the ability of an air based reforming system to respond to any increase in hydrogen production demand is highly dependant upon that system &# 39 ; s ability to provide appropriate thermal increases to the water feed stock , catalytic beds and other thermal masses of the containment components . the rate at which the thermal management system must respond is identical to the rate at which demand for hydrogen production changes . one system level approach to supplying more hydrogen for transient load increases , while the reformer &# 39 ; s thermal management system struggles with maintaining the necessary process conditions , is to produce and store excess pressurized hydrogen in holding tanks . an alternative approach to obtaining supplemental hydrogen from a holding tank would be to introduce a supplemental , exothermic oxygen source at the beginning of the primary reforming process . to be effective , the oxygen source would ideally need to be free or substantially free of contaminates such as nitrogen and other compounds that either create a cleanup requirement or potentially damage the various catalytic beds or the fuel cell mea . furthermore , for any such supplemental oxygen generation / delivery subsystem to be effective , it must not only generate oxygen but also generate sufficient heat to ideally flash an excess quantity of liquid water into steam . these compounds can then be subsequently used to accelerate the reforming of the hydrocarbon fuel , which is itself a highly exothermic reaction . such an approach meets both the immediate load following demand for increased hydrogen , and accelerates the addition of new thermal energy to move the primary reforming system to a higher rate of hydrogen production . when the primary reforming system has been brought up to temperature and can sustain the higher flow rate demand on its own , the supplemental oxygen , heat and steam system may be turned off . solid and liquid oxidizers are a traditional source for oxygen . when activated , most solid or liquid oxidizers release considerable quantities of thermal energy as they disassociate and release the chemically stored oxygen . the supplemental oxygen generation / delivery system needs to capture this energy for use in vaporizing water into steam and to deliver either the thermal energy or the desired steam directly to the steam reforming section . while there are several solid oxidizers available , many of which have been used to provide emergency oxygen in airplanes , submarines or emergency rescue gear , a preferred approach utilizes a liquid oxidizer . most preferably , the liquid oxidizer is diluted hydrogen peroxide ( h 2 o 2 ). diluted hydrogen peroxide is a mixture of hydrogen peroxide and water . the mixture may also include stabilizers . the relative concentration by weight of peroxide varies from standard plant production of approximately 70 % down to about 3 % found in many over the counter preparations for household use . a h 2 o 2 concentration of between about 65 % by weight to about 45 % by weight is the preferred concentration to best meet the requirements of the chemical reactions , as well as the general safety and handling requirements of any large market implementation . the dissociation of this compound ( h 2 o 2 → heat + h 2 o + o − ) is highly exothermic and directly generates the three desired components of water , oxygen and thermal energy . the use of hydrogen peroxide as the oxidizer is advantageous over the use of other oxidizers as there is no need to capture thermal energy and transfer it to liquid water . instead , water content is directly vaporized without the need for heat exchangers and pumps , thereby avoiding further system cost and complexity . an additional benefit is that there are no contaminates that must be cleaned up in the primary reforming system . in particular , there is no nitrogen released . the lack of additional nitrogen in the supplemental oxygen stream prevents increasing the nox formation rate within the primary reforming system , though total process mass does increase . instead , the nox cleanup catalysts of the primary reforming system can be brought up to the necessary operating temperatures as the nox free reactants generate and distribute exothermic energy throughout the entire reformer system , prior to shutting down a supplemental oxygen system . in selecting a solid or liquid oxidizer for this use , the impact of any associated chemical contaminates that would be released and how those contaminates would affect the catalytic beds or the fuel cell membrane must be considered . fig1 depicts one of the most recent process evolutions of steam reforming , specifically autothermal reforming , that the present invention can be applied to . referring to fig2 , a holding tank for the hydrogen peroxide / water mixture ( 1 ) feeds a pressurizing pump ( 2 ) that provides the necessary energy to allow for the controlled micro - injection ( 60 ) of this liquid . the quantity of the peroxide and water mixture that is injected ( 60 ) into the reaction pressure vessel ( 5 a ) is determined and controlled by the system controller ( 4 ). the products of the dissociation of peroxide can be immediately introduced into the primary steam reforming section ( 10 ) or the flow rate of these products can be modified by an intermediate control valve ( 20 ). the additional hydrocarbon fuel required may be provided by the primary reforming system &# 39 ; s fuel delivery mechanism . one specific embodiment