CH704556B1 - Heating. - Google Patents

Abstract

The invention relates to a heat-generating unit (1) or heating with a reactor (2) in which hydrogen peroxide (H 2 O 2) is split by catalytic dissociation into water and oxygen, thereby producing heat. Embodiments relate, inter alia, to: operating the reactor (2) with liquid and vapor phases (41, 42) of the catalyst fluid; Operating the reactor (2) with recirculation means (8, 15; 15 '; 410) for the catalyst fluid (40, 41); an integrated catalyst heat exchanger module (11 '); a preheat exchanger (171) for transferring heat from a residual fluid (170) to the catalyst fluid (40, 41); and combination with a fuel cell or oxygen-hydrogen combustion. Benefits include: exhaust-free heat production and optionally electricity production.

Description

Technical area

The invention relates to the field of heating technology, in particular of building heating or block power plants. It is based on a heat generating unit, a heater and a device according to the preamble of the independent claims.

State of the art

In the invention is based on known heating systems, in which by burning fossil fuels such as oil, gas, wood, pellets or similar. Heat is generated in a combustion chamber. The heat can be used via a heat exchanger to heat heating water that circulates in a closed Heizwasserkreislauf, or hot water, which is fed again and again fresh. The resulting polluting gases include carbon dioxide CO2, carbon monoxide CO, nitrogen oxides NOx, sulfur oxides and other toxic combustion products, as well as particulate matter. Also known are electrically operated heaters, either directly by ohmic resistance (electric heating, electric storage heater) or indirectly by increasing the temperature of ambient heat (heat pump) generate heat for buildings. The direct electric heaters are energetically inefficient. Heat pumps are rather complicated, are in need of maintenance because of their moving parts and are susceptible to faults and have a limited service life.

The known heaters are typically permanently installed in buildings. Also known are electrically heated radiators, which are placed in rooms as needed.

In CH 685 836 A5 a method for generating steam for operating a steam turbine is disclosed. For this purpose, a mixture consisting essentially of hydrogen peroxide (H2O2, also referred to below as WP) is fed to a reactor in which the WP is converted by means of a suitable catalyst to water, oxygen and exothermic heat. The released energy is used to convert the water into heated steam, which is supplied via an outlet opening in the reactor of the steam turbine as a drive medium.

Presentation of the invention

The object of the present invention is to provide an improved heat generating unit and heating and an improved system for heat generation and optional power generation, in which or no environmentally harmful exhaust gases or residues. This object is achieved according to the invention by the subject matters of the independent claims. Further features, in particular in dependent claims, or combinations of features or embodiments are optional and are typically as particular, preferably o.Ä. referred to and are therefore not essential to the invention, but are only to achieve additional benefits or effects.

The invention consists in a heat generating unit suitable for heating, e.g. Home heating, is suitable, wherein the heat generating unit comprises a reactor having a reactor housing in which at least one catalyst body is arranged for the catalytic exothermic conversion of a catalyst fluid, further wherein the catalyst fluid containing a mixture containing hydrogen peroxide (H2O2).

In one embodiment, the heat generating unit has a heat exchanger for heating a heat transfer fluid. The heat transfer fluid can be used to operate the heater and can be in particular heating water and / or service water.

In one embodiment, the catalyst fluid in the heat-generating operation to a liquid phase. In particular, the liquid phase is in thermal contact with the heat exchanger. In a further embodiment, the catalyst body is immersed in the heat generating operation at least partially in one or the liquid phase of the catalyst fluid. In particular, the reactor can be arranged upright. By these measures, the efficiency of the catalytic heat recovery and the heat transfer to the heat transfer fluid can be increased.

In one embodiment, the catalyst fluid in the heat generating operation to a vapor and / or gaseous phase.

In a preferred embodiment, the heat generating unit comprises an integrated catalyst heat exchanger module comprising the catalyst body and the heat exchanger. In particular, the integrated catalyst heat exchanger module can be arranged in the reactor or itself form the reactor.

Other embodiments relate to embodiments of the catalyst, in particular the integrated catalyst heat exchanger module, which further improve the efficiency of heat generation in the catalytic conversion and the heat transfer to the heat transfer fluid.

In one embodiment, the heat generating unit, in particular the reactor, recirculation means for recirculation of the catalyst fluid along the catalyst body. The recirculation improves the wetting of the catalyst body and thereby increases the efficiency of the heat recovery. The recirculating agents may e.g. a circulating pump, a pressure circulation, and / or self-contained, suitable for generating a recirculation flow throughflow channels for the catalyst fluid and in particular for its liquid phase.

In preferred embodiments, the catalyst body is a ceramic body containing Kordierit or consists of cordierite.

