve a desired level of water in the reservoir, the water flow rate between 904 and 940 is also controlled by feedback from the water reservoir electronic level sensor. The reservoir electronic level sensor provides feedback to pump 945 enabling the pumping rate to be adjusted. The goal is to maintain a reservoir water level at or near to a set volume. Because this measurement has direct correlation to the water balance, if all the systems are functioning optimally, the water level should be maintained at or near a constant level. However, slight deviations from a completely balanced system could compound over long term operation and the water reservoir could deplete or overfill. If low water level is detected by the electronic sensor, there is a need to avoid the water pump being starved of supply and the fuel solution not being sufficiently diluted. Thus, the control scheme operates according to the electronic level sensor. The control scheme decreases the water flow rate via pump 945 so that the water consumption is slower while the input water to the reservoir (from: oxidizer product water; fuel cell water; reactor recovered water) replenishes the reservoir to the desired level. If the level is rising, the water flow rate via pump 945 is increased to prevent overflow of the reservoir. For a fuel cell operating at 900 W, a preferred NaBH.sub.4 concentration entering the reactor is 10% NaBH.sub.4 (the storage concentration of NaBH.sub.4 fuel is 25%). The flow rate into the reactor is 23 ml/min. The fuel flow rate between 902 and 940 can be as low as 0 ml/min when hydrogen demand decreases or as high as 30 ml/min when hydrogen demand is high.

(91) Water flow rate from 904 to the reactor 903 via 940 is also preferably high when the reactor is being shut down. During shut down, the fuel pump 942 is turned off and water is used to flush the reactor of residual fuel solution as well as cool the reactor to room temperature.

(92) Reactor Water Recovery by Phase Separation. FIG. 20A is the configuration of the first stage high temperature phase separator 913. This high temperature phase separator has the inlet from 903 above the water line. The temperature of the hydrogen containing gas/fluid from reactor 903 is typically 110-130 C. The liquid waste is separated from the gas stream by gravity and the gas stream continues downstream via conduit 915 to the heat exchanger 918. The liquid waste in the separator typically is at 90 C. The liquid waste is transferred to waste bladders 917 described elsewhere in this application. According to the control scheme, the drain valve 916 opens once the water level in the separator reaches a predetermined point. The water level in the separator chamber is monitored by a continuous operating electronic sensor. A float-type sensor may be used 927.

(93) The gas stream exits the heat exchanger 918, it continues to the low temperature separator 920 where the condensed water is separated from the hydrogen-containing gas stream. FIG. 20B gives the configuration of the low temperature phase separator. The condensed water from 920 is recovered via 907 and 908 and fed to the water reservoir 904. In addition to capturing condensed water, the separator also captures micro particles in the stream by using a sparger to divide the stream into small bubbles, which pass through liquid water in the separator. In order to incorporate the sparger into the separator 928, the separator body is configured so that the inlet will remain below the water line and a stainless steel filter is fitted into the inlet. According to the control scheme, the drain valve 907 opens once the water level in the separator reaches a predetermined set point. The water level in the separator chamber is monitored by an electronic sensor. A float-type sensor may be used 929.

(94) Water Reservoir. FIG. 21A shows the design of the water reservoir 904 and the means of water recovery. The byproduct water from the oxidizer, fuel cell, and the recovered water reactor will fill the water reservoir, following which the water will be used to supply the fuel dilution water pump 945. The reservoir will also be vented with a Gore brand PTFE membrane which allows gas to flow freely in and out of the reservoir while preventing liquid from exiting the reservoir 930. This will allow the container to remain unpressurized throughout the duration of the mission. Furthermore, a differential pressure transducer 931 will be used in order to determine the difference between the water column pressure at the bottom of the reservoir and the pressure in the headspace of the reservoir, and the differential pressure will be used to calculate the water level. Alternatively a float type continuous level sensor 932 can be used to increase reliability and make the level sensing more robust see FIG. 21B. Under ideal conditions, the water level in the reservoir should not fluctuate, but if the water level is rising or falling over time, the water pump will slightly ramp up or down to account for minor differences that may occur between the inlet and outlet flow rates. This will help to eliminate an excessively low water level which would deprive the dilution pump or a high water level which could pressurize the container and lead to failure.

(95) Example 1 includes one set of operating conditions and parameters for the continuous H.sub.2 generating system.