is shown as a process block diagram in fig3 . in this embodiment , a similar hydrogen peroxide and water mixture tank ( 1 ) holds the mixture and feeds it to the pressurizing pump ( 2 ) for subsequent injection ( 60 ) into the reaction pressure vessel ( 5 b ). however , in this approach the reaction pressure vessel ( 5 b ) is reconfigured to accept pressurized ( 9 ), micro - injection ( 80 ) of the hydrocarbon fuel in use by the primary steam reformer ( 10 ), which is stored in a separate tank ( 8 ). the catalysts of the reaction pressure vessel ( 5 b ) need to be reconfigured to provide not only for hydrogen peroxide dissociation as depicted in fig2 , but also for the subsequent catalytic reduction and water gas shift reactions required to reform the hydrocarbon fuel . the injection rates are controlled by a similar system controller ( 4 ). the thermally energetic gas stream from the reaction pressure vessel ( 5 b ) is either directly introduced at the appropriate process point of the primary steam reformer ( 10 ) or an intermediate flow control valve ( 20 ) may be used to fine tune this flow rate if needed . in either configuration , fig2 or fig3 , there is a hot , thermally energetic gas flow that is introduced into the primary reforming system ( 10 ). this gas stream is immediately available to increase the rate of hydrogen production through the primary reforming system either directly , as in the system depicted in fig3 , or indirectly , as depicted in fig2 . for either configuration , the exothermic nature of the hydrogen peroxide reactions provide a means to accelerate the rate in which the catalytic beds in the primary reforming system are brought up to their functional temperature range or facilitates maintaining of the temperature range in those beds as the total mass flow is increased . when an oxidizer is used that does not contain nitrogen or other contaminates , it is not necessary for the catalytic beds , which are required to cleanup these formations , to be immediately and fully functional . these beds can initially be well below their minimum operational temperature without causing an adverse effect upon the quality of the hydrogen reformate feed stream provided to the fuel cell . as long as the contamination - free oxygen source is used , these beds can be brought up to the particular minimum temperature ranges over time , in preparation to perform their particular cleanup function . the catalytic beds need to be at their operational functional level whenever the transition is made from the oxidizer back to air as the oxygen source . as such , the current flow section through the reformer system can either be further heated to provide for increased reforming rates , or an entirely new flow section can be the recipient of all or part of the contamination - free reformate stream . in this latter process , the new “ cold ” flow section could be quickly brought thermally online in preparation for eventually performing all of the oxidation , water gas shift reactions and cleanup required when air is used as the oxidation source . during this time period , the supplemental hydrogen stream is immediately usable by the fuel cell stack , allowing for the entire fuel cell power system ( fcps ) to perform load following power production . when a pem type fuel cell is used , co will be one of the incompatible compounds generated by these processes . the formation of co can be controlled in the new flow section through both the manipulation of the oxidizer / water to fuel ratio as well as reliance upon the final co clean up stage of the primary reforming system . the final co to co 2 conversion process , typically referred to as the low temperature water - gas shift and the selective oxidation or preferential oxidation ( prox ) process ( fig1 ), occur at reduced temperatures , compared to those found in the upstream hydrocarbon reduction / oxidation beds . these components may need to be adapted , relocated , and / or duplicated to be able to fully perform their function of co cleanup when peroxide is being used to bring up a new flow section through the steam reforming system . in a preferred embodiment , depicted in fig4 , the primary steam reforming system is configured such that there were multiple , insulated , independently selectable flow sections ( 10 a , 10 b , 10 c ) through all or the majority of the temperature critical oxidation and gas cleanup sections . the number and relative size differences of these separate sections , if any , are a function of the overall fuel cell power system ( fcps ) duty cycle . the ratio between the fcps turndown capability ( y : 1 ) and the primary reformer turndown ( x : 1 ) is a design / analysis starting point to determine the actual number and configuration of required flow sections , namely ( y / x ). for example , if the fcps needs to work over a 6 to 1 turndown range in power output ( say 60 kwe maximum to 10 kwe minimum ) but a reforming process can only manage a 2 to 1 turndown ( 60 kwe to 30 kwe ), then the total volume of the 60 kwe capable reformer would need to be divided into a minimum total of 6 / 2 = 3 flow sections , ( i . e ., three , 20 kwe flow sections ). as the fcps increased its demand for hydrogen from 10 kwe to 30 kwe , the reformer will increase output from 50 % in just one section to meet the kwe flow demand to 100 % in the first section and 50 % output in a second section . at 100 % of the fcps power production of 60 kwe , all three flow sections will be at