Device and method for providing electrical energy by means of a hydrogen carrier medium, and mobile platform having such a device

Abstract

The invention relates to a device (5) for providing electrical energy by means of a hydrogen carrier medium, the device comprising: a dehydrogenation unit (9), which has a first dehydrogenation reactor (56), for releasing hydrogen gas from the hydrogen carrier medium; a current-generating unit (17), fluidically connected to the dehydrogenation unit (9), for generating electrical current from the released hydrogen gas; an electronics unit (23), electrically connected to the current-generating unit (17), for storing and / or controlling the generated electrical current; and an activation unit (29) for activating the device (5), wherein the activation unit (29) comprises an energy source (27, 28) for heating the first dehydrogenation reactor (56).

Description

[0001] Device and method for providing electrical energy by means of a hydrogen carrier medium and mobile platform with such a device

[0002] This patent application claims priority from German patent application DE 10 2022 206 342.2, the contents of which are incorporated herein by reference.

[0003] The invention relates to a device and a method for providing electrical energy by means of a hydrogen carrier medium and to a mobile platform with such a device.

[0004] DE 10 2020 102 923 A1 discloses a road vehicle carrying a hydrogen carrier that is powered by an electric motor. The electrical power required for this is generated by a fuel cell powered by hydrogen gas released from a hydrogen carrier medium. The hydrogen gas is released from the hydrogen carrier medium in a dehydrogenation unit at elevated temperatures. To ensure a sufficient supply of hydrogen gas to the fuel cell, it is therefore necessary that the dehydrogenation unit be permanently kept at operating temperature. This procedure is associated with high energy consumption and is not ecologically sensible. Alternatively, the dehydrogenation unit can be warmed up and brought to operating temperature when the fuel cell is to be operated. In particular, heating up from a standby mode can lead to undesirable decelerations that impair the vehicle's dynamics.

[0005] The invention is based on the object of improving the provision of electrical energy by means of a hydrogen carrier medium and in particular of improving the provision from a standby mode in such a way that the provision from the standby mode is possible autonomously and in particular without external energy supply and in particular the provision time is shortened.

[0006] This object is achieved according to the invention by a device having the features of claim 1 and by a method having the features of claim 13. The core of the invention is that a device for providing electrical energy by means of a hydrogen carrier medium can be activated by means of an activation unit, in particular without energy other than the hydrogen carrier medium being supplied from outside the device for activation. Activation takes place in particular by heating a first dehydrogenation reactor of a dehydrogenation unit, which serves to release hydrogen gas from the hydrogen carrier medium. The activation unit comprises a heating unit. The heating unit is in particular a separate component and in particular not the dehydrogenation unit itself.The heating for activating the device, in particular the dehydrogenation unit and in particular the first dehydrogenation reactor, is in particular not heat recovery from the dehydrogenation unit.

[0007] It has been found that the activation unit improves the operation of the device from a sleep mode. In the sleep mode, the dehydrogenation unit, and in particular the first dehydrogenation reactor, is inactive. The activation unit enables, in particular, immediate operation of the device from the sleep mode. The activation unit enables a so-called cold start of the device and, in particular, a cold start of an electric motor drive that is electrically connected to the device. The activation unit is also referred to as a cold start unit.

[0008] The activation unit comprises an energy source, in particular one with a cold start capability. The cold start capability is, in particular, a heating unit.

[0009] An electrical energy source, in particular an electronic unit suitable for storing electrical current, serves as a cold-startable energy source, wherein separate electrical energy storage devices, in particular rechargeable batteries, can also be present. The electrical energy source is used in particular to operate an electric heating unit. Additionally or alternatively, hydrogen, which is temporarily stored in the device in gaseous form, can serve as a cold-startable energy source. The temporarily stored hydrogen is also present in particular in the device's idle mode, i.e. before the device is activated from idle mode. The hydrogen can be thermally utilized, in particular burned, or converted into heat in a catalytic oxidation process.Additionally or alternatively, another fuel, in particular a fossil fuel and / or a liquid organic hydrogen carrier medium (LOHC), can serve as a cold-start energy source. This other fuel can be partially oxidized, in particular by catalytic means, thus releasing heat.

[0010] A heat source external to the device can also serve as a cold-start energy source, allowing heat to be provided independently of the device, especially when the device is in standby mode. External heat sources include, in particular, other process equipment such as motors or turbines.

[0011] It is conceivable that the external and / or internal heat sources feed a heat storage unit. This allows for flexible heat supply over time. In particular, heat from the heat sources can be stored and used when no cold start is required at the time of heat generation. The heat storage unit itself can serve as a cold-start energy source. The heat storage unit can be designed as a latent heat storage unit and / or as a thermochemical heat storage unit.

[0012] In particular, a time delay between a request for power from the electric motor drive and the provision of the electrical power from a power generation unit is a maximum of twelve hours, in particular a maximum of eight hours and in particular a maximum of six hours.

[0013] Hydrogen gas can be reversibly released from the hydrogen carrier medium and chemically bound to it again. Such a hydrogen carrier medium is, in particular, liquid and, in particular, a liquid organic hydrogen carrier medium (LOHC). A hydrogen carrier medium that is present in an at least partially hydrogen-laden form as perhydrodibenzyltoluene (HisDBT), perhydrobenzyltoluene (H12BT), methylcyclohexane (C7H14), which is dehydrogenatable to toluene (C?Hs), and / or dicyclohexane has proven particularly suitable. It is also possible to use a mixture of hydrogen carrier media in the at least partially hydrogen-laden form of perhydrodiphenylmethane and perhydrobiphenyl. These compounds can be dehydrogenated to diphenylmethane and biphenyl. A mixture of biphenyl to diphenylmethane in a ratio of 30:70, in particular 35:65, and especially 40:60 is particularly advantageous.The dehydrogenation of the hydrogen carrier medium in the dehydrogenation unit is catalytic, i.e., it occurs in the presence of a catalyst. The catalyst comprises a catalyst support on which catalytically active catalyst material is arranged and, in particular, attached. The catalyst material comprises, in particular, a metal, in particular platinum, palladium, nickel, rhodium, and / or ruthenium. Aluminum oxide, silicon oxide, titanium oxide, zirconium oxide, and / or activated carbon are used as catalyst supports. The catalyst support is, in particular, a porous oxide support. The catalyst support is, in particular, inert. The weight fraction of the catalyst material, based on the catalyst support, is between 0.1% and 10%.

[0014] The catalyst comprises a plurality of catalyst particles, in particular catalyst support particles, which are present in particular as pellets. The catalyst particles have an average particle size of 0.5 mm to 10 mm, in particular of 1 mm to 8 mm, and in particular of 2 mm to 4 mm. The catalyst particles are arranged in particular in the form of a fixed bed through which the hydrogen carrier medium flows.

[0015] A power generation unit is fluidly connected to the dehydrogenation unit. In the power generation unit, electrical power is generated from the released hydrogen gas. It is advantageous if waste heat is generated during operation of the power generation unit, i.e., if the power generation unit also generates heat in addition to electricity.