EXAMPLE 1

Input to Reactor

(96) TABLE-US-00001 NaBH.sub.4 storage concentration 25 wt % NaBH.sub.4 flow rate ~43 mL/min H.sub.2O flow rate ~13 mL/min NaBH.sub.4 feed concentration ~10 wt %

Reactor Conditions

(97) TABLE-US-00002 Temperature 125 C. Pressure 75 psia Insoluble NaBO.sub.2 formation No Insoluble NaBH.sub.4 No Residence time ~17 s

Output from Reactor

(98) TABLE-US-00003 H.sub.2 flow rate ~8.0 slpm H.sub.2 purity 99.999% H.sub.2 conversion 100% Insoluble NaBO.sub.2 No NaBH.sub.4 output concentration <0.05 wt % NaBO.sub.2 output concentration 17.3 wt %

(99) Example 2 includes another set of operating conditions and parameters for the continuous H.sub.2 generating system. In this configuration the reactor can be operated with no pre-heating but pressurized.

(100) TABLE-US-00004 REACTOR CONTROLS Reactor Inlet Feed Temperature 20 C. Reactor Back Pressure Control 60 psig NaBH.sub.4 feed concentration 10 wt % RESULTANT OPERATIONAL CONDITIONS Reactor Outlet Temperature 114 C. Outlet Water Vapor Quality 10% NaBO.sub.2 concentration 19 wt % NaBO.sub.2 Solubility 21 wt % Insoluble NaBO.sub.2 formation No

(101) Example 3 shows some of the values for preheating temperature and low values for the back pressure setting leads to borate insolubility. In this configuration the reactor can be operated with no pre-heating or pressure.

(102) TABLE-US-00005 REACTOR CONTROLS Reactor Inlet Feed Temperature 20 C. Reactor Back Pressure Control 0 psig NaBH.sub.4 feed concentration 10 wt % RESULTANT OPERATIONAL CONDITIONS Reactor Outlet Temperature 79 C. Outlet Water Vapor Quality 18% NaBO.sub.2 concentration 21 wt % NaBO.sub.2 Solubility 21 wt % Insoluble NaBO.sub.2 formation Yes

(103) Examples 4 includes another set of operating conditions and parameters for the continuous H.sub.2 generating system when the concentration of NaBH.sub.4 entering the hydrolysis reactor 20 wt %. With high NaBH.sub.4 inlet concentrations, both pre-heating and an increase in pressure are needed. In this configuration the reactor can be operated with pre-heating and pressurization.

(104) TABLE-US-00006 REACTOR CONTROLS Reactor Inlet Feed Temperature 70 C. Reactor Back Pressure Control 200 psig NaBH.sub.4 feed concentration 20 wt % RESULTANT OPERATIONAL CONDITIONS Reactor Outlet Temperature 166 C. Outlet Water Vapor Quality 54 wt % NaBO.sub.2 concentration 55 wt % NaBO.sub.2 Solubility 56 wt % Insoluble NaBO.sub.2 formation No

(105) Example 5 shows another embodiment of operating conditions. Preheating is applied but the back pressure regulator is set at a low pressure. These conditions in borate insolubility. In this configuration the reactor can be operated with pre-heating but not pressurized.

(106) TABLE-US-00007 REACTOR CONTROLS Reactor Inlet Feed Temperature 70 C. Reactor Back Pressure Control 0 psig NaBH.sub.4 feed concentration 20 wt % RESULTANT OPERATIONAL CONDITIONS Reactor Outlet Temperature 85 C. Outlet Water Vapor Quality 77 wt % NaBO.sub.2 concentration 71 wt % NaBO.sub.2 Solubility 56 wt % Insoluble NaBO.sub.2 formation Yes

(107) Example 6 shows yet another set of operating conditions. It uses a NaBH.sub.4 entering the hydrolysis reactor 20 wt %. The backpressure control is set at a high value. However, the inlet temperature is set at a low value. These conditions result in borate insolubility. In this configuration the reactor can be operated with no pre-heating but pressurized.

(108) TABLE-US-00008 REACTOR CONTROLS Reactor Inlet Feed Temperature 20 C. Reactor Back Pressure Control 200 psig NaBH.sub.4 feed concentration 20 wt % RESULTANT OPERAITONAL CONDITIONS Reactor Outlet Temperature 160 C. Outlet Water Vapor Quality 41 wt % NaBO.sub.2 concentration 49 wt % NaBO.sub.2 Solubility 21 wt % Insoluble NaBO.sub.2 formation Yes

(109) Example 7 includes another set of operating conditions and parameters for the continuous H.sub.2 generating system when the concentration of NaBH.sub.4 entering the hydrolysis reactor 10 wt %. In this configuration the reactor can be operated with pre-heating but not pressurized.