their 100 % hydrogen production capacity . there are many significant system level difficulties faced by current reforming systems when they are commanded to transition from lower hydrogen production levels to higher levels . the use of hydrogen peroxide in the processes of the present invention is specifically intended to facilitate that transition . cost is always a design issue for consumer - oriented products . two broad approaches of addressing cost through design are to minimize the total number of components and to identify simpler manufacturing and assembly approaches to those remaining components . the need to meet specific performance requirements is typically a countering design factor that has the tendency to increase cost . with that perspective , the oxygen assist approach of the present invention , which is generally characterized by the process block diagram in fig2 , represents a simpler system . since the primary reformer system ( 10 ) already has a fuel delivery system ( 80 ), as well as volumes within its structure for catalysts ( 40 , 90 , 100 , 110 ), duplicating those components in a hydrocarbon oxidation / reduction vessel ( 5 b ), as illustrated in fig3 , adds to overall system cost and complexity . indeed , to minimize the addition of more components , it may be preferable to remove the reaction pressure vessel ( 5 a ) of fig2 and integrate the remaining components of fig2 into the primary reforming system ( 10 ). the peroxide / water injector ( 60 ) and the necessary catalysis and / or electrical heated ignition grid ( 70 ) to initiate the dissociation of the peroxide could be integrated directly into each flow section ( 10 a , 10 b , 10 c ) of the primary reforming system ( 10 ). the fuel injection / delivery mechanism ( 80 ) would need to be located subsequently along each flow section . since the oxidation process of the hydrocarbon fuel is exothermic , a means of transferring that thermal energy gain to the endothermic generation of steam is provided and / or relocated to the flow section structure . by using an approach that encourages internal thermal conduction , thermal loss to the environment is minimized . to realize this goal , a series of mechanical rods ( 50 ), shaped to maximize thermal transfer , may be embedded with the various catalysts thereby mechanically interconnecting the exothermic oxidation and / or reduction catalyst beds ( 90 ) to the endothermic steam generation bed ( 40 ). the thermal transfer rods ( 50 ) may connect to other catalytic beds as required to facilitate creating and / or maintaining elevated temperatures of the gas clean up catalysts ( 100 ), ( 110 ). when the flow section and the associated beds are up to temperature to allow for transfer from peroxide as the sole oxygen source to eventually the ambient air , water can be pressure mist injected ( 30 ) into the vaporization bed ( 40 ). a throttle valve ( 20 ), used for control of external air flow and / or air / steam flow through the flow section , may then be opened to gradually transition the flow section from peroxide to 100 % air as the oxygen source . the following description illustrates how the above process of using hydrogen peroxide as a thermal / process assist functions in a hydrocarbon reforming system , starting from a “ cold ” non - operating state . referring to fig4 , to allow for near immediate delivery of fuel cell safe , hydrogen reformate , all throttle control valves ( 20 a , 20 b , 20 c ) remain closed ( as illustrated by throttle control valve , 20 a ) isolating all of the reforming flow sections from ambient air and its associated nitrogen contaminates . the peroxide / water injector ( 60 ) of at least one flow section begins to pressure inject this solution in a manner that encourages fine misting of the liquid . thermal rise of the flow section begins as the hydrogen peroxide mist makes contact with the dissociation catalyst ( 70 ), which may also contain an electrical heating grid / ignition element to further ensure dissociation . the hydrocarbon fuel is then pressure injected ( 80 ) down stream of the dissociation catalyst / ignition element in a manner that encourages fine misting of the fuel . pre - heating of the minute quantities of fuel , immediately prior to injection , would further accelerate the initial startup sequence by enhancing the thermal content of the fuel and improving the misting properties during injection by reducing the droplet size . a similar pre - heating of the small quantities of the hydrogen peroxide / water solution , just prior to its pressurized injection into the flow section is another means to facilitate its dissociation and release of thermal energy to the flow section . the dissociated peroxide , ( steam and oxygen mix ) with the injected hydrocarbon fuel enter the reduction and / or oxidation catalyst bed ( 90 ) to begin stripping hydrogen atoms from the hydrocarbon . since this reaction is highly exothermic , efforts are typically made to transfer this energy to the task of pre - heating the input fluids , primarily the water and the hydrocarbon fuel . to this end , thermal conduction rods ( 50 ) begin the transfer of thermal energy to the steam generating beds ( 40 ) in preparation for the transition back to air as the oxygen source . while the primary reforming system ( 10 ) may continue to use other external , thermal transfer means to heat process water , the depicted approach ( 30 , 40 ) assists the reforming system ( 10 ) to quickly adjust to smaller