[0016] In particular, it has been found that electrical power and / or heat generated by the power generation unit can be used in particular for operating the device itself and can be delivered in particular to external consumers, which are arranged in particular outside the device. In particular, the dehydrogenation unit is connected to the power generation unit in a heat-transfer manner. In particular, a heat circuit, in particular a closed one, is provided to transfer waste heat from the power generation unit to the dehydrogenation unit. The closed heat circuit comprises in particular at least one heat transfer medium that does not leave the process and is therefore retained without loss. In particular, energy loss in the form of anergy can be reduced. Such a device is particularly energy-efficient and therefore ecologically and economically sensible.The operation of the device is efficient and self-sufficient, especially with regard to activating the device using the activation unit.

[0017] Autonomous operation during activation means that external energy, i.e., energy from outside the device, is supplied exclusively in the form of the hydrogen carrier medium. Electrical energy stored in the device can be used to operate the activation unit.

[0018] The electronics unit is electrically connected to the power generation unit. The electronics unit serves to store and / or control the electrical power generated in the power generation unit. The power generation unit comprises, in particular, a power storage element, in particular a battery.

[0019] In particular, it was found that the volume requirement for hydrogen gas buffer storage in the device can be reduced and, in particular, eliminated. In particular, it is not necessary to retain hydrogen gas in the device, even in small quantities, to enable a cold start. Nevertheless, hydrogen gas can be present in small quantities, for example, in fluid lines, even in the device's idle mode. However, this does not increase the volume requirement for the hydrogen gas buffer storage.

[0020] The dehydrogenation unit comprises, in particular, the first dehydrogenation reactor, referred to as the starter reactor or first-stage reactor, and a second dehydrogenation reactor, referred to as the main reactor or second-stage dehydrogenation reactor. The second dehydrogenation reactor is connected downstream of the first dehydrogenation reactor. The two dehydrogenation reactors are arranged in series. It is possible to arrange additional dehydrogenation reactors in series between the starter reactor and the main reactor. The first and second dehydrogenation reactors can be structurally separated from one another or designed as an integrated reactor unit in a common housing.

[0021] When the device is activated, the activation unit is coupled, in particular, to the starter reactor for its heating. In addition, the main reactor can also be heated during activation. During regular operation, i.e., after activation, the main reactor is essentially and exclusively heated. During activation, the starter reactor is, in particular, the only dehydrogenation reactor in operation.

[0022] In regular operation, the dehydrogenation unit can be operated in multiple stages, particularly in two stages, with the starter reactor serving as the first-stage dehydrogenation reactor upstream of the main reactor serving as the second-stage dehydrogenation reactor. In the starter reactor, the at least partially loaded hydrogen carrier medium is first partially dehydrogenated and then passes through the activated main reactor for further dehydrogenation.

[0023] In the regular operating mode, a cascade start-up process is particularly possible, in which the dehydrogenation reactor of the next higher stage is activated whenever the dehydrogenation reactor of the previous stage is fully activated, and in particular has reached or exceeded a variably defined power threshold. This power threshold can, for example, be at least 50% of the rated power of the respective dehydrogenation reactor or more. For the cascade start-up process, it is energetically advantageous if the size of the dehydrogenation reactors increases along the fluid flow direction from the starter reactor to the main reactor, in particular continuously. It is therefore advantageous if the starter reactor has the smallest reaction volume and the main reactor the largest.

[0024] A device according to claim 2 simplifies the direct provision of heat for heating the dehydration unit. A heat generation unit can, for example, be electrically designed. This means that heat is generated by means of electrical current. In this case, the heat generation unit is electrically connected, in particular, to a power source. The power source can be a connection to an electrical grid, in particular a local or global power grid. The power source can also be a power storage unit, in particular in the form of a battery, which simplifies the autonomous operation of the device. Additionally or alternatively, the electrical current can also originate from the electronics unit powered by the power generation unit, wherein the electronics unit was, in particular, powered at an earlier time with electrical current generated by the power generation unit.The heat can advantageously be transferred to the dehydrogenation unit by means of a heat transfer unit. A heat transfer unit can, for example, comprise a heat transfer circuit carrying a heat transfer fluid, with thermal oil serving as the heat transfer fluid. The heat transfer fluid is directly heated by the heat generation unit, in particular the electric heater, and conveyed to the dehydrogenation unit by means of the heat transfer unit. The heat transfer fluid can transfer the heat to the dehydrogenation unit and be conveyed back to the heat generation unit, and in particular, reheated.

[0025] The heat generation unit can also comprise a chemical reactor, in particular an oxidation reactor. For example, the hydrogen carrier medium already present in the device can be at least partially oxidized. This oxidation reaction is exothermic and allows the provision of heat for the dehydrogenation unit. Additionally or alternatively, complete oxidation of the hydrogen carrier medium by combustion is possible.

[0026] Alternatively, the heat generation unit can also be arranged integrated in the power generation unit and / or in a post-treatment unit, in particular as a subordinate unit of the power generation unit and / or the post-treatment unit.

[0027] Activating the device, in particular the first dehydrogenation reactor and in particular other units of the device, requires electrical power and heat. During regular operation of the device, i.e., after the device has been activated by the activation unit and is in a quasi-stationary dehydrogenation mode, electricity and heat are still required. In particular, dehydrogenation in the dehydrogenation unit occurs endothermically, i.e., by means of heat input. A heat generation unit, a heat transfer unit, and a power generation unit are therefore advantageous for both operating the device in activation mode and in regular dehydrogenation mode.

[0028] It may be advantageous to provide precisely one heat generation unit, precisely one heat transfer unit, and precisely one power generation unit that are used for both operating modes. Alternatively, at least one, several, or all units can be provided multiple times in order to operate them separately in the respective operating mode. A device according to claim 3 enables improved heat provision for cold starts. The integrated arrangement of the activation unit in the dehydrogenation unit, in particular in the first-stage dehydrogenation reactor, enables a compact and small-sized device. Heat transfer losses are reduced. It is particularly possible for the heat generation unit, in particular in the form of the oxidation reactor and / or in the form of a combustion unit, to be integrated into the dehydrogenation unit, in particular in the first-stage dehydrogenation reactor.

[0029] It is particularly advantageous to design the first-stage dehydrogenation reactor with at least one double-walled tube, so that an inner reaction chamber and an outer reaction chamber surrounding the inner reaction chamber are formed. The dehydrogenation reaction can take place in one of the reaction chambers. Heat generation and / or heat transfer can take place in the other reaction chamber. It is particularly advantageous if the outer reaction chamber is a reaction tube of the first-stage dehydrogenation reactor. In particular, catalyst material is present in the reaction tube in order to be contacted with the at least partially loaded hydrogen carrier medium for its dehydrogenation. The inner reaction chamber serves to generate and / or transfer heat, in particular from a heat transfer fluid.In this configuration, the outer reaction chamber can be heated from the inside, in particular by the heat transfer fluid, and on the outside by an additional heat transfer fluid. The exothermic oxidation reaction and / or combustion can also take place directly in the inner reaction chamber.

