CN102884226A - Method for producing hydrogen from water by means of a high temperature electrolyzer - Google Patents
Method for producing hydrogen from water by means of a high temperature electrolyzer Download PDFInfo
- Publication number
- CN102884226A CN102884226A CN2011800232431A CN201180023243A CN102884226A CN 102884226 A CN102884226 A CN 102884226A CN 2011800232431 A CN2011800232431 A CN 2011800232431A CN 201180023243 A CN201180023243 A CN 201180023243A CN 102884226 A CN102884226 A CN 102884226A
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- China
- Prior art keywords
- heat
- hydrogen
- water
- booster compressor
- electrolyzer
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Classifications
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention relates to methods for producing hydrogen from water by means of a high temperature electrolyzer and comprises the following steps: heating the water to a process temperature of the electrolyzer (2) of more than 500 DEG C, electrolyzing the water in the electrolyzer (2) to form product gases hydrogen (H2) and oxygen (O2), compressing the product gas hydrogen (H2) by means of a compressing apparatus (4), cooling the compressed hydrogen (H2) by means of a cooling medium (6) and feeding the thermal energy augmented in the cooling medium (6) to the heating process of the water.
Description
Technical field
The present invention relates to a kind of high-temperature electrolysis device that utilizes according to claim 1 and from water, produce the method for hydrogen, and a kind of according to claim 11 equipment for generation of hydrogen that comprises the high-temperature electrolysis device of preamble.
Background technology
Owing to the quick consumption of rechargeable energy requires storage from a large amount of electric energy of renewable origin (for example, wind energy, sun power).At this, relate to because the short-term buffering that the day border fluctuation of renewable energy source causes, and the long-term buffering that causes owing to the seasonal fluctuation of production of renewable energy resources and power requirement.If carry out storage to electric energy (this because low electrolytic cell voltage but favourable) by the high-temperature electrolysis water vapor, then must at first spend for the energy consumption of evaporation liquid water and be used for energy consumption with product gas hydrogen and oxygen compression at this.This energy consumption should be minimized, with the efficient of maximization power storage.
If power storage is carried out by the high-temperature electrolysis water vapor, then used the vaporizer that is used for liquid water and used the compressor that is used for product gas in system's output in system's input up to now.At this, vaporizer must be provided for the evaporation enthalpy of required reactants water steam and the compression energy that compressor must be provided for product gas hydrogen and oxygen.
Summary of the invention
Therefore, technical problem to be solved by this invention provide with respect to prior art have obvious improved energy balance in order to water is converted into equipment and the method for hydrogen by high-temperature electrolysis.
This technical problem is solved by a kind of method and a kind of equipment for generation of hydrogen with feature of claim 11 for generation of hydrogen with feature of claim 1.
The method of utilizing the high-temperature electrolysis device to produce hydrogen from water according to the present invention comprises the steps:
At first, water is heated to the process temperature of electrolyzer, wherein process temperature particularly is between 600 ℃ to 800 ℃ usually above 500 ℃.In next step, in electrolyzer, carry out the electrolysis of water, wherein produce product gas hydrogen and oxygen from reactants water.Further, cool off the hydrogen that is compressed with the product gas hydrogen compressed and by heat-eliminating medium with gas booster compressor.The heat energy of putting aside in heat-eliminating medium in cooling is fed in the water heat-processed of forming process reactant.
The compression of the product gas hydrogen that produces is essential or suitable, so that hydrogen is stored during with as far as possible little volumetric flow rate, until hydrogen is used to obtain energy again.But introduced merit by being compressed in the product gas hydrogen (H2).By the compression work of this introducing, hydrogen is heated significantly, surpasses 400 ℃ temperature so that hydrogen can have according to external boundary condition under the pressure that for example is in 100bar after the compression.According to the present invention, this energy is transferred to heat-eliminating medium with the form of the heat energy of hydrogen, and wherein heat-eliminating medium is heated and has carried again the heat energy of the hydrogen that is cooled at present.This heat energy is used for adding again the water that the thermosetting raw material is the reactant of electrolytic process suitably.Therefore, obviously improved the energy balance of whole process.
Heat energy also can be described as heat transfer process by the reception of refrigerant.For keeping heat transfer process effective as far as possible, can be suitably with compression process be attached thereto the heat exchange or the process of cooling that connect and be configured to a plurality of levels, i.e. cascade.