In embodiments, the catalyst fluid contains a maximum of 50 wt .-%, preferably at most 35 wt .-%, more preferably at most 25 wt .-%, in particular at most 20 wt .-%, of hydrogen peroxide (H2O2, WP). Alternatively, the catalyst fluid may consist largely of hydrogen peroxide. WP in a lower concentration has the advantage that the catalyst fluid can be stored in environmentally friendly and without special safety measures in tanks. WP in higher concentration has the advantage of higher energy content.

Other embodiments relate to embodiments of the reactor, a preheat exchanger for heat transfer from a residual fluid to the catalyst fluid, and excitation means for removing vapor and / or gaseous bubbles from the surface of the catalyst body, in particular a vibrator or an acoustic source.

The invention also relates to a heater, in particular building heating or heating for generating process heat, with a heat generating unit as described above; and a system comprising such a heat-generating unit in combination with a fuel cell for generating electricity and / or an additional heating, in which or which of the released in the dissociation of hydrogen peroxide (H2O2) on the catalyst body oxygen is reacted with suitably supplied hydrogen (H2) to water. By operating with two reaction media (H2O2, H2), energy efficiency can be further increased in an environmentally friendly manner.

Further embodiments, advantages and applications of the invention will become apparent from the dependent claims, from each claim combination and from the following description and the figures.

Brief description of the drawings

They show schematically <Tb> FIG. 1 <SEP> Embodiments of a Catalyst Heat Generating Unit with Circulating Pump; <Tb> FIG. 2 <SEP> Embodiments of a catalyst heat generation unit with accumulator circulation; <Tb> FIG. 3 <SEP> Embodiments of a Compact Heat Generation Module with Integrated Catalyst Heat Exchanger; <Tb> FIG. 4-6 <SEP> Embodiments of a catalyst heat generation unit with pre-evaporator.

In the figures, the same or functionally identical parts are provided with the same reference numerals.

Ways to carry out the invention

In the description, many exemplary embodiments are given, which are also partially shown in the figures. The embodiments serve to illustrate and are not to be used to limit the interpretation of the claims. For example, features that are shown or described as part of an embodiment should also be usable in other embodiments and thus represent the basis for further embodiments. Such modifications and variations are expressly embodied in the present disclosure. In particular, all features in dependent claims in any combination can be combined.

The invention relates to a heat generating unit 1 for a heater, in particular for a house heating, wherein the heat generating unit 1 comprises a reactor 2 with a reactor housing 3, in which at least one catalyst body 4 for the catalytic exothermic conversion of a catalyst fluid 40, 41 is arranged. The catalytic heating enables environmentally friendly, emission-free heat generation. In the following, exemplary embodiments are given for this purpose.

According to the invention, the catalyst fluid 40, 41 contains a mixture containing hydrogen peroxide (H2O2). In particular, the catalyst body can be a ceramic body 4 which contains cordierite or consists of cordierite. For example, the catalyst body 4 contains compounds and / or combinations of the amount comprising aluminum, silicon, copper, magnesium, titanium, manganese, iron, lanthanum, cerium, praseodymium, neodymium, phosphorus, potassium, calcium, cobalt, zinc, tin, lead, Sulfur, chlorine, nickel, strontium, zirconium, molybdenum, rhodium, silver, potassium permanganate and rare earth elements.

In embodiments, the catalyst fluid contains at most 50 wt .-%, preferably at most 35 wt .-%, more preferably at most 25 wt .-%, in particular at most 20 wt .-%, hydrogen peroxide (H2O2), or the catalyst fluid is largely from hydrogen peroxide. In principle, other catalyst fluids 40, 41 and / or other catalyst materials are possible.

Fig. 1 shows an embodiment of a heat generating unit 1 and in particular a heating module 1 or a heater 1. The heat generating unit 1 has a reactor 2 with a reactor housing 3. At the reactor bottom 3b is an inlet port 30b, e.g. in the form of an inlet valve 30b, for an inlet 5 of catalyst fluid 50, e.g. for a H2O2-containing mixture. At the bottom of the reactor 3b, the catalyst fluid typically collects in the form of a liquid sewer 40. Above the liquid sewer 40, a gas or vapor phase 41 of the catalytic fluid may be present. In the operating state, i. Heat generation state, often also forms a more or less thick foam layer, which floats on the liquid phase 40, depending on the nature of liquid or gaseous and is separated when the catalytic dissociation subsided again in liquid phase 40 and vapor or gas phase 41. At the reactor bottom 3b is also an outlet port 17, e.g. in the form of an outlet valve 17, for a residual fluid 170. An outlet opening 30c, in particular a pressure relief valve 30c, for gaseous products, in particular oxygen (O2), is present on the reactor lid 3c. On the reactor jacket 3a, a flow 9 and a return 10 are provided, via which a heat transfer fluid 90, e.g. Heating water 90 and / or hot water 90, a heat exchanger 11 can be supplied and removed again. The specified openings can also be arranged on other, not shown, parts of the reactor housing 3.

