• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Moving bed hydride heat pumps and pressure pumps are described in which a hydride-forming material is transported between two or more reactor vessels (21,23). Each vessel can be maintained at a predetermined temperature, and thus, the hydride-forming material may be heated or cooled by moving It into an appropriately heated or cooled reactor vessel (21,23). In this way thermal cycling of reactor vessels is reduced or eliminated. Both continuously operating and moving batch hydride pumping systems are disclosed.
    公开号:SU1097871A1
    申请号:SU792790595
    申请日:1979-07-12
    公开日:1984-06-15
    发明作者:Хилл Баумэн Уолкер；Эллиот Сайрович Брюс
    申请人:Стандарт Ойл Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to heat and injection pump installations in which the hydro-forming material is subjected to heat circulation, namely to hydride-transferring devices, in which the hydride-forming material periodically moves between a high pressure medium and a low pressure medium.
    Known hydride injection-heat pump containing reactors filled with hydride-forming material, equipped with its own heating and cooling elements and branch pipes for supplying and discharging hydride 1.
    A disadvantage of the known pump is the relatively low efficiency, since its reactors and the hydrides contained in them undergo thermal cycling together. Thermal cycling of the main structural elements (periodic heating of the thermal mass of the reactors) requires energy. This energy is only partially recovered (minus the heat loss to the environment) when the temperature of the reactors changes periodically, which leads to a decrease in the thermodynamic efficiency of the pump.
    The purpose of the invention is to increase efficiency.
    The goal is achieved by the fact that in a hydride injection-heat pump containing high and low pressure reactors filled with hydride forming material, equipped with heating cooling elements and hydride inlet and outlet nozzles, the reactors are interconnected by supply lines of hydrogenated and dehydrogenated material having thermal contact with each other and equipped with devices for transferring the hydrogenated and dehydrated material from the low-pressure reactor to the reactor second pressure in the opposite direction.
    Moreover, the low pressure reactor is located above the high pressure reactor, and the devices for moving the hydrogenated and dehydrated material are made in the form of throttles and an additional heater, installed respectively on the supply lines of the hydrogenated and dehydrated material.
    In addition, devices for the hydrogenated and dehydrated material are made in the form of lock bins with inlet and outlet connections connected via valves to the pipelines for supplying the hydrogenated and dehydrated material.
    FIG. Figure 1 shows typical pressure isotherms — composition for an idealized hydride forming material; in fig. 2 shows the design of an injection heat pump for a moving hydride; in fig. 3 illustrates another embodiment of a pump design for a motive hydride; in fig. 4 shows a third variant of a pump for a moving hydride.
    FIG. 5 and 6 depict idealized pressure-composition curves for the pumping cycles shown in FIG. 2
    Hydro-forming materials used in the invention are capable of capturing and then releasing large quantities of hydrogen, corresponding to the temperature and pressure of hydrogen. The term "hydrogen" means all hydrogen isotopes, including deuterium and tritium.
    Typically, each hydride former has an equilibrium temperature, which is a function of hydrogen pressure.
    When the hydride former is heated to a temperature above the equilibrium temperature and an additional heat supply occurs, the hydride begins to decompose, releasing the previously absorbed hydrogen. Conversely, the hydraulic generator will absorb hydrogen when its temperature becomes below the equilibrium temperature, and further heat removal occurs. Thus, by regulating the temperature and the partial pressure of hydrogen on the hydride-forming material, as well as supplying or removing heat from it, the content of hydrogen accumulated in the hydride can be changed. Of greatest interest in this case are those materials that are exothermic hydrogen scavengers. For these, materials are characterized by the release of large amounts of heat when
    by absorbing hydrogen.
    Most of the preferred hydride forming materials are either metal alloys or pure metals that are capable of storing large amounts of hydrogen in a metal lattice.