In heat transfer process, suitable is by for example gas booster compressor cooling of compressor of heat-eliminating medium.Therefore heat-exchange equipment is as the whole integral part of gas booster compressor.
On the other hand, gas booster compressor is adiabatic with respect to its environment in the zone of heat-flash load at least in part, and the gas that compresses for example cooled off by heat-exchange equipment in gaseous conductance subsequently.
Basically, suitable in all alternative is that gas booster compressor is passed with the cooling channel, so that the heat of accumulating in gas booster compressor can be used suitably.
In other suitable form of implementation, compressed product gas is but hydrogen-cooled and comprise water as the heat-eliminating medium of the part of heat-exchange equipment, and described water is again as the reactant that is used for electrolytic process.At this, reactants water (process water) is conducted through heat-exchange equipment as refrigerant, and is introduced in the electrolyzer with corresponding temperature with vapor form at last.
Also being proved to be suitable is will leave from the electrolyzer that also has about 500 ℃ to 800 ℃ electrolyzer process temperature but hydrogen-cooled, then with described hydrogen compressed.It is suitable carrying out this process of cooling before compression, so that gas booster compressor is not subject to unnecessary thermal load.At this, suitable is that the reactants water that will have vapor form in heat transfer process joins the product gas hydrogen of heat and/or the product gas oxygen of heat.This heat transfer process by preferably also using with the form of convection recuperator can be directly used in the used heat of product gas the heating to reactant.In the particularly preferred thermal insulation of electrolyzer self and the situation in the effective heat exchange of product and reactant, the energy waste of high-temperature electrolysis device is very low.
In described method so far, especially with hydrogen as the product gas compression and will be provided to again at the energy of this formation the heat-processed of water.Basically, also can be suitable be with oxygen compression and temporarily storage in the case that provides especially for this reason.If oxygen also should be compressed, then also be similar to the heating that aforementioned description was exported and was provided to water in this formed heat of compression, this has improved the efficient of process again.
Other integral part of the present invention is the equipment for generation of hydrogen.This equipment comprises for the high-temperature electrolysis device that water is converted into hydrogen.In addition, this equipment comprises the gas booster compressor of the hydrogen that produces for compression.Gas booster compressor comprises again heat-exchange equipment, and described heat-exchange equipment is used for being transferred in the heat of compression that compression process produces the reactants water of high-temperature electrolysis device.Gas booster compressor preferably is configured to the form of compressor at this.
According to claim 11, equipment be used for the described method of executive basis claim 1 to 9 especially, and have respectively the advantage of having explained.
At this, may be suitable be that gas booster compressor is being subject to being adiabatic in the zone of heat-flash load in its environment especially.At this, gas booster compressor is not discharged the heat of compression that produces to environment, and the described heat of compression can obtained from hydrogen after compression process by the heat-exchange equipment that links to each other targetedly.
To this alternatively or addedly, may be suitable be so that heat-exchange equipment partly surrounds gas booster compressor, this realizes by the heat energy of being introduced by compressed element that for example makes the cooling channel pass gas booster compressor and therefore to obtain gas booster compressor.
Description of drawings
Other form of implementation of the present invention and other characteristics are explained in detail according to following accompanying drawing.At this, has identical title but the feature of different structure is endowed identical Reference numeral.
Each figure is:
Fig. 1 shows the indicative flowchart of the hydrogen generation of passing through the high-temperature electrolysis device of hydrogen compressed with the connection,
Fig. 2 shows the indicative icon of process flow as shown in Figure 1, and wherein heat-eliminating medium is configured to the form of reactants water,
Fig. 3 shows the gas booster compressor that the passage that is cooled passes, and
Fig. 4 shows with the gas booster compressor of adiabatic apparatus with the interchanger that is connected.
Embodiment
Hereinafter, schematically explained a kind of method of utilizing the high-temperature electrolysis device from water, to produce hydrogen according to Fig. 1.At first, will be labeled as H
2O
fLiquid water be directed in the interchanger 10 by water supply part 18.The heat-eliminating medium 6 that has had heating in this interchanger 10 further also will discussed in the flow process for its heating, by described heat-eliminating medium 6 with liquid water be heated in the boiling spread temperature and with its evaporation.