Optionally, a preheat exchanger 171 for heat transfer from the residual fluid 170 to the catalyst fluid 40, 41 present and in particular in the supply line 9 for the catalyst fluid 40, 41 may be arranged. Shown are also a heat storage 18 and other components 19, 20, 26, but not necessarily part of the heat generation module 1 are.

In one embodiment, the reactor housing 3 of the reactor 2 consists of a relative to the catalyst fluid 40, 41, in particular to hydrogen peroxide, inert material. For example, the reactor housing 3 is made of chrome steel, fiber reinforced plastic, PVC, fluorine-containing plastic, in particular Polytrifluoräthylen, polyethylene, polypropylene, or polyethylene terephthalate, or combinations of these materials. The reactor housing 3 may also have an inner coating, preferably of aluminum.

In reactor volume 2, a catalyst body 4, e.g. made of ceramic and especially cordierite. The catalyst body 4 is in the filled operating state of the module 1 in an atmosphere which is at least partially formed by the catalyst fluid 40, 41 and preferably comprises a liquid phase 40 and / or a vapor phase and / or a gaseous phase 41 of the catalyst fluid. In this case, a foam phase 40, 41 can be regarded as a combination of a liquid phase 40 with a gaseous phase 41. The catalytic conversion of hydrogen peroxide H2O2 in the catalyst fluid 40, 41 produces water H2O and oxygen O2, as described in the cited patent specification CH 685 836 A5, which is hereby included in the description with its entire disclosure content. The residual water 170, which is composed of the catalytically split WP and the water mixed in the supplied catalyst fluid 50, can be removed from the reactor vessel 2 at suitable times, in particular after conversion of the hydrogen peroxide as completely as possible via the outlet opening 30b. Likewise, at suitable times, in particular when a predeterminable overpressure is exceeded, the catalytically produced oxygen 60 can be discharged through the outlet opening 30c.

In one embodiment, the catalyst body 4 has a tubular structure and / or honeycomb structure; and / or the catalyst body 4 has an elongated, in particular cylindrical or planar shape, and can be flowed through along its longitudinal axis 4a.

In one embodiment, the catalyst body 4 is arranged upright, wherein substantially vertically oriented flow channels 410 for a vertically movable, in particular vertically rising (Fig. 1, 2, 4, 5) or vertically sinking (Fig. 6), catalyst fluid flow 400th available. Also, the reactor 2 may be arranged standing. Standing arrangement means that a longitudinal axis 2a of the reactor 2 or a longitudinal axis 4a of the catalyst body 4 is vertical, i. essentially parallel to gravity, oriented.

Alternatively, the catalyst body 4 lying, i. horizontal or perpendicular to gravity, to be arranged in order to achieve a long residence time of the catalyst fluid 40, 41 and thus the most complete dissociation of hydrogen peroxide.

In one embodiment, the catalyst body 4 is immersed in the heat generating operation at least partially in the liquid phase 40 of the catalyst fluid in order to achieve efficient wetting of the catalyst body 4. In another embodiment, the heat exchanger 11 is immersed in the liquid phase 40 so that the liquid phase 40 is in close thermal contact with the heat exchanger 11, e.g. by heat convection, stands and a particularly good heat transfer takes place.

In an embodiment also shown in Fig. 1, the reactor 3, a bypass 11 with level sensors 13 for level control in particular the liquid phase 40 of the catalyst fluid 40, 41 on. In addition, the reactor 2 may have a connection 14 for fittings, in particular for at least one temperature sensor 32 and / or at least one pressure sensor 33, for regulating the heat generation.

Fig. 1 also shows an embodiment in which in the stationary reactor 2 at least two superimposed catalyst body 4 are present, which have a variable distance d2 for self-regulation of heat production, which in particular by means of a resilient mounting 21, e.g. in the vertical or longitudinal direction and / or in the horizontal or lateral direction, at least one of the catalyst body 4 happens. In addition, the distance d2 between catalyst bodies 4 and / or a distance d1 between the reactor bottom 3b and the lowermost catalyst body 4 can be selected within a predeterminable range, in particular between 10 mm and 50 mm.

In a further embodiment, the reactor 2 comprises excitation means 21, 22 for removing vapor and / or gaseous bubbles from the surface of the catalyst body 4. In particular, the excitation means may comprise a vibrator 21, in particular in the vertical or longitudinal direction and / or in the horizontal or lateral direction, for the catalyst body 4 and / or an acoustic source 22 for the acoustic excitation of the catalyst fluid 40, 41, in particular with ultrasound. The vibrator 21 has, in contrast to the resilient mounting 21, an active drive, e.g. with an eccentric or similar, on.