    0 The amount of hydrogen accumulated in the lattice can be expressed as the atomic ratio H / hn, where H is the number of hydrogen atoms and w is the number of metal atoms. A useful characteristic of many hydride formers, including many metal hydride formers, is that for a given equilibrium temperature, the equilibrium pressure will be approximately constant for a wide range of hydrogen capacity of the hydroformer during
    Q cycle of hydrogenation or dehydration.  From the point of view of the atomic ratio, this means that for a given temperature these materials are essentially isobaric in a wide range of N / T.  Alloys, mixtures and intermetallic compounds of nickel-magnesium, lanthanum-nickel, calcium-nickel, iron-titanium-nickel, titanium-nickel, niobium, scandium, vanadium, etc can be used as hydride formers. P.  In addition, hydrocarbon compounds with carbon-to-carbon unsaturated bonds can be used, which can receive and release hydrogen under appropriate conditions.  FIG.  Figure 1 shows idealized isotherms for a preferred hydride forming agent suitable for - use.  These materials have isobaric equilibrium zones in which for a given equilibrium temperature the equilibrium pressure is essentially constant over a wide range of hydrogen concentrations.  It should be borne in mind that this is the partial pressure of hydrogen, and not the total pressure, which is shown in the graphs (Fig.  one).  Further, if there is no additional explanation, then we are talking about the partial pressure of hydrogen.  The materials that are most suitable for use have plateau zones that are essentially isobaric for a H / W range of about 0.10 or greater.  Such materials are able to absorb or desorb large amounts of hydrogen at fixed temperature and pressure by adjusting the flow of heat and hydrogen near the material.  The equilibrium temperature for a given pressure will not be the same for all hydride-forming materials.  On the other hand, different hydride forming materials have different equilibrium temperatures for a given pressure, as a result of which two or more hydride forming materials can be used in a combination of heat transfer circuits.  For hydride formers, higher equilibrium temperatures are mainly associated with higher hydrogen pressures.  The hydride forming materials can be used to create both heat pumps and injection pumps using hydride-dehydride cycles.  Moreover, the hydride-forming materials themselves move from one core to another, thereby reducing the thermal cycling of the reactor tanks.  Hydride pumps, in which the hydride-forming material moves from one core to another, are called in the further hydride pumps of the moving bed.  The main hydrogenation / dehydrogenation cycles using moving layers of the hydride forming material can operate as pressure pumps as well as heat pumps.  Schematically shows the injection pump of the moving hydride forming material.  Many of the hydride-forming materials are crushed spontaneously into a powder after repeated thermal cycling.  The size of the individual particle powder depends mainly on the mechanical properties of the hydride forming agent, which is cycled in an environment rich in hydrogen.  Some of the hydride-forming metals may give spontaneous sintering, and the average particle size of such materials may depend on the dynamic balance between competing particle growth processes (sintering or agglomeration or other similar processes) and particle destruction (crushing).  For many of these materials, the average particle diameter ranges from one to fifty microns.  In pseudo-liquid. In the flow medium, the driving medium is used to transfer solid particles in the direction of flow of the fluid (medium).  The velocity of the fluid, which is necessary to dilute the drip of known density and size, can be determined on the basis of standard engineering principles.  The presence of small particles gives a number of advantages.  The rate of heat transfer is usually greater for smaller particles, and the speed of the liquid required to liquefy the powder with smaller particles will be lower.  However, on the other hand, the interparticle bond and the gas-solid interface can present significant difficulties when the particle size decreases.  The preferred particle sizes and speed of the dilution fluid will vary depending on the properties of the hydride forming material used.  By the term "pseudo-liquid and" pseudo-liquid layer, it is meant here a wide variety of transportation methods by which solids are captured by the flowing liquid.  The term is to be understood in such a way that it includes methods of transportation that, in addition to the moving fluid, means are used for the transfer. the placement or dispersion of solid particles, as well as transport methods in which the motive fluid separates and transports the particles itself.  For example, in combination with a moving fluid, laptops, acoustics or electromechanical means can be used to produce a pseudo-liquid flow.  There is a large amount of liquids to liquefy the hydride formers.  