[0030] A fluidic connection of the activation unit to the dehydrogenation unit according to claim 4 enables the provision of hydrogen gas from the dehydrogenation unit for operating the activation unit. In particular, the first-stage dehydrogenation reactor is fluidic connected to the activation unit. The activation unit can be operated directly with the hydrogen provided in the first-stage dehydrogenation reactor, thus providing electricity and heat for activating the device. In particular, the dehydrogenation unit is designed in several stages, in particular in two stages. Upon activation of the device, the starter reactor functions as a release device. After activation of the device, the starter reactor can serve as a precursor to the main reactor of the dehydrogenation unit. In particular, the starter reactor can be structurally combined with a recuperator in one apparatus.Such an apparatus, which represents the first dehydrogenation stage, is traversed by three different media. The first medium is an at least partially charged hydrogen carrier medium, which is dehydrogenated. During activation, a liquid heat transfer medium flows through the apparatus in a second media region as the second medium. The third medium is an at least partially discharged hydrogen carrier medium, which originates in particular from the main reactor. The third medium is therefore in particular the reaction product from the main reactor, in particular an at least partially discharged hydrogen carrier medium, which can be passed through the starter reactor as an integrated recuperator for heat dissipation, in particular in countercurrent.

[0031] After activation, the third medium passes through a third media zone. The second media zone can remain unused or can be additionally flowed through by liquid and / or gaseous heat transfer medium. It is advantageous if the second media zone is located internally, i.e., centrally and concentrically with respect to the first media zone, in the starter reactor. Instead of a heat transfer medium such as thermal oil, heating elements can also be arranged centrally to heat the liquid heat transfer medium.

[0032] It is advantageous to feed the material flows generated in the dehydrogenation unit, in particular between the starter reactor and the main reactor, to the activation unit or the power generation unit, depending on the operating mode. For this purpose, it is advantageous if appropriate valves and / or pumps are present to control the material flows, in particular by means of a control unit, in particular in an automated manner. In the multi-stage design of the dehydrogenation unit, it has proven advantageous if the ratio of the dehydrogenation output of the starter reactor to the dehydrogenation output of the main reactor is set such that the temporarily stored electrical energy required for activation is less than 100 kWh per MW of dehydrogenation output and the activation duration is less than 6 hours.

[0033] A device according to claim 5 enables the overall efficiency to be increased. A purification unit is arranged downstream of the dehydrogenation unit and serves to purify the hydrogen gas released in the dehydrogenation unit. During activation operation of the device, exclusively hydrogen gas released in the starter reactor is fed to the purification unit. During regular operation of the device, a hydrogen gas stream generated in the starter reactor and / or main reactor is fed to the purification unit. The hydrogen gas leaving the purification unit has a purity of at least 98%, in particular at least 99%, in particular at least 99.9%, in particular at least 99.99%, and in particular at least 99.999%. A purity of 99% means that the proportion of impurities in the hydrogen gas stream is 1%. The purification unit is arranged in particular upstream of the power generation unit.Such a pure hydrogen gas stream can be converted into electricity particularly efficiently. The purification unit is designed as a pressure swing adsorption device.

[0034] A post-treatment unit according to claim 6 ensures targeted treatment of material streams. The post-treatment unit comprises, in particular, a hydrogen burner and can be used, for example, to provide heat for the dehydrogenation unit. The post-treatment unit is arranged, in particular, downstream of the dehydrogenation unit and, in particular, downstream of the purification unit. In particular, residual gas separated from the hydrogen gas in the purification unit, which is also referred to as off-gas, can be discharged to the post-treatment unit and burned there. A control system such that a required amount of hydrogen is separated from the off-gas in the purification unit, which amount is required in the hydrogen burner of the post-treatment unit, is particularly advantageous. An off-gas proportion from the purification unit of at least 5%, in particular at least 10%, and, in particular, at least 30% has proven advantageous.The design of the cleaning unit, especially in the form of a pressure swing adsorption apparatus, is therefore particularly uncomplicated, space-saving and cost-efficient.

[0035] Pressure swing adsorption enables the release of hydrogen gas, particularly with improved purity. This is achieved by frequent pressure changes, which result in short cycle times. With an increased amount of adsorbent material, the purity of the hydrogen gas can be further increased. Additionally or alternatively, a relatively large pressure difference during the pressure changes can further improve hydrogen purity. Conversely, this means that with constant hydrogen gas purity and, for example, more frequent pressure changes, the amount of adsorbent material and / or the relative pressure difference and the associated power consumption for the vacuum pump and / or compression can be reduced.

[0036] In particular, it was recognized that even comparatively frequent pressure changes, i.e., short cycle times, are unproblematic with regard to the overall efficiency of the process, although more frequent pressure changes and short cycle times result in a reduced yield of purified hydrogen gas and thus an increased off-gas flow. It has proven advantageous if the off-gas content from the purification unit is no more than 10%, and in particular no more than 5%. It is advantageous if the off-gas content is as small as possible. However, it was recognized that a comparatively large off-gas content is acceptable, since the off-gas flow can be advantageously utilized thermally in the aftertreatment unit.

[0037] The post-treatment unit serves in particular as a filter and / or burner unit, the waste heat of which can be efficiently used in the device.

[0038] A fuel cell according to claim 7 enables direct and efficient conversion of the released hydrogen gas into electricity. The overall efficiency of the device can be increased, in particular, if various operating points of the device are suitably defined. From a full-load operating point, at which the dehydrogenation unit is operated at a nominally maximum release rate, the device can be controlled to a partial-load or minimum-load operating point by reducing the reaction pressure and the hydrogen gas release rate and increasing the dehydrogenation stroke in the dehydrogenation unit. Additionally or alternatively, in the power generation unit, in particular in the fuel cell, the inlet pressure can be reduced, the degradation reduced, and / or the efficiency increased.

[0039] The fuel cell is, in particular, a proton exchange membrane (PEM) fuel cell. It is advantageous if, in addition to the PEM fuel cell, a hydrogen burner, in particular a catalytic one, is connected to the dehydrogenation unit in a heat-transfer manner. This hydrogen burner serves as a heat source, particularly both during activation and in regular operating mode. At least a portion of the hydrogen gas stream released in the dehydrogenation unit can be fed to the hydrogen gas burner, burned, and thus generate heat that can be used to operate the dehydrogenation unit.

[0040] The operating temperature of the PEM fuel cell is typically between 60°C and 120°C. The PEM fuel cell can be designed as a high-temperature or low-temperature PEM fuel cell.

[0041] Alternatively, the fuel cell can also be designed as a solid oxide fuel cell (SOFC) and / or as a solid acid fuel cell (SAFC).

[0042] It is particularly conceivable to combine different fuel cell components in a fuel cell unit. For example, such a fuel cell unit can comprise at least one SOFC element, also referred to as an SOFC stack, and at least one PEM fuel cell element, referred to as a PEM stack. The PEM stack particularly simplifies cold starting of the device, as the operating temperature is lower than that of the SOFC. Waste heat from the SOFC can then be advantageously used for heat recovery for hydrogen release in the dehydrogenation unit.

[0043] With a high-temperature fuel cell, particularly SOFC, SAFC, or a high-temperature PEM fuel cell, waste heat can be transferred to the dehydrogenation unit and utilized particularly advantageously. In particular, exhaust gas from the high-temperature fuel cell, especially used air, can be used to provide heat for the dehydrogenation unit.