Fig. 1 also shows an important embodiment in which the heat generating unit 1, in particular the reactor 2, comprises recirculation means 8, 15 for recirculating (i.e., repeatedly passing) the catalyst fluid 40, 41 along the catalyst body 4. In particular, the recirculation means comprise a circulating pump 8, which circulates the liquid phase 40 separated in a degassing tank 15. In particular, the circulating pump 8 temporarily or continuously transports the liquid phase 40 in the form of a recirculation flow 70 via return flow pipe 7 in the stationary reactor 2 from the reactor bottom 3b in the direction of the reactor cover 3c. For this purpose, an inlet opening 31b, in particular with an outlet valve 15a, and on the other hand, on the reactor lid 3c an inlet opening 31c for the recirculation flow 70 of the catalyst fluid 4 may be arranged in the reactor 2 on the one hand on the reactor bottom 3b. To regulate the liquid level in the degassing tank 15 and the degassing tank 15 may be equipped with level sensors 13.

Fig. 2 shows an embodiment in which the recirculation means instead of circulation pump 8 and degassing tank 15 comprise a pressure storage tank 15, which by means of the vapor and / or gaseous phase 41, the catalyst fluid 40, 41 circulates. To regulate the accumulator circulation, the pressure vessel 15 may have level sensors 13 for determining the liquid level in the pressure vessel 15 and a first valve 15a (lower valve, here inlet valve) and a second valve 15b (upper valve, here outlet valve) for the catalyst fluid flow 70 to be circulated. The control can be carried out so that first with closed valves 15a, 15b in the reactor 2, a pressure build-up, then with open inlet valve 15a and closed outlet valve 15b of the pressure vessel 15 with catalyst fluid 40, 41 fills and in the degassing tank 15, a separation of the vapor - Or gaseous phase 41 is carried out by the liquid phase 40, then with closed valves 15a, 15b and open outlet valve 30c, a pressure reduction in the reactor 2 is carried out, and then with a closed inlet valve 15a and 15b open exhaust valve a strong, pressure-driven fluid flow 70, preferably predominantly the liquid phase 40, takes place via return flow pipe 7 in the upper part of the reactor 2.

If the tank 15 is filled with liquid 40, a reverse circulation or purging in the opposite direction of flow is possible. In this case, pressure from the reactor 2 via the second valve 15b (upper valve) is passed into the pressure storage tank 15, the reactor 2 pressure relief via outlet port 30c and then the accumulator tank 15 via the first valve 15a (lower valve) emptied while the catalyst fluid flow and the phases 40, 41 circulated in the reactor 2. Depending on the design, the accumulator circulation requires a required minimum differential pressure. In experimental reactor 2 it could be shown that a differential pressure of e.g. 1.5 bar or higher is sufficient for a good pressure circulation. An advantage of accumulator recirculation is that there is no need for a circulation pump for the corrosive HP.

According to one embodiment, the reactor housing 3 may be a pressure vessel 3 for pressure operation, which for operating pressures e.g. less than 20 bar, in particular less than 10 bar, preferably less than 5 bar, is designed. In such pressure operation, the reactor 2 may be discharged at high speed from the residual fluid 170. As a result, the temperature drop occurring during the emptying can be kept low. For a low pressure operation, e.g. between 2.5 bar and 4 bar, or a (largely) depressurized operation, e.g. below 1.5 bar, the reactor 2 must be vented more often. Optionally, if required, the emptying of the reactor 2 can be assisted by the residual fluid 170 with a pump (not shown). A low pressure operation has the advantage that the reactor vessel 3 is only for small maximum pressures, e.g. for a maximum of 5-6 bar or a maximum of 3 bar, must be designed. This results in significant design simplifications, pressure tests are easier or omitted and the reliability is increased. Also, for low pressure operation, because of the simultaneous heat and oxygen production in the catalytic dissociation of WP, the temperature and pressure in reactor 2 can be controlled relatively independently, i. The heat production runs efficiently even at low pressure operation.

Fig. 3 shows an embodiment of an integrated catalyst heat exchanger module 11 for the previously discussed heat generating unit 1. The integrated catalyst heat exchanger module 11 comprises the catalyst body 4 and a heat exchanger 11 for heating the heat transfer fluid 9. In particular the integrated catalyst heat exchanger module 11 may be arranged in the reactor 2, or it may itself constitute the reactor 2 or its essential components. As illustrated in FIG. 3, the integrated module 3 may have an inlet connection 5 for flowable catalyst fluid 50, an outlet connection 6 for gas to be discharged 60, especially oxygen, as well as a flow 9 and return 10 for the heat transfer fluid 90 have. Also, a heat storage 18 may be present.