increases in hydrogen production demands without the need to inject any hydrogen peroxide / water solution . the thermal conduction rods ( 50 ) may also be extended from the highly exothermic oxidation / reduction beds ( 90 ) to down stream catalytic beds ( 100 , 110 ) used for gas clean up such as nox to n 2 and co to co 2 conversion . the geometry , material construction , location and member of these rods ( 50 , 50 a , 50 b , 50 c of fig6 ) can be adjusted , based upon process analysis to best meet the thermal transfer needs while minimizing cost . thermal insulating sleeves ( 120 ), can be added to sections of the thermal conducting rods ( 50 a , 50 b , 50 c of fig6 ) to either avoid excess thermal transfer to a particular catalyst bed ( 100 , fig4 ) or to ensure sufficient thermal transfer to catalytic beds further downstream ( 110 ). as the catalytic beds in those flow sections are actively brought up to operating thermal conditions , using hydrogen peroxide as the sole oxygen source , the flow control valve begins to open in a manner similar to that depicted by valve 20 c , to allow ambient air or air / steam to begin to mix in with the reforming process . in turn , the rate at which the hydrogen peroxide / water solution is injected ( 60 ) would be proportionally reduced . eventually , the active flow section would be operating entirely on air as the oxygen source . at this point , the primary reforming system ( 10 ) may continue to operate on the active flow sections or bring a non - active flow section online using the process described above . the new flow section ( for example 10 b ) is isolated from the external air or air / steam gas flow by fully closing the flow control valve ( 20 b ). as thermal conditions in flow section ( 10 b ) reach those required to allow for air operation , the flow control valve ( 20 b ) begins to open , initiating the transition to 100 % air operation in that flow section . at any point in time during the primary reforming system &# 39 ; s ( 10 ) operation on 100 % air , one or more of the flow sections may have additional , intermittent amounts of hydrogen / peroxide solution injected ( 60 ) into the flow sections to meet sudden increased demands for hydrogen production ( transient load demands ). likewise , additional quantities of water may be injected ( 30 ) into the vaporization beds ( 40 ) to ensure sufficient process steam was also present for these transient load conditions . there are those applications in which the cost of fully duplicated hydrogen generating systems , as depicted in the process diagram of fig3 , is necessary and justified . one example is those instances in which the hydrogen peroxide / water supported reforming is the only reforming system , as described in copending u . s . patent application ser . no . 10 / 884 , 771 which is incorporated herein by reference . other application requirements may require a much greater thermal transfer rate to heat the catalytic beds of the primary reforming system . this higher thermal transfer rate would be possible by introducing a much hotter gas stream into the primary reforming system than that provided by the previously described dissociation of hydrogen peroxide . the source of this much hotter gas stream ( 700 degree c . versus 100 - 200 degree c .) could be the fully oxidized / reduced hydrocarbon gaseous fuel stream exiting from the pressure reaction vessel ( 5 b ) as illustrated in the process diagram of fig3 . fig5 illustrates a design layout of how the components listed in the fig3 process diagram could be configured . since this approach does create a stand alone reforming system , it would need to have nearly identical functionality as depicted in the fig4 reforming system . the primary differences would be that the reaction vessel ( 5 b ) needs to be included and since all of the input compounds are liquids and the output product is a gas stream , the vessel ( 5 b ) is not a flow through design as shown in the flow sections ( 10 a , 10 b , 10 c ) of fig4 . the other components depicted in reforming flow sections of fig4 need to be duplicated in the self contained reformer ( 5 b ) in order to preserve the necessary functionality . hydrogen peroxide / water solution is injected ( 60 ) into the vessel ( 5 b ) to be dissociated by catalysts and / or heated electrical grid ( 70 ). the hydrocarbon fuel is injected ( 80 ) and mixed with the dissociated hydrogen peroxide prior to entering oxidation / reduction catalytic bed ( 90 ). thermal conduction rods ( 50 ) passively transfer the thermal energy from this exothermic bed , upstream to a steam generation bed . additional water may be injected ( 30 ) into this thermal mass bed ( 40 ) to provide additional process steam when needed . fig5 does indicate additional catalytic beds ( 100 , 110 ) for gas cleanup that may or may not be included in a particular system configuration . if the reaction vessel ( 5 b ) is the only reforming system , then these catalysts need to perform the preferential oxidation ( prox ) and water gas shift of co to co 2 in order to provide a fuel cell safe hydrogen fuel stream . there is however , no need for any nox cleanup due to the absence of nitrogen in this process . in the embodiment employing a second system reformer ( i . e . the primary reforming system ( 10 )) it is advantageous to minimize the thermal loss to additional catalyst mass ( 100 , 110 ) in the reaction vessel ( 5 b ) by leaving it out and relying upon similar catalysts in the primary