[0044] It is particularly conceivable for additional heat generation to occur by passing exhaust gas from the fuel cell to the aftertreatment unit and oxidizing unused hydrogen gas in the aftertreatment unit. In particular, the aftertreatment unit can be operated flexibly so that exhaust gas from the fuel cell and / or from the purification unit is used. Additionally or alternatively, hydrogen gas, in particular from the dehydrogenation unit, can also be used directly to generate heat in the aftertreatment unit. It has been found that the heat provided by the fuel cell can be advantageously used for the dehydrogenation unit if the air-hydrogen ratio in the high-temperature fuel cell is at most 10, in particular at most 5, and in particular at most 3.It has been found that a significant portion of the thermal energy generated as waste heat in the power generation unit can be made available in the dehydrogenation unit particularly advantageously through direct heat extraction. In particular, waste heat is extracted from the exhaust stream of the power generation unit and / or heat is transferred from the power generation unit to the dehydrogenation unit via a closed heat cycle. In this case, a reduced excess air occurs at the power generation unit, resulting in a reduced air-to-hydrogen ratio. The waste heat is reliably removed from the high-temperature fuel cell. The heat required for the dehydrogenation reaction in the dehydrogenation unit can be covered up to 100% by the waste heat from the high-temperature fuel cell.

[0045] In addition to or as an alternative to a fuel cell, the power generation unit can comprise a hydrogen combined heat and power plant, a catalytic hydrogen burner, a conventional hydrogen burner, a gas turbine, and / or a hydrogen combustion engine. The hydrogen combustion engine and / or the gas turbine can each be coupled to at least one generator, in particular a turbogenerator, for power generation.

[0046] The waste heat generated at the power generation unit can additionally or alternatively be used as thermal energy within the device, in particular in the dehydration unit, or outside the device and provided accordingly.

[0047] A device according to claim 8 enables particularly efficient heat removal from the power generation unit, in particular from the fuel cell and in particular the solid oxide fuel cell, from the gas turbine and / or from the hydrogen combustion engine, and the transfer of the heat to the dehydrogenation unit. Alternatively, the heat from the power generation unit, in particular from the fuel cell and in particular the solid oxide fuel cell, from the gas turbine and / or from the hydrogen combustion engine, can also be dissipated to another heat sink, in particular to another heat exchanger. The device enables at least partial direct heat removal from the power generation unit, in particular from the fuel cell and in particular the solid oxide fuel cell, from the gas turbine and / or from the hydrogen combustion engine, thereby improving the overall efficiency of the process.

[0048] For heat transfer, a heat circuit, in particular a closed one, is arranged in the device. It is understood that the heat circuit can also be designed by at least two heat transfer media with at least one intermediate heat exchanger connected between them, i.e., in particular, as a so-called open heat circuit, for example, to decouple individual heat transfer steps from one another temporally and / or spatially.

[0049] A device according to claim 9 enables a robust dehydrogenation reaction. In particular, the dehydrogenation unit can be easily scaled in terms of its performance. In particular, the integration of the activation unit into the dehydrogenation unit is simplified by designing the reaction tubes, in particular of the starter reactor, as double-walled tubes. Since the dehydrogenation reaction is a catalytic reaction, the catalyst is arranged in at least one reaction tube. The tube bundle reactor comprises, in particular, a plurality of reaction tubes, in particular at least 5, in particular at least 10, in particular at least 15, in particular at least 25, in particular at least 40, in particular at least 50, in particular at least 100, in particular at least 200, in particular at least 500, and in particular at most 1000 reaction tubes.

[0050] In the main reactor, the reaction tubes can be simple and, in particular, without double walls. The main reactor is, in particular, a tube bundle reactor, as described in DE 10 2015 219 305 A1.

[0051] A resource unit according to claim 10 enables an increase in the degree of self-sufficiency. The device enables, in particular, the generation and provision of compressed air, nitrogen, and / or cooling water within the device itself. Compressed air is generated, in particular, by means of a compressor. A control unit according to claim 11 enables controlled and, in particular, fully automatic operation of the device. In particular, the control unit enables a control-technical coupling with the electric motor drive.

[0052] The degree of energy self-sufficiency is understood to be the proportion of energy provided by a primary energy source, i.e., by the hydrogen carrier medium, relative to the total energy supplied to the device, including activation. The degree of energy self-sufficiency is, in particular, at least 50%, in particular at least 90%, and in particular 100%.

[0053] A mobile platform according to claim 12 essentially has the advantages of the device according to the invention, to which reference is hereby made. The mobile platform has the device and can be driven independently by means of the electric motor drive, which is supplied with electrical power by the device. The mobile platform is in particular a vehicle, in particular a land vehicle such as a motor vehicle or a truck, a rail vehicle such as a train, or a watercraft such as a ship. The mobile platform can also be an aircraft or helicopter. In particular, the electric motor drive is electrically connected to the power generation unit of the device. In particular, the control unit of the device is connected to a central control of the mobile platform or integrated therein.

[0054] A method according to claim 13 essentially has the advantages of the device according to the invention, to which reference is hereby made. The method simplifies a cold start of the power generation unit.

[0055] In particular, the activation of the device by means of the activation unit is improved by heating the first dehydrogenation reactor by means of the heating unit. The first dehydrogenation reactor forms a starter reactor during activation. The starter reactor initially releases a small amount of hydrogen gas, whereby this initially released hydrogen gas can be used to provide additional heat and / or electrical current in order to provide further heat or activation energy in another form. The device can be operated in a so-called hot standby mode by generating at least, and in particular exactly, the amount of thermal and electrical energy required to maintain a self-sufficient operating mode. In particular, in hot standby mode, sufficient thermal and electrical energy is generated to compensate for heat losses and operating energy.The energy required for this purpose shall in particular be no more than 25% of the nominal energy generation capacity and in particular no more than 10% of the nominal energy generation capacity and in particular at least 3% of the nominal energy generation capacity.

[0056] An energetically advantageous operation of the device results from arranging components of the device whose surfaces are at a temperature level of at least 200°C in a first room and components whose surfaces are at a temperature level of less than 200°C in a second room. The first room has a first room temperature of at most 90°C, in particular at most 70°C. The second room has a second room temperature, which is in particular at most 60°C and in particular at most 45°C. The first and / or the second room are in particular air-conditioned.

[0057] In the first space, in particular the dehydrogenation unit with the starter reactor and the main reactor, the recuperator, the heating unit, in particular heat fluid lines and / or further components of the heat fluid system, the aftertreatment unit, in particular at least partially, and / or the power generation unit, in particular at least partially in the form of a high-temperature fuel cell system, are arranged.

[0058] In particular, storage containers for the at least partially loaded and / or at least partially discharged hydrogen carrier medium, the control unit, the cleaning unit and / or further parts of the high-temperature fuel cell system are arranged in the second space.

[0059] A method according to claim 14 enables a particularly advantageous use of the device. In particular, it was recognized that the starter reactor can also be used for regular operation of the device as a component of the dehydrogenation unit. The dehydrogenation unit comprises, in particular, a second dehydrogenation reactor connected downstream of the first dehydrogenation reactor. In particular, it was recognized that the starter reactor can be used in two different functions: in addition to the initial dehydrogenation for the initial provision of hydrogen gas to activate the device, it can also be used as a first-stage dehydrogenation reactor in the multi-stage dehydrogenation unit.

[0060] A method according to claim 15 increases the flexibility during cold starting, in particular in the selection of the heating unit.

[0061] A method according to claim 16 enables particularly advantageous energy recovery, especially during regular operation of the device. In the first dehydrogenation reactor, in addition to the first-stage dehydrogenation reaction, an integrated heat transfer to the reaction tubes in the dehydrogenation reactor also takes place. A product stream from the second dehydrogenation reactor serves as the heat transfer fluid, in particular. Recuperation takes place in the first dehydrogenation reactor.