According to FIG. 3, the integrated catalyst heat exchanger module 11 may have first throughflow channels 410 for flowing through the catalyst fluid 40, 41 and second throughflow channels 411 for flowing through the heat carrier fluid 90. Various variants are possible, some of which are mentioned here: the first and second flow channels 410, 411 may e.g. be arranged in different levels, in particular in alternating order; and or the first and second flow channels 410, 411 may be substantially elongated and oriented at a predeterminable angle, in particular at 90 ° or 180 °, relative to one another; and or On the integrated catalyst heat exchanger module 11, a distribution volume 410a may be present on first surfaces and a collection volume 410b for flowing through the first flow channels 410 with the catalyst fluid 40, 41 on second surfaces, and a distribution volume 411a on fourth surfaces and on fourth surfaces a collecting volume 411 b for flowing through the second flow channels 411 with the heat transfer fluid 90 may be present.

In other embodiments, not shown, the first and second flow passages may be arranged in concentric ring cylinders, in particular in alternating sequence, and be flowed through in the DC direction or countercurrent direction. The respective first flow passages can also be serially connected one behind the other in a meandering or otherwise manner, or be annular, helical or self-contained, as can the respective second flow passages.

The first flow channels 410 comprise material of the catalyst body 4 or consist thereof. The second flow channels 411 may comprise or consist of thermally conductive material, in particular copper or aluminum.

FIGS. 4 to 6 show further exemplary embodiments. There may or may also be an atomizer 230 for atomization and / or an evaporator 23, 24 for pre-evaporation, in particular for cold evaporation of portions of the liquid phase 40 of the catalyst fluid 40, 41 present and in particular in the reactor 2. For example, the evaporator may be an acoustic evaporator 23, in particular ultrasonic evaporator 23, and / or a capillary evaporator 24.

Fig. 4 shows an embodiment in which, for example, a nebulizer 230, and / or an ultrasonic evaporator 23 and / or a capillary evaporator 24 are present and the catalyst fluid interacts only as a vapor phase or gas phase 41 with the catalyst body 4. As a result, extensive WP dissociation can be achieved even on relatively short flow-through paths or in relatively short flow-through channels 410, and recirculation means 8, 15; 15 renounce. Fig. 5 shows the same arrangement, but with a bypass 12 with level sensors 13, as already known from Fig. 1, for liquid level measurement. By means of the apparatus 12, 13, the liquid level can be measured and a control of the injection or the atomizer 230 and / or the at least one evaporator 23, 24 take place.

Fig. 6 shows an embodiment in which the reactor 2 in the "drip" or "gravity mode", i. E. is operated with the flow direction of the catalyst fluid 40, 41 vertically downward or parallel to gravity. For this purpose, the previously discussed inlet opening 30b for the catalyst fluid 40, 41 are arranged on the reactor cover 3c. In addition, an atomizer 230 and / or at least one evaporator 23, 24 (eg ultrasonic evaporator 23 or capillary or evaporation evaporator) are present (as in Fig. 4, 5), but this time in the upper part of the reactor 2. In addition, a simplified circulation with Circulation pump 8 (as in Fig. 1), but without Entgasungstank, and a bypass 12 with level sensors 13 for liquid level measurement available. This embodiment is characterized by highly efficient operation with predominant gas or vapor phase 41 of the catalyst fluid in combination with efficiency enhancing liquid phase recirculation 70.

The invention is also a heating, in particular building heating, which comprises the previously described heat generating unit 1 according to one of the disclosed variants or combinations thereof.

In particular, the heater may have an automatic control 25, with which a filling 50 of the reactor 2 with the catalyst fluid 40, 41, an emptying of the reactor 2 of residual fluid 170, and, if present, a recirculation by controlling the recirculation means 8, 15; 15 is regulated.

In embodiments, the heater may e.g. a storage tank for the catalyst fluid 40, 41 and a heat radiator have (not shown), and / or a heat exchanger 11, 11 for service water and / or heating water and a heat storage 18, in particular with a hot water solar or auxiliary electric heating, have, and / or be stationary or be a non-stationary heating module; and or have an automatic control 25; In particular, the controller 25 may include an inlet valve 30b for the catalyst fluid 40, 41 and / or an outlet valve 30c for gaseous products such as e.g. Regulate oxygen (O2) and / or an outlet valve 17 for a residual fluid 170.

In one embodiment, the heater for a low-temperature operation, in particular below 100 ° C, be designed for heating buildings. Alternatively, the heater for a high-temperature operation, in particular above 100 ° C, be designed to generate process heat.