However, the main characteristics that should be paid attention to when choosing a liquid are the high rate of transfer of heat and hydrogen, as well as the fact that it does not impair the hydride-forming ability of the hydride-forming agent.  The preferred fluid is hydrogen, which easily accumulates in the hydride system, and is characterized by a high heat transfer rate and has a minimal toxic effect on the hydride former.  Pressure pump (FIG.  2) contains a high pressure reactor 1 and a low pressure reactor 2.  The high-pressure reactor 1 is equipped with a nozzle 3, through which hydrogen is removed from the reactor under high pressure, and a heating-cooling element 4, which serves to transfer high-temperature heat to the reactor.  Similarly, a low pressure reactor 2 is provided with a nozzle 5, through which low pressure hydrogen is supplied from a source, as well as heating-cooling elements 6 connected to a low-temperature heat absorber.  Both reactors are partially filled with hydride-forming material, which is cycled between reactors I and 2 using the device 7 for transporting the hydrated material through the supply line 8 of the hydrogenated material in the indicated solid arrow, and using the device 9 for moving the dehydrated material in the opposite direction through pipeline 10 and supply of dehydrated material.  For the thermal coupling of the two hydride forming material streams, a countercurrent heat exchanger P is used, by which part of the thermal energy of the hydride forming material leaving the high pressure reactor 1 is recovered and used to heat the hydride forming material entering the reactor 1.  FIG.  3 is a diagram of a pump operating in continuous mode for a pseudo-liquid hydride.  The pump contains a high pressure reactor 1 and a low pressure reactor 2 in which the corresponding hydride forming material is located.  High-pressure hydrogen is removed from reactor 1 through nozzle 3, and high-temperature heat is introduced using heating-cooling element 4.  Similarly, low pressure hydrogen is supplied to the low pressure reactor 2 through nozzle 5, and low temperature heat is removed from it by means of the heating and cooling element 6.  A pipeline 8, equipped with a throttle 12, is installed between two pressure reactors 1 and 2, the low pressure reactor 2 being located above the high pressure reactor 1, and the weight of the pseudo-liquid hydride located in the pipeline 8 is sufficient to maintain the required pressure difference between the reactors 2 and 1 .  Between reactors 2 and 1, pipeline 10 is installed, which acts as a bubble lift.  An additional heater 13 is associated with a portion of the pipeline 10.  Both conduits 8 and 10 are thermally coupled using a countercurrent heat exchanger 11, which transfers heat from the rising flow of pseudo-liquid dehydrated material in conduit 10 directed downward through the flow of pseudo-liquid hydride in conduit 8.  The heat exchanger 11 can be a very simple device that only provides thermal coupling between the two hydride-forming material streams.  Heat recovery in hydride pumps is carried out without the use of complex systems using a moving heat exchange medium and heat exchange pumps.  In this case, the hydride-forming material itself moves, and heat recovery is carried out by installing pipelines containing two hydride-forming material streams adjacent to each other and the heat-conducting material between them.  Pump (FIG.  4) contains a high-pressure reactor 1, equipped with a nozzle 3 for supplying high-pressure hydrogen, and a heating-cooling element 4 for removing high-temperature heat.  Low-temperature heat is supplied to the Low-pressure reactor 2 by means of the heating-cooling element b, and the low-pressure hydrogen is removed from the reactor through the nozzle 5.  Reactors 1 and 2 are connected with slotted bunkers 14, 15 and 16.  Valves 17-21 are provided to regulate the flow between the reactors and the shed hoppers.  Pump (FIG.  2) works as follows.  When devices 7 and 9 are turned on to move the hydrogenated and dehydrated material, the latter moves in a counterclockwise direction in a continuous cycle.  FIG.  Figure 5 is an idealized representation of the hydrogenation / dehydrogenation cycle, which is performed on the injection pump shown in FIG.  2  Point A in the graph of FIG.  5 represents the state of the dehydrogenated material entering the low pressure reactor 2, the hydrogen content, pressure and temperature of the material being low.  The material absorbs hydrogen in the reactor 2.  Low pressure hydrogen is taken up by the material during the exothermic reaction.  The heat energy is removed from the reactor 2 by means of a heating and cooling element 6 to maintain the hydrogenating material at the desired low temperature.  When the hydrogen content of the hydride forming material increases, the material from point A moves to point B in the graph of FIG.  five.  After saturation with the hydride, the material is transferred to the high pressure reactor, where it is heated by the heating and cooling element 4 to a higher temperature.  