(110) TABLE-US-00009 REACTOR CONTROLS Reactor Inlet Feed Temperature 30 C. Reactor Back Pressure Control 0 psig NaBH.sub.4 feed concentration 10 wt % RESULTANT OPERATIONAL CONDITIONS Reactor Outlet Temperature 80 C. Outlet Water Vapor Quality 20 wt % NaBO.sub.2 concentration 21 wt % NaBO.sub.2 Solubility 26 wt % Insoluble NaBO.sub.2 formation No

(111) FIGS. 22A and 22B are graphs that show the product as a weight percent wt % of the NaBH.sub.4 and NaBO.sub.2, in relation to: FIG. 22A the wt % of reactant NaBH.sub.4, and in FIG. 22B the wt % of the reactant H.sub.2O.sub.2.

(112) It is contemplated that any embodiment discussed in this specification can be implemented with respect to any method, kit, reagent, or composition of the invention, and vice versa. Furthermore, compositions of the invention can be used to achieve methods of the invention.

(113) It will be understood that particular embodiments described herein are shown by way of illustration and not as limitations of the invention. The principal features of this invention can be employed in various embodiments without departing from the scope of the invention. Those skilled in the art will recognize, or be able to ascertain using no more than routine experimentation, numerous equivalents to the specific procedures described herein. Such equivalents are considered to be within the scope of this invention and are covered by the claims.

(114) All publications and patent applications mentioned in the specification are indicative of the level of skill of those skilled in the art to which this invention pertains. All publications and patent applications are herein incorporated by reference to the same extent as if each individual publication or patent application was specifically and individually indicated to be incorporated by reference.

(115) The use of the word a or an when used in conjunction with the term comprising in the claims and/or the specification may mean one, but it is also consistent with the meaning of one or more, at least one, and one or more than one. The use of the term or in the claims is used to mean and/or unless explicitly indicated to refer to alternatives only or the alternatives are mutually exclusive, although the disclosure supports a definition that refers to only alternatives and and/or. Throughout this application, the term about is used to indicate that a value includes the inherent variation of error for the device, the method being employed to determine the value, or the variation that exists among the study subjects.

(116) As used in this specification and claim(s), the words comprising (and any form of comprising, such as comprise and comprises), having (and any form of having, such as have and has), including (and any form of including, such as includes and include) or containing (and any form of containing, such as contains and contain) are inclusive or open-ended and do not exclude additional, unrecited elements or method steps. In embodiments of any of the compositions and methods provided herein, comprising may be replaced with consisting essentially of or consisting of. As used herein, the phrase consisting essentially of requires the specified integer(s) or steps as well as those that do not materially affect the character or function of the claimed invention. As used herein, the term consisting is used to indicate the presence of the recited integer (e.g., a feature, an element, a characteristic, a property, a method/process step or a limitation) or group of integers (e.g., feature(s), element(s), characteristic(s), propertie(s), method/process steps or limitation(s)) only.

(117) The term or combinations thereof as used herein refers to all permutations and combinations of the listed items preceding the term. For example, A, B, C, or combinations thereof is intended to include at least one of: A, B, C, AB, AC, BC, or ABC, and if order is important in a particular context, also BA, CA, CB, CBA, BCA, ACB, BAC, or CAB. Continuing with this example, expressly included are combinations that contain repeats of one or more item or term, such as BB, AAA, AB, BBC, AAABCCCC, CBBAAA, CABABB, and so forth. The skilled artisan will understand that typically there is no limit on the number of items or terms in any combination, unless otherwise apparent from the context.

(118) As used herein, words of approximation such as, without limitation, about, substantial or substantially refers to a condition that when so modified is understood to not necessarily be absolute or perfect but would be considered close enough to those of ordinary skill in the art to warrant designating the condition as being present. The extent to which the description may vary will depend on how great a change can be instituted and still have one of ordinary skilled in the art recognize the modified feature as still having the required characteristics and capabilities of the unmodified feature. In general, but subject to the preceding discussion, a numerical value herein that is modified by a word of approximation such as about may vary from the stated value by at least 1, 2, 3, 4, 5, 6, 7, 10, 12 or 15%.

(119) All of the compositions and/or methods disclosed and claimed herein can be made and executed without undue experimentation in light of the present disclosure. While the compositions and methods of this invention have been described in terms of preferred embodiments, it will be apparent to those of skill in the art that variations may be applied to the compositions and/or methods and in the steps or in the sequence of steps of the method described herein without departing from the concept, spirit and scope of the invention. All such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and concept of the invention as defined by the appended claims.