The invention is also, as shown in dashed lines in Figures 1 - 6 and disclosed as optional, a system comprising a heat generating unit 1 for the catalytic dissociation of hydrogen peroxide in combination with an additional module 20, 26, in which in the dissociation the hydrogen peroxide (H2O2) on the catalyst body 4 liberated oxygen (O2) is used to generate electrical energy and / or additional heat energy. In one exemplary embodiment, an oxygen storage tank 19 can be arranged between the heat generation unit 1 and the additional module 20, 26, and / or means for supplying a reactant, in particular hydrogen (H 2), can be present. The additional module is preferably a fuel cell 20, in which the oxygen (O 2) with suitably supplied hydrogen (H 2) can be converted into water and electricity in a silent combustion, or it is an additional heater 26, in which the oxygen (O2) with suitably supplied hydrogen (H2) in an exothermic combustion to water and heat energy can be implemented. By operating with two fuels, especially hydrogen peroxide and hydrogen, additional heat and power can be produced as needed.

The disclosed heat generating unit 1 or heating or the disclosed system are particularly suitable for heating buildings that are well insulated to modern standards. When converting from conventional firing media, especially oil, an existing oil tank can e.g. be converted by internal coating with suitable plastic films to a WP tank. The WP tank may generally consist of the same non-corrosive materials as the reactor housing 3 (as previously disclosed).

LIST OF REFERENCE NUMBERS

[0052] <tb> 1 <SEP> Heating, heating module, heat generating unit <Tb> 2 <September> reactor <tb> 2a <SEP> Longitudinal axis of the reactor <tb> 3 <SEP> Reactor housing, pressure housing, thermally insulated housing <Tb> 3 <September> reactor shell <Tb> 3b <September> reactor bottom <Tb> 3c <September> reactor cover <tb> 30b <SEP> Inlet opening for catalyst fluid (e.g., H2O2-containing mixture), inlet valve <tb> 30c <SEP> Gaseous product discharge port (e.g., oxygen (O2)), relief valve <tb> 31b <SEP> Recirculation flow outlet port (catalyst fluid, e.g., H2O2-containing mixture), exhaust valve <tb> 31c <SEP> Recirculation Flow Inlet Portion (Catalyst fluid, e.g., H2O2-containing mixture) <Tb> 32 <September> Temperature Sensor <Tb> 33 <September> Pressure Sensor <tb> 4 <SEP> Catalyst, ceramic body, cordierite body <tb> 4a <SEP> Longitudinal axis of the catalyst <tb> 40 <SEP> catalyst fluid, catalyst fluid <tb> 41 <SEP> catalyst fluid, catalyst vapor, catalyst gas <Tb> 400 <September> catalyst fluid flow <tb> 410 <SEP> first flow channels (for catalyst fluid) <tb> 410a <SEP> first distribution volume, first collection volume <tb> 411 <SEP> second flow channels (for heat transfer fluid) <tb> 411a <SEP> second distribution volume, second collection volume <tb> 4a <SEP> Longitudinal axis of the catalyst body <tb> 5 <SEP> Feed for catalyst fluid <Tb> 50 <September> Flow <tb> 6 <SEP> Gaseous product discharge pipe (e.g., oxygen (O 2) vapor mixture) <Tb> 60 <September> gas flow <tb> 7 <SEP> Return pipe, pipe <tb> 70 <SEP> recirculation flow (catalyst fluid, e.g., H2O2-containing mixture) <Tb> 8 <September> Circulation <tb> 9 <SEP> Flow for heat transfer fluid, service water (service water, heating water) <tb> 90 <SEP> Heat transfer fluid, working water flow <tb> 10 <SEP> Return for heat transfer fluid, service water (service water, heating water) <Tb> 11 <September> Heat Exchanger <tb> 11 <SEP> integrated catalyst heat exchanger <tb> 12 <SEP> Bypass for Level Control for Catalyst Fluid (e.g., H2O2-Containing Mixture) <tb> 13 <SEP> Level Probes (for Catalyst Fluid Level) <tb> 14 <SEP> Connection for fittings (e.g., pressure sensor, temperature sensors) <Tb> 15 <September> degassing tank <tb> 15 <SEP> Pressure vessel, accumulator tank <Tb> 150 <September> accumulator flow <Tb> 151 <September> pressure feed flow <tb> 15a, 15b <SEP> valves <tb> 16 <SEP> Accumulator line, line <tb> 17 <SEP> outlet port, exhaust valve, residual fluid outlet, (residual) water outlet, <tb> 170 <SEP> residual fluid, (residual) water flow <tb> 171 <SEP> Preheat exchanger, preheater for catalyst fluid <tb> 18 <SEP> Heat storage, hot water storage tank <Tb> 19 <September> oxygen storage <Tb> 20 <September> Fuel Cell <tb> 21 <SEP> resilient storage <tb> 21 <SEP> Stimulant, vibrator <tb> 22 <SEP> Stimulus, acoustic source <tb> 23 <SEP> Evaporator, ultrasonic evaporator <Tb> 230 <September> nebulizer <tb> 24 <SEP> Evaporator, capillary evaporator <tb> 25 <SEP> Heating control, reactor control <tb> 26 <SEP> Additional heating, afterburner with pure oxygen <tb> d1 <SEP> Distance between reactor bottom and ceramic body <tb> d2 <SEP> Distance between adjacent ceramic bodies <tb> WP <SEP> Hydrogen peroxide, H2O2