At this temperature, the equilibrium pressure of hydrogen becomes higher than before, and the high pressure hydrogen is withdrawn through nozzle 3, as a result of which the hydride is displaced from point C to point D in the graph of FIG.  five.  Heating-cooling element 4 supplies high-temperature heat, under the action of which the endothermic dehydrogenation process takes place.  After the material is substantially dehydrated, it returns from the high pressure reactor 1 to the low pressure reactor 2 to repeat the cycle, t. e.  the pump uses heat transfer from a higher temperature to a low temperature to compress the hydrogen.  The hydrogenation / dehydrogenation cycle shown in FIG.  2 and 5 can be reversed, and then the device functions as a heat pump.  High pressure hydrogen is used to transfer thermal energy from a low temperature heat source to a higher temperature.  In this case, the hydrogenated material (shown by the dotted line in FIG.  2) enters the low pressure reactor 2 through line 8.  Low pressure hydrogen is removed through the pipe 5, and this endothermic reaction proceeds under the action of the low-temperature heat of the heating-cooling element 6.  Applied to the graphics of FIG.  6, the material moves from point E to point F, as it desorbs hydrogen at. low temperature and pressure.  After the material has substantially dehydrated, it moves through conduit 10 to the high pressure reactor 1, where the material is exposed to high pressure hydrogen and absorbs hydrogen.  The exothermic absorption process is accompanied by the release of a large amount of heat, having a high temperature, which is absorbed by the heating and cooling element 4.  The hydride former shifts from point G to point H in the graph of FIG.  3 as it absorbs hydrogen.  After the material has undergone substantial hydrogenation, it is returned to the low pressure reactor 2 via line 8, and the cycle begins again.  The hydrogenation / dehydrogenation heat pump cycle proceeds under the action of high pressure hydrogen to transfer heat from a low temperature heat source to a high temperature heat absorber.  The composition curves shown in FIG.  5 and 6 are somewhat idealized since they do not take into account the effect of hysteresis.  In general, the actual pressure composition curves show that for a given temperature, the absorption will take place only at a pressure that is higher than the pressure at which desorption occurs.  Such an action will reduce the overall performance of the pump and may require an increase in the desorption temperature (pressure) or a decrease in the absorption temperature (pressure).  However, the resulting loss in productivity can be low due to careful selection of the hydride forming material.  Some hydrides produce a pronounced hysteresis, while in others the effect of hysteresis is almost negligible.  The composition curves in the graphs of FIG.  5 and 6 are idealized in the sense that the isotherms for any given hydride generator may not produce a region of perfectly constant pressure over a wide range of N / T.  Such a deviation from the fully isobaric behavior for a certain range of N / t will affect the overall efficiency of the hydride cycle.  Preferred hydride forming materials are those that have isotherms with an extended isobaric zone.  The hydride injection pump shown in FIG.  3, works as follows.  Since the circulation rate of the hydride-forming agent between the upper and lower reactors depends on throttle adjustment and the amount of heat added to the dehydride in line 10 (using an additional heater 13), the heat added to the dehydride using heater 13 causes additional hydrogen to desorb, which forms "bubbles in pseudo-liquid dehydride.  In another case, a carrier gas may be supplied to the conduit 10 to promote the formation of bubbles.  These bubbles reduce the total weight of the material in conduit 10 and cause the dehydride to rise upward through conduit 10 to the upper low pressure reactor 2.  After being in the upper reactor 2 for a time that is necessary for complete dehydrogenation, the material is lowered into the lower reactor 1 by gravity.  The reactors can be performed with high heat transfer characteristics and carry out a rapid displacement of the pseudo-liquid stream in order to guarantee a faster completion of the reaction than the average residence time of the material in reactors 1 and 2.  Alternatively, the material may pass through reactors 1 and 2 in the form of a layered or blocking flow, the average rate of which is chosen such as to ensure a complete reaction.  Pump operation (FIG.  4) is carried out as follows.  In the reactor 2 installed above the other reactor, a low pressure is constantly maintained.  The hydrated material falls into reactor 2 at a point at a certain height.  As hydrogen desorbs this material, heat is absorbed at the heating and cooling element 6.  The dehydrogenated material is displaced to the bottom of the reactor, since the dehydride is gradually removed from the base of the reactor 2.  