[0062] A method according to claim 17 enables an advantageous and, in particular, automated and, in particular, fully automatic change of operating modes, in particular from an activation mode to regular operation and / or from regular operation to a rest or standby mode. The change of these operating modes particularly affects the first dehydrogenation reactor and / or the second dehydrogenation reactor.

[0063] A method according to claim 18 has proven to be particularly efficient. In particular, the device can be operated inexpensively in a standby mode. The standby mode is also referred to as standby operation. In the standby mode, either exclusively the power generation unit or the power generation unit with other power-consuming components of the device is operated with sufficient power and heat. This means that the power generation unit and these other components are not switched off and are available for regular operation at short notice. In particular, it was found that the amount of hydrogen gas required for this purpose is reduced and can be made available in a straightforward manner, particularly due to the size of the first dehydrogenation reactor. In particular, it was found that it is not necessary to operate the second dehydrogenation reactor for this reason.In particular, it was recognized that the second dehydrogenation reactor cannot readily provide a correspondingly reduced amount of hydrogen gas, especially because the amount of hydrogen gas provided by the second dehydrogenation reactor is too large. Therefore, it is not necessary to temporarily store excess hydrogen gas provided by the second dehydrogenation reactor but not required for idle operation. This type of idle operation is particularly efficient.

[0064] In particular, when a switching temperature is reached in the second dehydrogenation reactor, the first dehydrogenation reactor can be switched from the activation mode to the regular operating mode. The first dehydrogenation reactor then serves as the starter reactor for the multi-stage dehydrogenation unit. The switching temperature in the second dehydrogenation reactor is in particular at least 280°C, in particular at least 300°C, and in particular at least 320°C.

[0065] Additionally or alternatively, switching is also possible depending on the hydrogen gas release rate in the first dehydrogenation reactor. A minimum value for the hydrogen gas release rate is, in particular, 50% of a nominal hydrogen gas release rate of the first dehydrogenation reactor, in particular at least 70%, in particular at least 90%, and in particular 100% of the nominal hydrogen gas release rate. The hydrogen gas release rate is a project-specific and / or reactor-specific parameter and depends, in particular, on the respective reactor volume and / or the catalyst requirement.

[0066] In particular, it is possible to switch the first dehydrogenation reactor from the regular operating mode back to the activation mode or to a rest or standby mode when the switching temperature in the second dehydrogenation reactor and / or the hydrogen gas release performance fall below the above-mentioned minimum values.

[0067] Both the features specified in the patent claims and the features specified in the exemplary embodiment of a device according to the invention are suitable, either individually or in combination with one another, for further developing the subject matter of the invention. The respective combinations of features do not represent any limitation with regard to further developments of the subject matter of the invention, but are essentially merely exemplary in nature.

[0068] Further features, advantages, and details of the invention will become apparent from the following description of an embodiment with reference to the drawings. They show:

[0069] Fig. 1 is a schematic representation of a mobile platform with a device according to the invention,

[0070] Fig. 2 is a plan view of a first stage dehydrogenation reactor of a dehydrogenation unit of the device according to claim 1,

[0071] Fig. 3 is a sectional view along section line III-III in Fig. 2,

[0072] Fig. 4 is an enlarged detail view of detail IV in Fig. 3,

[0073] Fig. 5 is a sectional view rotated by 90° along section line VV in Fig. 2,

[0074] Fig. 6 is an enlarged detailed view of detail VI in Fig. 5.

[0075] A mobile platform, shown purely schematically in Fig. 1 and designated by 1, can be designed as a vehicle, in particular a land vehicle or a watercraft, in particular a ship or an aircraft. The mobile platform 1 has an electric motor drive 2, which is operatively connected to drive elements (not shown), such as wheels or a drive turbine. The drive 2 generates and provides a driving force to drive the drive elements.

[0076] The mobile platform 1 has a central controller 3, which is in particular bidirectionally connected to the drive 2. The bidirectional signal connection is symbolized by the double arrow 4 in Fig. 1. The central controller 3 has, in particular, power electronics, which are used, in particular, to control the drive 2, to communicate with a vehicle control system (not shown), and / or to diagnose the drive 2. The power electronics can include an electronic control unit, an inverter, and a DC / DC converter.

[0077] The mobile platform 1 comprises a device, designated as a whole by 5. The device 5 serves to provide electrical energy using a hydrogen carrier medium. The device 5 is electrically connected to the drive 2 via electrical lines 6.

[0078] The device 5 comprises a storage container 7, which is connected to a dehydrogenation unit 9 via a first fluid line 8. In the dehydrogenation unit 9, the hydrogen carrier medium is dehydrogenated, thereby releasing hydrogen gas.

[0079] According to the illustrated embodiment, the dehydrogenation unit 9 is designed as a multi-stage unit, in particular a two-stage unit. The dehydrogenation unit 9 comprises a first dehydrogenation reactor 56, referred to as the starter reactor, and a second dehydrogenation reactor 57, referred to as the main reactor.

[0080] The dehydrogenation reactors 56, 57 are fluidically connected to one another, in particular by means of a fluid line.

[0081] The dehydrogenation unit 9, in particular the first dehydrogenation reactor 56 and / or the second dehydrogenation reactor 57, is fluidly connected to the first storage tank 7 via a return line 10. The storage tank 7 has a first sub-chamber 11, in which at least partially loaded hydrogen carrier medium is stored, and a second sub-chamber 12, in which at least partially discharged hydrogen carrier medium is stored. The sub-chambers 11, 12 are separated from one another by a partition 13, in particular a fluid-tight one. The partition 13 can also be designed to be partially permeable. The partition 13 can also be designed to be variably arranged in the storage tank 7 in order to adapt the volumes of the sub-chambers 11, 12. It is conceivable to design the storage tank 7 as a so-called stratified storage system. Such a stratified storage system is disclosed in DE 10 2016 206 106 A1, to which reference is hereby expressly made with regard to design and operation.

[0082] Alternatively, it is also possible to provide a further storage container (not shown) in addition to the storage container 7. In this case, the storage container 7 is designed to store the at least partially charged storage medium, and the further storage container is designed to store the at least partially discharged hydrogen carrier medium.

[0083] A purification unit 15 is connected to the dehydrogenation unit 9 via a second fluid line 14. In particular, both the first dehydrogenation reactor 56 and the second dehydrogenation reactor 57 are each directly fluidically connected to the purification unit 15. Depending on the operating mode of the device 5, either the first dehydrogenation reactor 56 and / or the second dehydrogenation reactor 57 can be connected to the purification unit 15. According to the illustrated embodiment, the purification unit 15 is designed as a pressure swing adsorption apparatus.

[0084] It is possible to arrange a separation unit (not shown) between the dehydrogenation unit 9 and the purification unit 15 in order to separate components of the hydrogen carrier medium, particularly vaporous and / or droplet-shaped components, from the hydrogen gas. The separation unit comprises, in particular, a condenser.

[0085] In the purification unit 15, the hydrogen gas released in the dehydrogenation unit 9 is purified and fed to a power generation unit 17 via a third fluid line 16. The power generation unit 17 has a fuel cell 18, which, according to the illustrated embodiment, is designed as a proton exchange membrane (PEM) fuel cell. The third fluid line 16 opens, in particular, into the fuel cell 18.