Claims (35)

1. Heat generating unit (1) for a heater, in particular for a house heating, characterized in that the heat generating unit (1) comprises a reactor (2) with a reactor housing (3) in which at least one catalyst body (4) for the catalytic exothermic transformation of a Catalyst fluid (40, 41) is arranged, and that the catalyst fluid (40, 41) contains a mixture containing hydrogen peroxide (H2O2). 2. Heat generating unit (1) according to claim 1, characterized in that the heat generating unit (1) has a heat exchanger (11, 11) for heating a heat transfer fluid (90). 3. Heat generating unit (1) according to one of the preceding claims, characterized in that the catalyst fluid in the heat generating operation has a liquid phase (40). 4. Heat generating unit (1) according to claim 3, characterized in that the catalyst body (4) is immersed in the heat generating operation at least partially in the liquid phase (40) of the catalyst fluid. 5. Heat generating unit (1) according to any one of the preceding claims, characterized in that the catalyst fluid in the heat generating operation has a vapor phase (41). 6. Heat generating unit (1) according to one of the preceding claims, characterized in that <tb> a) <SEP> the catalyst body (4) has a tubular structure or honeycomb structure, and / or b) <SEP> of the catalyst body (4) has an elongated, in particular cylindrical, shape and can be flowed through along its longitudinal axis (4a), in particular that the longitudinal axis (4a) is vertically aligned in the stationary reactor (2). 7. Heat generating unit (1) according to claim 2, characterized in that the heat generating unit (1) comprises an integrated catalyst heat exchanger module (11) comprising the catalyst body (4) and the heat exchanger (11), in particular that the integrated Catalyst heat exchanger module (11) in the reactor (2) is arranged or forms the reactor (2). 8. Heat generating unit (1) according to claim 7, characterized in that the integrated catalyst heat exchanger module (11) has first flow passages (410) for flowing through the catalyst fluid (40, 41) and second flow passages (411) for flowing through the heat transfer fluid ( 90). 9. Heat generating unit (1) according to claim 8, characterized in that a) <SEP> the first and second flow passages (410, 411) are elongate, in different parallel planes, in particular in planes with alternating order of the first and second flow passages (410, 411) are arranged and at an angle are oriented relative to each other, and / or <b> <SEP> on the integrated catalyst heat exchanger module (11) at first surfaces a distribution volume (410a) and at second surfaces a collecting volume (410b) for flowing through the first flow channels (410) with the catalyst fluid (40, 41) are present, and that on third surfaces a distribution volume (411a) and on fourth surfaces a collecting volume (411b) for the passage of the second flow channels (411) with the heat transfer fluid (90) are present. 10. Heat generating unit (1) according to claim 8, characterized in that the first and second flow passages are arranged in concentric annular cylinders, in particular in an alternating sequence, and can be flowed through in the DC or countercurrent direction. 11. Heat generating unit (1) according to any one of claims 9 to 10, characterized in that the first flow channels (410) material of the catalyst body (4) or consist thereof, and that the second flow channels (411) thermally conductive material, in particular copper or aluminum , exhibit or consist of. 12. Heat generating unit (1) according to claim 3, characterized in that an evaporator (23, 24) for pre-evaporation, in particular for cold evaporation of portions of the liquid phase (40) of the catalyst fluid (40) present, in particular in the reactor (2) , is. 13. Heat generating unit (1) according to one of the preceding claims, characterized in that the heat generating unit (1), in particular the reactor (2), recirculation means (8, 15; 15; 410) for recirculation of the catalyst fluid (40, 41) along of the catalyst body (4). 14. Heat generating unit (1) according to claim 13, characterized in that the recirculation means comprise a circulating pump (8), which circulates the liquid phase (40), in particular that the circulation pump (8) temporarily or continuously the liquid phase (40) in standing Reactor (2) from the reactor bottom (3b) in the direction of the reactor cover (3c) transported. 15. Heat generating unit (1) according to any one of claims 13 to 14, characterized in that the recirculation means comprise a pressure accumulator (15), which circulates the catalyst fluid (40, 41) by means of the vapor phase (41). 16 heat generating unit (1) according to any one of the preceding claims, characterized in that in the stationary reactor (2) at least two superimposed catalyst body (4) are provided, for self-regulation of heat production, a variable distance (d2), in particular by means of resilient mounting ( 21) at least one of the catalyst body (4). 17, heat generating unit (1) according to any one of the preceding claims, characterized in that the catalyst body is a ceramic body (4) containing Kordierit or consists of Kordierite. 