Between the latter and the airlock hopper 15 is a valve 17.  The latter periodically opens to allow material to pass from reactor 2 to hopper 15, after which the valve closes. Hydrogen may be added to pressure in pressure bin. However, this may not be necessary for proper operation of the device.  At the base of the hopper 15, another valve 18 is installed, opening into the lower reactor 1.  When this valve 18 is open, the dehydrogenated particles fall from the airlock to the lower reactor 1, and the valve 18 is closed.  High-pressure hydrogen is fed to reactor 1 via nozzle 3.  This hydrogen is absorbed by the hydride-forming material, which exothermically releases the high-temperature heat absorbed by the heating and cooling element 4.  At the base of the reactor 1, a valve 19 is installed, opening into the lower lock tank 16, into which portions of the hydrated material are fed.  Thereafter, high pressure hydrogen is supplied to the hopper, and as soon as valve 19 is closed, valve 20 opens, whereby high pressure hydrogen flows into hopper 16.  The moving hydrogen transports the powder hydride to the upper bunker 14 where it is collected.  Hydrogen is removed from hopper 14 to re-adjust gas pressure before valve 21 opens, and a portion of hydride powder will fall into low pressure reactor 2.  The countercurrent heat exchanger 11 thermally binds the hydride located in the hopper 16 to the hydride-forming material in the bunker 15, thereby recovering part of the thermal energy of the hydride.  The use of a sluice hopper for transporting the hydride has been applied to both the hydride injection pumps and the hydride pumps, in which the high-pressure reactor is installed above the low-pressure reactor.  In this case, gravitational forces are used to move the powdered hydride generator down through the main part of the cycle, and the fluidized flow is used to lift the hydride generator to complete the cycle.  By varying the relative size of the lock bins 14, 15 and 16 with respect to reactors 1 and 2, the system can be performed to operate both in a continuous cycle and in a cycle of a moving batch.  When bunkers are used to transfer portions that are relatively small compared to the volume of hydroforming in any of reactors 1 and 2, the cycle is almost continuous.  Airlock bins can be made to place the entire contents of reactors 1 and 2 in them. In this case, the pump operates in a cycle of a moving batch.  Transportation of the hydride in the state of a pseudo-liquid drift (Fig.  3) the number of moving parts is minimized.  Since the weight of the pseudo-fluid hydride column is used to maintain the pressure drop between the upper and lower reactors, the vertical separation between the reactors must be chosen to ensure the required total pressure drop.  In many cases, and for many cycles of hydride (dehydrogenation), a relatively large vertical separation of pump units may be required.  Therefore, the use of this method is recommended for transporting a hydride for large scale industrial systems.  The second method of fluidized transport of hydride formers is shown in FIG.  6  The method, based on the use of slag bins, can be used with a low weight of the column hydride to maintain the pressure differential between the reactors.  The use of lock bins for hydride transportation provides a number of advantages over the design of FIG.  five.  The device can be made smaller, since here, to create a pressure differential in the system, the weight of the hydrating agent is not required.  However, the lock bins method requires the use of a large number of valves operating under severe conditions, including the flow of solid particles in many cases, as a result of which the maintenance of the valves is increased in order to ensure their proper operation.

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    权利要求:
    Claims (3)
    [1]
    1. HYDRIDE SUPPLY-HEAT PUMP, containing high and low pressure reactors filled with hydride-forming material, equipped with heating and cooling elements and hydride inlets and outlets, characterized in that, in order to increase efficiency, the reactors are interconnected by pipelines for supplying hydrogenated and dehydrogenated mate rial, having thermal contact with each other and equipped with devices for moving hydrogenated and dehydrogenated material from a low pressure reactor to high pressure reactor and in the opposite direction.
    [2]
    2. The pump according to π. 1, characterized in that the low-pressure reactor is located above the high-pressure reactor, and the device for moving the hydrogenated and dehydrogenated material is made in the form of a throttle and an additional heater installed respectively on the pipelines for supplying hydrogenated and dehydrogenated material.
    [3]
    3. The pump according to paragraphs. 1 and 2, characterized in that the device for conveying hydrogenated and dehydrogenated material is made in the form of airlock hoppers with inlet and outlet nozzles connected through valves to the pipelines for supplying hydrogenated and dehydrogenated material.