reforming system to complete the gas clean up . this approach provides the primary reforming system with the hottest , most energetic gas possible for heat and brings the thermal mass of the primary system to operational temperature . the effective thermal transfer of the heats of dissociation and combustion from the point of generation to the regions in need of thermal energy is an important determinant to the success of the assisted reforming approaches of the present invention . one approach to this energy transfer described above utilizes internal , thermal conductive structures ( 50 , and 50 a , 50 b , 50 c of fig6 ) to transfer heat from high temperature exothermic catalyst beds ( 90 ) to endothermic beds ( 40 , 100 , 110 ) to minimize thermal loss to the environment and to accelerate thermal conduction to regions where the energy is needed . steam reforming of hydrocarbons utilizes several different catalytic beds to accomplish different tasks including steam generation , hydrocarbon fuel oxidation , nox cleanup , and water gas shift for co to co 2 conversion . all of these beds need to be at elevated temperatures in order for them to function as designed . of the beds listed , only the catalyst beds and / or regions in which carbon oxidation / reduction is occurring will have an exothermic release of energy . this exothermic release has been traditionally used to heat the follow on catalytic beds to their required temperature range . a traditional mechanism to accomplish this thermal transfer has been the hot gas molecules themselves as they travel through the various subsystems of the steam reformer . because steam based reforming is being applied to generate hydrogen for fuel cells , and for pem type fuel cells in particular , the product gas stream from the reformer can not be delivered to the fuel cell until the gas has been cleaned of co , and nox , assuming that there is no sulfur present . the clean up of these pollutants cannot occur to the degree necessary until the various catalytic beds are up to their operational temperatures . steam reforming has another consideration that internal , thermal conduction structures would be of value . in particular , the heating and eventual formation of steam is a process that is upstream of the exothermic oxidation of the hydrocarbon fuel . consequently , the use of the gas flow to transfer thermal energy is not possible . however , thermal conduction structures would be able to efficiently and cheaply transport the thermal energy against the flow stream . effective thermal transfer to the upstream steam generation bed allows for reduced parasitic loads used to pump and heat water external to the reforming process . this will also allow for an increase in the reforming system &# 39 ; s ability to generate steam , thereby improving the overall load response capability . referring to fig6 , the ideal shape and surface area ratios of the heat transfer structures ( 160 ) for heat absorption from the oxidation bed ( 90 ) and the preferred shape for the thermal release into the steam generation bed ( 40 ) or the gas cleanup beds ( 100 , 110 ) are not identical in moving along the length of the thermal transfer rod ( 270 ). the actual number , size and spacing of heat transfer plate structures ( 160 ) is determined by the thermodynamic needs of the reforming system and the material limitations that are imposed . in one preferred embodiment , a core of thermally conducting aluminum ( 140 , fig6 ), or similar material , is wrapped with a thin exterior layer of temperature - resistant stainless steel or similar type material ( 150 ). the stainless steel sheath prevents the aluminum from reacting with the hot gases , and contains any aluminum that may melt or flow . solid rods of temperature resistant stainless steel may be used ( 130 , fig6 ), though such types of steel offer poor thermal conductivity and use a considerable amount of relatively expensive metal . due to the very large temperature extremes that occur within the catalytic beds , a bimetallic composite structure with significantly different thermal growth coefficients will need to be carefully designed to handle the differential thermal growth . thermal insulators ( 120 ) may be used to preferentially direct thermal conduction past one region ( 100 , fig4 ) or regions to another region requiring an input of thermal energy ( 110 ). this approach aids in overall thermal management of the collective beds and preferentially accelerates the heating of selected beds ( 110 for example ) during initial system startup or activation of a new flow section . a preferred approach to implementing passive , thermal conductive heat transfer structures located within various catalytic and thermal mass beds is illustrated in fig7 . these transfer structures ( 50 ) need to be placed inside a thermally insulated ( 210 ) vessel ( 10 ) in such a fashion that the thermal and / or catalytic beds are well packed around them . in consideration of the need for a low cost assembly process , i . e ., one that could be fully automated , a thermal transfer structure similar to ( 50 c ), best meets those requirements . this structure consists of a series of separate pieces each of which can be axially assembled within the flow section ( 10 ). specifically , a thermal conductive mechanism of one or more thermal transfer rods ( 270 ) using a bi - material construction with an inner core ( 140 ) selected to maximize thermal transfer , and protected from the high