[0086] The power generation unit 17 further comprises a heating unit 19, which is coupled to the dehydrogenation unit 9 in a heat-transfer manner, allowing a heat flow Q from the heating unit 19 to the dehydrogenation unit 9. The heating unit 19 is connected to the cleaning unit 15 via a fourth fluid line 20. The heating unit 19 is optional. Particularly when the fuel cell 18 is designed as a high-temperature fuel cell, the waste heat from the high-temperature fuel cell can serve as an additional heating unit, in particular to transfer heat to the dehydrogenation unit 9 and / or other components of the device 5. In any case, a separate heating unit is unnecessary when a high-temperature fuel cell is used.

[0087] A post-treatment unit 21 is also connected to the cleaning unit 15 via a fifth fluid line 22. The power generation unit 17 is fluidly connected to the post-treatment unit via an exhaust line 54. Exhaust gas generated in the power generation unit 17, in particular in the fuel cell 18, can be delivered directly to the post-treatment unit 21 and oxidized there, i.e., converted into heat.

[0088] An electronics unit 23 is electrically connected to the power generation unit 17 by means of a further electrical line 6. The electronics unit 23 comprises a power storage element 24, in particular a battery. The electronics unit 23 comprises a control unit 25. The control unit 25 is in particular in a bidirectional signal connection 26 with the central control unit 3 of the mobile platform 1.

[0089] The drive 2 is electrically connected, in particular electrically, to the power generation unit 17, in particular the fuel cell 18, and / or the electronics unit 23, in particular the power storage element 24, by means of the electrical lines.

[0090] The device 5 has a heat generation unit 27, which, according to the illustrated embodiment, is designed as an electric heater. The heat generation unit 27 is operatively connected to a heat transfer unit 28. The heat transfer unit 28 is designed as a heat transfer circuit, in particular as a closed heat transfer circuit. Thermal oil serves, in particular, as the heat transfer fluid. The heat transfer fluid is heated in the heat generation unit 27, conveyed to or into the dehydrogenation unit 9 by means of the heat transfer unit 28, and there releases heat Q to the dehydrogenation unit 9. The heat flow Q is symbolically represented in Fig. 1. The cooled heat transfer fluid is conveyed back to the heat generation unit 27 in the heat transfer circuit and can be reheated. The heat generation unit 27 and the heat transfer unit 28 form an activation unit 29. The activation unit 29 is a heating unit for heating the dehydrogenation unit 9.

[0091] If the power generation unit 17, in particular the fuel cell 18, is designed as a high-temperature fuel cell, in particular as an SOFC fuel cell, a closed heat circuit 55 can be provided for heat transfer from the SOFC fuel cell 18 to the dehydrogenation unit 9. The closed heat circuit 55 is designed in particular correspondingly and in particular identically to the heat transfer unit 27. In particular, the closed heat circuit 55 comprises a heat transfer fluid, in particular thermal oil, which is handled separately from the other media of the device 5. The closed heat circuit 55 enables direct heat transfer and thus improved heat dissipation from the SOFC fuel cell 18 to the dehydrogenation unit 9, which represents a heat sink.

[0092] In particular, the heat generation unit 27 is designed as a heating element, in particular as an electric heater, which is electrically connected in particular to the electronics unit 23. Electrical power for operating the heat generation unit 27 can be provided by the electronics unit 23, in particular by the power storage element 24.

[0093] In addition to the heating element in the form of the electric heater, the heat generation unit can comprise further components, in particular the aftertreatment unit 21 and / or the power generation unit 17, in particular the fuel cell 18 and / or the heating unit 19.

[0094] The first dehydrogenation reactor 56 is explained in more detail below with reference to Figs. 2 to 6.

[0095] The first dehydrogenation reactor 56 is designed as a tube bundle reactor. The tube bundle reactor has a housing 31 that is essentially hollow-cylindrical with respect to a longitudinal axis 30. A plurality of reaction tubes 32 are arranged in the housing 31, according to the exemplary embodiment 57 shown. The reaction tubes 32 are arranged in a substantially regular, in particular honeycomb-like, grid. In particular, a reaction tube 32 is surrounded by a plurality of reaction tubes 32, whose longitudinal tube axes 33 form the vertices of a regular hexagon in a plane perpendicular to the longitudinal axis 30. It is advantageous if the reaction tubes 32 are arranged as closely as possible to fill the cross-section of the housing 31 of the first dehydrogenation reactor 56.

[0096] The catalyst is arranged in each of the reaction tubes 32.

[0097] The first dehydrogenation reactor 56 has a hydrogen carrier medium inlet chamber 34, into which a hydrogen carrier medium supply line 35 opens. The hydrogen carrier medium supply line 35 is designed as a pipe socket with a molded-on flange, which is fastened and, in particular, welded to an outer cylindrical surface of the housing 31. The hydrogen carrier medium inlet chamber 34 is arranged at a first end 36 of the housing 31. At a second end 37, which is arranged on the housing 31 opposite the first end 36, a hydrogen carrier medium discharge line 38 opens out of the housing 31. The hydrogen carrier medium discharge line 38 is designed as a pipe socket with a molded-on flange and is, in particular, connected to the second fluid line 14. At least partially discharging hydrogen carrier medium and hydrogen gas are discharged via the hydrogen carrier medium discharge line 38.To separate particles, particularly vaporous ones, of the at least partially discharged hydrogen carrier medium from the hydrogen gas stream, an additional separation unit can be arranged, particularly between the first dehydrogenation reactor 56 and the purification unit 15. A hydrogen carrier medium flow direction 39 is defined by the hydrogen carrier medium supply line 35 and the hydrogen carrier medium discharge line 38 and is oriented from right to left according to Fig. 3.

[0098] A holding element 40 is arranged on each end face of the reaction tubes 32. The holding element 40 prevents the catalyst from passing from the reaction tube 32 into the hydrogen carrier medium inlet chamber 34 and / or to the hydrogen carrier medium supply line 35. The holding elements 40 reliably hold the catalyst in the reaction tubes 32. The holding elements 40 are each designed, in particular, as a continuous grid that extends substantially over the entire cross-sectional area of ​​the housing 31. The grid elements have a mesh size that is small enough to retain the catalyst particles and / or large enough to allow the liquid hydrogen carrier medium to pass through. The heat transfer unit 28 is connected to the housing 31 by a heat transfer fluid supply line 41 and a heat transfer fluid discharge line 42.The heat transfer fluid supply line 41 opens into a heat transfer fluid inlet chamber 43, which extends in a plane perpendicular to the longitudinal axis 30 over a cross-sectional area of ​​the housing 31, wherein this cross-sectional area corresponds in particular to the cross-sectional area of ​​the housing 31. In the axial direction relative to the longitudinal axis 30, the heat transfer fluid chamber is separated by two partition walls 44 in the housing 31. Several heat transfer fluid guide lines 45 are connected to the heat transfer fluid chamber 43. Each heat transfer fluid guide line 45 is arranged within a reaction tube 32, in particular concentrically therewith. The connection of the heat transfer fluid guide lines 45 to the heat transfer fluid chamber 43 is effected by means of a, in particular curved, connection section 46, which runs at least in sections transversely to the longitudinal axis 30 of the housing 31 and opens into the heat transfer fluid chamber 43.The connection section 46 is sealed and extends out of the reaction tube 32. The reaction tube 32 is separated from the heat transfer fluid chamber 43. The material flows of the hydrogen carrier medium and the heat transfer fluid are separated from each other.