    Figure 1 ^ // 77
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    同族专利:
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3922872A|1975-02-04|1975-12-02|Us Energy|Iron titanium manganase alloy hydrogen storage|
    US3943719A|1975-02-26|1976-03-16|Terry Lynn E|Hydride-dehydride power system and methods|
    US4044819A|1976-02-12|1977-08-30|The United States Of America As Represented By The United States Energy Research And Development Administration|Hydride heat pump|
    US4039023A|1976-02-25|1977-08-02|The United States Of America As Represented By The Secretary Of The Navy|Method and apparatus for heat transfer, using metal hydrides|
    US4090361A|1976-03-15|1978-05-23|Terry Lynn E|Power cycles based upon cyclical hydriding and dehydriding of a material|
    US4055962A|1976-08-18|1977-11-01|Terry Lynn E|Hydrogen-hydride absorption systems and methods for refrigeration and heat pump cycles|
    GB1572737A|1977-01-17|1980-08-06|Exxon France|Heat pump|
    US4200144A|1977-06-02|1980-04-29|Standard Oil Company |Hydride heat pump|JPS5953201B2|1979-12-18|1984-12-24|Matsushita Electric Ind Co Ltd|
    JPS631148Y2|1980-04-03|1988-01-12|
    DE3020565A1|1980-05-30|1981-12-10|Studiengesellschaft Kohle mbH, 4330 Mülheim|METHOD AND DEVICE FOR ENERGY-SAVING PRODUCT HEAT FROM THE ENVIRONMENT OR FROM WASTE HEAT|
    JPS5924357B2|1980-06-23|1984-06-08|Kobe Steel Ltd|
    US4366680A|1981-01-28|1983-01-04|Lovelace Alan M Administrator|Cycling Joule Thomson refrigerator|
    US4436539A|1981-10-06|1984-03-13|Technion Research And Development Foundation Ltd.|Method and apparatus for air-conditioning by means of a hydrogen heat pump|
    US4425318A|1981-11-12|1984-01-10|Allied Corporation|Hydriding body-centered cubic phase alloys at room temperature|
    US4402187A|1982-05-12|1983-09-06|Mpd Technology Corporation|Hydrogen compressor|
    DE3310012A1|1983-03-19|1984-10-18|Bergwerksverband Gmbh, 4300 Essen|METHOD AND DEVICE FOR INERTING TRANSPORT CONTAINERS|
    US4659554A|1984-06-04|1987-04-21|Allied Corporation|Low-energy process for separation of hydrogen isotopes|
    US4599867A|1985-01-25|1986-07-15|Retallick William B|Hydrogen storage cell|
    US4641499A|1985-02-14|1987-02-10|The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration|Ten degree Kelvin hydride refrigerator|
    FR2582790B1|1985-06-04|1987-07-24|Elf Aquitaine|THERMOCHEMICAL PROCESS AND DEVICE FOR STORING AND CLEARING HEAT|
    DE3639545C1|1986-11-20|1988-06-01|Studiengesellschaft Kohle Mbh|Process for heat storage and transformation as well as cold generation|
    ES2036677T3|1987-04-14|1993-06-01|Uwe Rockenfeller|CHEMICAL ENERGY ACCUMULATION SYSTEM.|
    FR2615601B1|1987-05-22|1989-11-10|Faiveley Ets|DEVICE AND METHOD FOR PRODUCING COLD AND / OR HEAT BY SOLID-GAS REACTION|
    US4827726A|1987-07-14|1989-05-09|Ernest Gladstone|Method of and arrangement for generating hydrogen|
    DE3809680C2|1988-03-17|1991-03-21|Mannesmann Ag, 4000 Duesseldorf, De|
    US4928496A|1989-04-14|1990-05-29|Advanced Materials Corporation|Hydrogen heat pump|
    US4939902A|1989-10-24|1990-07-10|Retallick William B|Air conditioner for an automobile|
    US5048299A|1989-10-24|1991-09-17|Retallick William B|Air conditioner for an automobile|
    US5161382A|1991-05-24|1992-11-10|Marin Tek, Inc.|Combined cryosorption/auto-refrigerating cascade low temperature system|
    JP2624077B2|1992-02-15|1997-06-25|日本ケミコン株式会社|Solid electrolytic capacitors|
    US5450721A|1992-08-04|1995-09-19|Ergenics, Inc.|Exhaust gas preheating system|
    JP3407913B2|1992-12-28|2003-05-19|三洋電機株式会社|Heat transport system using hydrogen storage alloy|
    US5386705A|1993-08-27|1995-02-07|California Institute Of Technology|Staged regenerative sorption heat pump|
    AU2431595A|1995-05-02|1996-11-21|Thermal Electric Devices, Inc.|Low mass hydride heat pump|
    US6000463A|1999-01-19|1999-12-14|Thermal Corp.|Metal hydride heat pump|
    US7581698B2|2004-04-23|2009-09-01|Airbus Deutschland Gmbh|Method and apparatus for tempering gaseous and/or liquid media in transportation vehicles, particularly in aircraft|
    US7213409B1|2005-07-14|2007-05-08|The United States Of America As Represented By The Secretary Of The Navy|Reconfigurable hydrogen transfer heating/cooling system|
    US8318131B2|2008-01-07|2012-11-27|Mcalister Technologies, Llc|Chemical processes and reactors for efficiently producing hydrogen fuels and structural materials, and associated systems and methods|
    US9188086B2|2008-01-07|2015-11-17|Mcalister Technologies, Llc|Coupled thermochemical reactors and engines, and associated systems and methods|
    US7901491B2|2008-03-31|2011-03-08|General Electric Company|Hydrogen storage material and related system|
    US8246903B2|2008-09-09|2012-08-21|H.C. Starck Inc.|Dynamic dehydriding of refractory metal powders|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/923,805|US4178987A|1978-07-12|1978-07-12|Moving bed hydride/dehydride systems|
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