temperature environment by a thin , thermally - resistant sheath ( 150 ) is preferred . a stop or machined feature ( 171 , 172 respectively ) is placed in the flow section vessel ( 10 ) to locate the thermal structure end plate ( 181 or 182 respectively ). the end plate ( 181 ) provides location for one or more thermal transfer rods ( 270 ), thermal transfer plates ( 160 ) and bed separators ( 200 ). the thermal transfer rod ( s ) ( 270 ) can have a constant diameter along its length , or a continuing , sequential reduction in the cross - sectional area along its length to facilitate the sequential press fit placement of components ( 160 ), ( 200 ), ( 120 ) during assembly . one means to fully automate the assembly of the entire structure is to press one or more thermal transfer rods ( 270 ) into the first end plate ( 182 ) and insert the structure into the reaction vessel ( 10 ) until it locates to the stop ( 172 ). with the assembly ( 10 , 182 , 270 ) in a vertical position and connected to a vibrator mechanism , and with the free end of the rods ( 270 ) rigidly located to the walls of the flow section vessel ( 10 ), ( by an external assembly device ), the first section of the first bed ( 110 ) can be added while vibrating the structure to ensure the necessary degree of compaction . the first thermal transfer plate ( 160 ) is pressed into location after the desired level of catalyst bed material has been added , further compacting the bed if necessary . this is repeated sequentially for the remaining sections of catalyst beds ( 110 , 100 , 90 ), dividing and separating each by a correctly spaced thermal transfer plate ( 160 ). thermal insulators ( 120 ) can be used to preferentially allow heating of one bed faster or to a greater degree than another catalytic bed . an example would be the desire to heat the low temperature water gas shift bed ( 110 ) for co to co 2 conversion as quickly as possible to ensure minimal co being entrained with the gas outflow stream . a bed separator ( 200 ) may be added to provide a mixing volume ( 192 ) for the injected hydrocarbon fuel ( 80 ) and the steam / oxygen mixture . a similar volume ( 191 ) can be created for injecting and dispersing the hydrogen peroxide / water solution ( 60 ) upstream of the dissociation elements ( 70 ). the final end plate ( 181 ) and retaining ring ( 171 ) may be installed to prevent movement of the assembled catalytic beds , independent of the vessels orientation or vibration during shipment or use . the flow section ( 10 ) is then enclosed with a cap ( 280 ). another passive , low cost , thermal transfer mechanism that greatly decreases the time required to bring an adjacent , non - active flow section fully up to operating temperature is depicted in fig8 . fig8 shows the most downstream components of any of the above described flow sections , whether it represents a configuration as depicted in fig4 or fig5 . as previously described , the ability of a steam reforming system , whether utilizing air or another oxidizer source , to generate a fuel cell safe hydrogen feed stream is dependent upon being able to bring the temperatures of the various catalytic beds up to operational temperatures . a subdivision of the steam reforming flow path into separate , independent flow sections has been presented in this disclosure as a means to reduce the mass , and therefore the time required , to heat just a portion of these critical catalytic beds to the necessary temperatures . another addition to that concept is the utilization of the thermally energetic gaseous flow that has left the active flow sections to pre - warm the beds of the inactive sections . once the reformate gas stream ( 250 ) has left a flow section , its thermal energy must be reduced from many hundreds of degrees centigrade to less than approximately 80 degree c . fig8 illustrates a method to capture some of this unwanted thermal energy using a heat exchange device ( 240 ) in the gas stream and to passively transfer ( 230 ) this energy back “ upstream ” into the inactive flow sections . fig8 shows two such flow sections , the primary section and other sections . the primary flow section is considered to be the first flow section that is ignited during every startup of the hydrogen gas generation system . once the product gases have left the catalytic beds of the primary flow section , the thermal energy of that gas stream is lost to the primary flow section . in order to recover additional benefit from the thermal energy of that gas stream , additional components are required . this additional recovery may be accomplished by using a gaseous compatible heat exchanger ( 240 ) device to transfer thermal energy from the exhaust ( 250 ) of the primary flow section to secondary , tertiary flow sections , and so on , into adjacent flow sections using conduction through transfer rods ( 230 ) into heat transfer plates ( 220 ). thermal energy applied to the heat transfer plates ( 220 ) will be conducted into the structure end plates ( 180 ), beginning the thermal heating of the adjacent flow section and associated catalytic beds through the previously described thermal transfer structures ( 50 ). the reformate discharge region ( 250 ) of each flow section needs to be configured to facilitate the attachment of a discharge manifold ( 260 ) that interconnects all of the various flow sections into a common discharge flue / manifold . the gaseous heat exchanger is preferably located in the common flue area of the discharge manifold , thereby offering the opportunity to transfer thermal energy to all possible flow sections . this presents the ability to preferentially conduct thermal energy from the primary flow section to the secondary flow section by selecting unique cross - sectional areas of the thermal transfer rods ( 230 ). preferential energy transfer to sequential , non - primary flow sections can be accomplished by designing the thermal transfer rods to each subsequent flow section to have different thermal conductance or capacitance . this approach is especially effective if each flow section has an independent external airflow control valve ( 20 ). a closed airflow control valve allows for no cooling gases ( air ) to flow past the catalytic beds of an adjacent flow section , the ability to transfer thermal energy to that flow section is significantly improved . as the secondary flow section is brought online , thermal energy will quickly stop flowing into that section as the exothermic output exceeds the conducted thermal energy potential of ( 240 ), ( 230 ) and ( 220 ). at this point , the tertiary flow section receives the majority of the recovered thermal energy of the combined gaseous discharge streams of the primary and secondary flow sections . fig8 does not show a thermal transfer rod ( 230 ) or a thermal plate ( 220 ) inserted into the primary flow section . though these devices may be placed in this section , this is only beneficial to starting the system if there is an external or alternative heating means applied to the gaseous heat exchanger ( 240 ). otherwise , a physical connection to the thermal transfer structure ( 50 ) of the primary flow section increases the time required to bring the various beds of that flow section up to operational temperatures . a final mechanism which dramatically increases the rate of thermal transfer to the flow section of either process configuration represented by fig2 or fig3 is the concentration level of the hydrogen peroxide itself . the greater the water content in the diluted hydrogen peroxide solution , the greater will be the portion of the dissociation energy absorbed by water . at some point , the quantity of water may become so great that there is insufficient energy to vaporize all of the water without an additional heating source . one source of this additional heat may be one of the active flow sections previously described utilizing the various passive thermal transfer mechanisms previously described . hydrogen peroxide commonly ranges in concentrations from about 70 % by weight to about 3 % by weight . a 70 % by weight peroxide is the typical output from production plant and is aggressively and highly exothermic in its dissociation . the concentration levels compatible with the hydrocarbon reforming processes of this invention are preferably between about 55 % by weight and about 40 % by weight . public safety issues would tend to strongly encourage the use of the lower concentration levels of hydrogen peroxide if not further reducing those levels below about 40 % hydrogen peroxide by weight . as previously described , once the reforming process is occurring , there is an over abundance of thermal energy available for use . while catalysts are more commonly used to dissociate hydrogen peroxide , thermal energy , in and of itself is sufficient to dissociate hydrogen peroxide . the only difficulty with low concentration levels of hydrogen peroxide would be during the initial startup of a cold reforming system . at “ cold ” start up conditions , the diluted hydrogen peroxide solution would still dissociate but the overall temperature will be reduced due to the presence of greater water concentrations and the lack of any additional heat from the reforming process . one solution to this problem , for either type of reforming system generally described by fig2 or fig3 , is the use of high concentrations of hydrogen peroxide to generate an initial large thermal surge within the flow section ( 10 ). then , as other thermal increases occur from the early chemical oxidation / reduction reactions of the hydrocarbon fuel , a transition can be made back to the more dilute hydrogen peroxide to continue the start of the flow section . while it is possible to manually fill two separate hydrogen peroxide tanks , one with a low concentration and the other with the higher concentration , this solution is only marginally better from a public safety perspective because there is less total volume of the higher concentration hydrogen peroxide being handled and shipped around the country . a preferred approach to address the thermal starting issues with highly dilute hydrogen peroxide includes the use of a concentrated quantity of the peroxide specifically for starting . to avoid the economic impracticality of two different concentrations of hydrogen peroxide available at all fueling stations , a portion of the diluted peroxide could be diverted from the system holding tank ( 1 , fig9 ) and then thermally heated ( 13 ) to evaporate off excess water , thereby increasing the concentration of the peroxide . this system is illustrated in fig9 . since hydrogen peroxide has a boiling point about 50 ° c . greater than water , it is relatively easy to preferentially evaporate water from the dilute mixture , thereby increasing the concentration of peroxide over water . the concentrated peroxide is then exclusively used to start the entire reforming process . by design , the concentration of the hydrogen peroxide is sufficiently high