[0099] The heat transfer fluid flow direction 47 is directed from the heat transfer fluid supply line 41 to the heat transfer fluid discharge line 42, i.e., from left to right as shown in Fig. 3. The heat transfer fluid flow direction 47 is opposite to the hydrogen carrier medium flow direction 39. According to the illustrated embodiment, heat transfer from the heat transfer fluid, in particular thermal oil, to the hydrogen carrier medium occurs in countercurrent. Heat transfer can also occur in cocurrent or crosscurrent.

[0100] The tube bundle reactor is, in particular, set up and operated with the longitudinal axis 30 oriented horizontally. The tube bundle reactor can also be arranged with the longitudinal axis 30 inclined relative to the horizontal, wherein the angle of inclination is, in particular, between 0° and 90°, and the tube bundle reactor can, in particular, also be oriented vertically. The heat transfer fluid supply line 41 and the heat transfer fluid discharge line 42 are, in particular, designed as pipe sockets with a molded-on flange.

[0101] The reaction tubes 32 are designed as double-walled tubes, wherein the hydrogen carrier medium flows along the annular cross-section and the heat transfer fluid flows along the inner tube cross-section, in particular in mutually opposite directions 39, 47.

[0102] The heat transfer unit 28, in particular the heat transfer fluid guide lines 45, are integrated into the dehydrogenation unit 9 and in particular into the first dehydrogenation reactor 56. In particular, a heat transfer fluid guide line 45 is integrated into each reaction tube 32 and is arranged concentrically therein. The heat transfer fluid guide line 45 thus enables heating of the reaction tube 32 from the inside. Heat transfer is thereby improved.

[0103] According to an exemplary embodiment not shown, it is particularly conceivable for the heat generation unit 27 to be arranged directly integrated into the dehydrogenation unit 9, and in particular into the first dehydrogenation reactor 56. A heat transfer unit is unnecessary in this case. An integrated heat generation unit 27 can be implemented, in particular, as an oxidation unit for oxidizing the hydrogen carrier medium and, in particular, for combusting the hydrogen carrier medium.

[0104] The heat transfer fluid guide lines 45 extend axially relative to the longitudinal axis 30 through the holding element 40 attached to the first end face 36 and the adjoining hydrogen carrier medium inlet chamber 34. The heat transfer fluid guide lines 45 are attached to a tube plate 53 oriented transversely, in particular perpendicularly, to the longitudinal axis 30.

[0105] The hydrogen carrier medium inlet chamber 34 is delimited in the axial direction in particular by the holding element 40 and the tube sheet 53. In the axial direction relative to the longitudinal axis 30, a hydrogen vapor chamber 48 is delimited between the partition wall 44 facing away from the second end 37 and the holding element 40 on the hydrogen carrier medium inlet chamber 34. The hydrogen vapor chamber 48 is formed by the spaces remaining between the reaction tubes 32. The hydrogen vapor chamber 48 has a hydrogen vapor supply line 49 and a hydrogen vapor discharge line 50, which, in accordance with the lines described above, are designed as pipe sockets with a molded-on flange. The hydrogen vapor supply line 49 and the hydrogen vapor discharge line 50 define a hydrogen vapor flow direction which, according to Fig. 3, is oriented essentially from left to right.Flow guide elements 51 are arranged in the hydrogen vapor chamber 48, each of which is oriented transversely and in particular perpendicularly to the longitudinal axis 30 and extends over at least 30%, in particular at least 50%, and in particular at least 80% of the cross-sectional area of ​​the housing 31. Adjacent flow guide elements 51 are arranged offset from one another in such a way that hydrogen vapor is guided in a meandering manner through the hydrogen vapor chamber 48 along the hydrogen vapor flow direction. The flow guide elements 51 are arranged in the housing 31 in such a way that a free surface 52 results in a plane perpendicular to the longitudinal axis 30, through which free surface the hydrogen vapor can flow past the flow guide element 51.

[0106] A method for providing electrical energy using a hydrogen carrier medium is explained in more detail below.

[0107] At least partially loaded hydrogen carrier medium is conveyed from the first subchamber 11 of the storage tank 7 into the dehydrogenation unit 9, where it is catalytically dehydrogenated. At least partially discharged hydrogen carrier medium is conveyed back to the second subchamber 12 of the storage tank 7 via the return line 10.

[0108] The hydrogen gas released in the dehydrogenation unit 9 is conveyed to the purification unit 15 and purified there. The impurities separated in the purification unit 15 are conveyed to the aftertreatment unit 21 and, in particular, combusted. The purified hydrogen gas stream is fed to the power generation unit 17, and in particular to the fuel cell 18, where it is converted into electricity. It may be advantageous if at least a partial stream of the hydrogen gas is fed to the heating unit in order to provide a heat flow Q for the dehydrogenation unit 9.

[0109] The electrical current generated in the fuel cell 18 is made available to the drive 2 via electrical lines 6, either directly and / or indirectly via the electronics unit 23. In particular, electrical current can be temporarily stored in the power storage element 24.

[0110] A particularly advantageous mode of operation of the device 1 using the activation unit 29 is one which enables uncomplicated activation, in particular heating, of the dehydration unit 9, particularly when the device 1 was previously in a standby mode, i.e., the dehydration unit 9 was not being operated. For a so-called cold start, electrical current is first provided from the electronics unit 23, in particular from the power storage element 24, in order to operate the heat generation unit 27. In the heat generation unit 27, the heat transfer fluid, i.e., the thermal oil, is heated and pumped by means of a pump (not shown in detail) via the heat transfer fluid supply line 4 into the heat transfer fluid chamber 43 and from there into the individual heat transfer fluid guide lines 45.In addition, electrical power from the electronics unit 23, in particular the power storage element 24, is used to operate pumps to convey the hydrogen carrier medium from the storage container 7 into the dehydrogenation unit 9, in particular into the first dehydrogenation reactor 56. Thus, in the activation mode, only the first dehydrogenation reactor 56 of the dehydrogenation unit 9 is operated.

[0111] As soon as hydrogen gas is released in the first dehydrogenation reactor 56, it can be used in the power generation unit 17 to generate electrical power. Heat is also generated in the power generation unit 17. The power and heat generated in the power generation unit 17 can then be used to carry out and ensure the continued, constant, and especially self-sufficient operation of the dehydrogenation unit 9. Subsequently, additionally provided energy can be used, in particular, to put further dehydrogenation reactors, in particular the second dehydrogenation reactor 57, and / or other system components into operation. In activation mode, the second dehydrogenation reactor 57 is not operated. In activation mode, no dehydrogenation reaction takes place in the second dehydrogenation reactor 57. However, the second dehydrogenation reactor 57 can be preheated in activation mode.

[0112] To initially activate the first dehydrogenation reactor 56, electrical energy from the power storage element 24 can be used to operate the electric heater of the heat generation unit 27. The electric heater serves to heat the first dehydrogenation reactor 56. Additionally, the electrical current from the power storage element 24 can be used to switch and operate other components of the device 5. By activating the first dehydrogenation reactor 56, hydrogen gas can be released there, initially in small quantities.