18. Heat generating unit (1) according to claim 17, characterized in that the catalyst body (4) compounds and / or combinations of the amount comprising aluminum, silicon, copper, magnesium, titanium, manganese, iron, lanthanum, cerium, praseodymium, neodymium, Phosphorus, potassium, calcium, cobalt, zinc, tin, lead, sulfur, chlorine, nickel, strontium, zirconium, molybdenum, rhodium, silver, potassium permanganate and rare earth elements. 19. Heat generating unit (1) according to one of the preceding claims, characterized in that the catalyst fluid (40, 41) a maximum of 50 wt .-%, preferably at most 35 wt .-%, more preferably at most 25 wt .-%, in particular at most 20 Wt .-%, hydrogen peroxide (H2O2), or that the catalyst fluid (40, 41) consists largely of hydrogen peroxide. 20. Heat generating unit (1) according to claim 3, characterized in that a) the reactor (3) has a bypass (11) with level sensors (13) for level control of the liquid phase (40) of the catalyst fluid (40, 41), and / or <b> the reactor (2) has at least one temperature sensor (32) and / or at least one pressure sensor (33) for regulating the heat generation. 21. Heat generating unit (1) according to one of the preceding claims, characterized in that a) <SEP> the reactor (2) has a pressure-resistant reactor housing (3), and / or <b> b) <SEP> the reactor (2) has a thermally insulated reactor housing (3). 22. Heat generating unit (1) according to one of the preceding claims, characterized in that a) <SEP> the reactor housing (3) has an inlet (30b) for the catalyst fluid (40, 41) and an outlet (17) for a residual fluid (170), and / or <b> <b> <SEP> the reactor housing (3) has an outlet (30c), in particular a pressure relief valve (30c), for gaseous products, in particular oxygen (O2). 23. Heat generation unit (1) according to one of the preceding claims, characterized in that a preheat exchanger (171) for heat transfer from a residual fluid (170) to the catalyst fluid (40, 41) and in particular in a feed line (9) for the catalyst fluid ( 40, 41) is arranged. 24. Heat generating unit (1) according to one of the preceding claims, characterized in that the reactor (2) comprises excitation means (21, 22) for removing vaporous bubbles from the surface of the catalyst body (4), in particular that the excitation means comprises a vibrator (21 ) For the catalyst body (4) and / or an acoustic source (22) for the acoustic excitation of the catalyst fluid (40, 41), in particular with ultrasound. 25. Heat generating unit (1) according to claim 3, characterized in that the heat exchanger (11, 11) is immersed in the liquid phase (40). 26. Heat generating unit (1) according to claim 8, characterized in that the first and second flow passages (410, 411) are elongated, in different parallel planes, in particular in planes with alternating sequence of the first and second flow passages (410, 411), are arranged and oriented at 90 ° or 180 ° relative to each other. 27, heating, in particular building heating, characterized by a heat generating unit (1) according to one of the preceding claims. 28. Heating according to claim 27, characterized in that a) <SEP> the heater has a storage tank for the catalyst fluid (40, 41) and a heat radiator, and / or b) <SEP> the heater has a heat exchanger (11, 11) for service water and / or heating water and a heat accumulator (18), in particular with a hot water solar or electric auxiliary heater. 29. Heater according to claim 27 or 28, characterized in that the heater is installed stationary or is a non-stationary heating module. 30. Heating according to one of claims 27 to 29, characterized in that the heater has an automatic control (25) having an inlet valve (30b) for the catalyst fluid (40, 41) and an outlet valve (17) for a residual fluid (170 ), in particular that the control (25) additionally controls an outlet valve (30c) for gaseous products (O2). 31. Heater according to one of claims 27 to 30, characterized in that <a) <SEP> the heater is designed for low-temperature operation, in particular below 100 ° C, for heating buildings, or <b> <b> <SEP> the heater is designed for high-temperature operation, in particular above 100 ° C., for generating process heat. 32. Device, characterized by a heat generating unit (1) according to claim 1, in combination with an additional module (20, 26), in which in the dissociation of the hydrogen peroxide (H2O2) on the catalyst body (4) liberated oxygen (O2) for generating electrical energy and / or used for additional heat generation. 33. Apparatus according to claim 32, characterized in that the heat generating unit (1) according to one of claims 17 to 19 is formed. 34. Device according to one of claims 32 to 33, characterized in that between the heat generating unit (1) and the additional module (20, 26) an oxygen storage tank (19) is arranged, and / or that means for supplying a reactant, in particular hydrogen (H2), are present. 35. Device according to one of claims 32 to 34, characterized in that the additional module is a fuel cell (20) or an additional heater (26), in which the oxygen (O2) is reacted with suitably supplied hydrogen (H2) to water.