to completely vaporize all water present upon its dissociation as well as contain sufficient thermal energy to begin the heating of the flow section components . the concentration of peroxide needed may be determined through various approaches including measurement of specific conductance , ph , vapor pressure or density . all of these values vary in a quantitatively measurable and predictable fashion as the relative percentage of hydrogen peroxide varies . a direct or indirect measurement approach will need to be taken to determine the peroxide concentration . concentrating the hydrogen peroxide beyond about 65 % to about 70 % peroxide by weight is not beneficial . in fact , beyond this concentration , there is insufficient water ( steam ) to oxidize a fuel such as ethanol . the need for subsequent humidification of the final hydrogen feed stream , further increases the minimum amount of water required . additionally , peroxide in concentrations greater than 70 % becomes an increasingly aggressive oxidizer and a potential health hazard if it comes into contact with skin . measurement and control efforts ( 15 and 4 ) would need to be taken to assure that a maximum percent concentration as determined by the system requirements is not exceed . there are several potential thermal sources ( 14 ) that can be used to evaporate excess water from the diluted hydrogen peroxide / water solution . the best approach varies depending upon the system requirements of the application in which the fuel cell power system is installed . for an automotive application in which there is a significant electron storage capacity , ( regenerative braking , for example ) an electrical heating element would likely be the simplest and most cost efficient means of providing the thermal energy ( 14 ) necessary to evaporate the excess water . for other applications , the hot reformate gas stream can be the thermal energy ( 14 ) and allowed to pass through a heat exchanger , thereby transferring the necessary heat to vaporize the water directly . a more indirect approach is to pass the coolant from existing fcps heat exchangers ( 14 ) through a coiled tube inside the hydrogen peroxide concentrating vessel ( 13 ). two or more of the above methods can be integrated to meet multiple application requirements . for example , passive methods can be the primary mechanism used to concentrate the peroxide in order to minimize parasitic energy consumption . a back up system of indirect electrical element heating may be used as an emergency starting capability . the hydrogen peroxide concentrating vessel ( 13 ) needs to have several features . first among these is the need for the material to be compatible with concentrated h 2 o 2 . secondly , the vessel would need to be sealed , or sealable , from the environment as well as pressure capable since the fluids are being heated , which will increase the vapor pressure . since vapor pressure , as a function of temperature and percent concentration of peroxide is one means to determine concentration , this is one preferable approach to concentration determination ( 15 , 4 ). upon heating the peroxide in the concentration vessel to a measured , predetermined temperature value , there will be some unique vapor pressure specific to the percent concentration of peroxide to water . at a predetermined , and / or controller - selectable vapor pressure point , selected to maximize the rate of water evaporation or oppositely minimize the quantity of hydrogen peroxide contained in the trap vapor , a vent ( 16 ) could be opened to vent the water vapor . the continued heating and subsequent venting of vapor would continue until a determination was made that the hydrogen peroxide solution was at the necessary percent concentration . the vessel also needs to include a safety vent mechanism in the case of run away pressure buildup . a second peroxide concentrating vessel may be added to ensure an adequate supply for all start / stop scenarios . while one vessel , which has previously concentrated its quantity of peroxide to the necessary level , is being used to start the reformer system , a second vessel is active in concentrating its portion of diluted peroxide . in order to minimize the loss of peroxide during this process , temperatures well away from the boiling point of peroxide may be selected . the process controller is able to select the most appropriate temperature value and adjust that value as the concentrating process proceeds or the starting demands change . because there is substantial run time after each start of the fcps , the concentration of peroxide need not be an aggressive accelerated process . the foregoing description of the present invention has been presented for purposes of illustration and description . furthermore , the description is not intended to limit the invention to the form disclosed herein . consequently , variations and modifications commensurate with the above teachings , and the skill or knowledge of the relevant art , are within the scope of the present invention . the embodiments described hereinabove are further intended to explain the best mode known for practicing the invention and to enable others skilled in the art to utilize the invention in such , or other , embodiments and with various modifications required by the particular applications or uses of the present invention . it is intended that the appended claims be construed to include alternative embodiments to the extent permitted by the prior art .