[0113] The hydrogen gas released in the first dehydrogenation reactor 56 is conveyed to the purification unit 15 and from there proportionally delivered to the power generation unit 17, in particular the fuel cell 18 and / or the heating unit 19, as well as to the aftertreatment unit 21. Electrical power generated in the power generation unit 17 is fed to the electronics unit. Electrical energy can be temporarily stored in the electronics unit 23, in particular in the power storage element 24. However, the electrical energy can also be delivered directly to the heat generation unit 27 in the form of the electrical heater to produce heat, which is delivered to the first dehydrogenation reactor 56 by means of the heat transfer unit 28. In the activation mode, the heat transfer unit 28 is thus supplied with heat, in particular by the heat generation unit, in particular the electrical heater 27 and / or the aftertreatment unit 21.In activation mode, the heat transfer unit 28 can transfer heat to the first dehydrogenation reactor 56 for activation, to the second dehydrogenation reactor 57 for preheating and / or to the power generation unit 17, in particular the fuel cell 18, for warming up.

[0114] During regular operation of the dehydrogenation unit 9, reaction products, in particular from the second dehydrogenation reactor 57 and / or other downstream dehydrogenation reactors, can be fed to the first dehydrogenation reactor 56, in particular its hydrogen vapor chamber 48. These material flows serve in particular for heat recovery in order to heat the reaction tubes 32 on their outer surface. These operating materials thus serve to heat the reaction tubes 32 from the outside. The hydrogen vapor chamber 48 serves in particular as a recuperator, which is arranged in particular as an integrated part of the first dehydrogenation reactor 56.

[0115] During regular operation of the device 5, i.e., in particular, after sufficient energy and heat have been provided by the device 5 itself to operate the second dehydrogenation reactor 57, the activation unit 29 can be deactivated. In particular, the electrical heating of the heat generation unit 27 is no longer operated in order to reduce the overall energy consumption of the device 5. In this operating mode, the heat generation unit 27 is formed by the aftertreatment unit 21 and additionally by the power generation unit 17, in particular the fuel cell 18.

[0116] Due to the supply of the fuel cell 18 with sufficient released hydrogen gas from the dehydrogenation unit 9, waste heat is generated in the power generation unit 17, in particular in the fuel cell 18, which is transferred directly to the heat transfer unit 27. From the heat transfer unit 27, the heat is transferred, in particular directly, to the second dehydrogenation reactor 57. In addition, heat is transferred to the first dehydrogenation reactor 56 from the second dehydrogenation reactor 57 and / or from the heat transfer unit 27.

Claims

Patent claims 1. Device (5) for providing electrical energy by means of a hydrogen carrier medium comprising a. a dehydrogenation unit (9) having a first dehydrogenation reactor (56) for releasing hydrogen gas from the hydrogen carrier medium, b. a power generation unit (17) fluidically connected to the dehydrogenation unit (9) for generating electric current from the released hydrogen gas, c. an electronic unit (23) electrically connected to the power generation unit (17) for storing and / or controlling the generated electric current, d. an activation unit (29) for activating the device (5), wherein the activation unit (29) comprises an energy source (27, 28) for heating the first dehydrogenation reactor (56).

2. Device according to claim 1, characterized in that the heating unit comprises a heat generation unit (27) and / or a heat transfer unit (28).

3. Device according to one of the preceding claims, characterized in that the activation unit (29), in particular the heat generation unit (27) and / or the heat transfer unit (28), is at least partially integrated in the dehydration unit (9), in particular in the first dehydration reactor (56).

4. Device according to one of the preceding claims, characterized in that the activation unit (29) is fluidically connected to the dehydrogenation unit (9), in particular to the first dehydrogenation reactor (56), for the transfer of hydrogen gas.

5. Device according to one of the preceding claims, characterized by a cleaning unit (15) arranged downstream of the dehydration unit (9), which is in particular designed as a pressure swing adsorption apparatus.

6. Device according to one of the preceding claims, characterized by a post-treatment unit (21) for post-treatment of material streams, in particular from the cleaning unit (15).

7. Device according to one of the preceding claims, characterized in that the power generation unit (17) comprises a gas turbine, a hydrogen combustion engine and / or a fuel cell (18), in particular a proton exchange membrane fuel cell, a solid oxide fuel cell or a solid acid fuel cell.

8. Device according to claim 7, characterized in that the power generation unit (17) is coupled to a heat sink in a heat-transferring manner by means of a, in particular closed, heat circuit, wherein the heat sink is in particular the dehydration unit (9).

9. Device according to one of the preceding claims, characterized in that the dehydration unit (9), in particular the first dehydration reactor (56) and / or a second dehydration reactor (57), is designed as a tube bundle reactor with several reaction tubes (32).

10. Device according to one of the preceding claims, characterized by at least one operating unit for generating an operating medium, in particular compressed air, nitrogen and / or cooling water, using heat and / or electric current.

11. Device according to one of the preceding claims, characterized by a control unit (25) for controlled operation of the device (5), wherein the control unit (25) is in particular in signal communication with an external signal transmitter (3) which specifies a current requirement to be provided by the power generation unit (25).

12. Mobile platform (1) with an electric motor drive (2) for generating a driving force and with a device (5) according to one of the preceding claims, which is electrically connected to the drive (2). Method for providing electrical energy using a hydrogen carrier medium comprising the process steps Providing a device (5) comprising a dehydrogenation unit (9) having a first dehydrogenation reactor (56) for releasing hydrogen gas from the hydrogen carrier medium, — a power generation unit (17) fluidically connected to the dehydration unit (9) for generating electricity from the released hydrogen gas, an electronic unit (23) electrically connected to the power generation unit (17) for storing and / or controlling the generated electricity, an activation unit (29) for activating the device (5), wherein the activation unit (29) comprises a power source (27, 28) for heating the first dehydration reactor (56), wherein the device (5) is in a standby mode in which the dehydration unit (9) is inactive, Activating the device (5) by means of the activation unit (29), wherein the activation includes heating the first dehydration reactor (56) by means of the energy source (27, 28). Release of hydrogen gas from the hydrogen carrier medium by means of the first dehydrogenation reactor (56), Generating electricity from the released hydrogen gas using the power generation unit (17), Storing and / or controlling the generated electrical current by means of the electronic unit (23) electrically connected to the power generation unit (17). Method according to claim 13, characterized by operating the device (5) in a regular operating mode in which the first dehydrogenation reactor (56) is operated as the first-stage reactor of the dehydrogenation unit (9) and a second dehydrogenation reactor (57) downstream of the first dehydrogenation reactor (56) is operated as the main reactor for hydrogen release.

15. Method according to claim 13 or 14, characterized by providing electric current, in particular by means of the electronic unit (23), for commissioning the energy source, in particular a heating unit (27, 28) and / or for supplying heat transfer fluid to the dehydration unit (9).

16. A method according to claim 14 or 15, characterized by heat transfer to the first dehydration reactor (56) from a product stream of the second dehydration reactor (57).

17. A method according to any one of claims 14 to 16, characterized by switching the dehydration reactors from an activation mode to the regular operating mode and / or back, in particular automatically, in particular fully automatically.

18. Method according to any one of claims 13 to 17, characterized by operating the device (5) in an idle mode in which the first dehydrogenation reactor (56) releases a reduced amount of hydrogen gas, which is particularly sufficient to generate electricity and / or heat to provide operation of the power generation unit (17) and / or the device (5) in a standby mode.

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