In next step, will be labeled as H
2O
gThe water of evaporation, also be the water of gaseous state, be incorporated in the other interchanger 10 '.By this interchanger 10 ' with water vapor or vaporous water H
2O
gBe heated to similarly the process temperature of high-temperature electrolysis device 2.Vaporous water H in the 2 interior introducings of high-temperature electrolysis device
2O
gHas about 500 ℃ to 800 ℃ temperature.In the electrolyzer 2 that is also referred to as soild oxide electrolyzer (SOE), with water H
2O
gBe converted in known manner product gas hydrogen (H
2) and oxygen (O
2).The product gas that is called especially hereinafter hydrogen leaves from electrolyzer 2, and also has the almost process temperature of electrolyzer at this.Particularly the product gas of hydrogen is cooled in interchanger 10 ' again and preferably is lower than 100 ℃ temperature, preferably is cooled to especially the room temperature (about 50 ℃) of about room temperature or rising.
Although two interchanger 10 ' are illustrated as to be in position separately only owing to the diagram reason illustrates in circulation in Fig. 1.Preferably, for interchanger 10 ', use described convection recuperator, wherein in two passages that are interweaved, guide relatively cold heat-eliminating medium in a side, be vaporous water in this case, at the medium of opposite side guiding relatively hot, be the hydrogen from electrolyzer in this case, although wherein these two media are separated from each other by system and are mutually heated.This means that for example the water vapor of 100 ℃ heat enters and run into herein the hydrogen of about 600 ℃ to 800 ℃ heat in a side of convection recuperator 14.When the mutual circulation of this interchanger, hydrogen H
2Constantly cooled off, until it has the output temperature of the water vapor that roughly flows into, namely about 100 ℃.In contrast, water H
2O
gWhen flowing through convection recuperator 14, constantly heated, until it has the hydrogen H that almost leaves from electrolyzer 2 when leaving interchanger 14
2Temperature.
Certainly, in this interchanger, there is certain thermosteresis, but in the situation of whole system-gas that namely enters and leave and the good thermal insulation of electrolyzer 2, when whole system once was heated to 600 ℃ to 800 ℃ process temperature, described thermosteresis was relatively low.The thermosteresis of high-temperature electrolysis device is therefore because the good thermal insulation of aforementioned heat transfer process and whole equipment is relative low.
What still notice in this case, is reactants water owing to the reason of process technology is provided to the hydrogen of the low amount that branches out from the product hydrogen that leaves.
100 ℃ the hydrogen of being cooled to now that still can again be cooled off in further circulation or can be cooled with other interchanger must be compressed with economically storage.At this, what possibility was suitable is that hydrogen pressure is reduced to about 100bar.Under 100 times of atmospheric pressure storages, the volume of gas reduces by 100 times.Purpose is that hydrogen is stored in the torage tank to conserve space as far as possible.Approximately 100bar(is especially between 50bar and 200bar) storage pressure be proved to be technical suitable, and realize economically.
But, when hydrogen compressed in gas in hydrogen (or in similarly using also in the second product gas oxygen also) introduced compression work.This compression work is converted into heat in compressed gas system, therefore with compressed hydrogen intense heating.According to external boundary condition, compressed hydrogen has 200 ℃ to 600 ℃ temperature under the pressure of common 100bar.Basically, this heat energy of gas is the energy that in advance is incorporated in the compressor with the form of electric energy and loses during with gas cooling when processing such as normal conditions.This energy is released in the environment.But be uneconomic in this process, therefore, also introduced heat transfer process in suitable mode in the case, described heat transfer process obtains heat energy from the gas of compression, and the described heat energy that obtains is supplied to again reactants water, particularly liquid water.This illustrates by two interchanger 10 that begin in process to locate with the end of processing place in Fig. 1.In the bottom of Fig. 1, namely at liquid water H
2O
fThe zone in interchanger 10 and in the upper area of Fig. 1 at H to be compressed
2The zone in interchanger 10 formed a unit, therefore described unit interconnects by the pipeline 7 that transports corresponding heat-eliminating medium 6, and is endowed a Reference numeral.
Interchanger 10 in upper area comprises gas booster compressor 4, and described gas booster compressor 4 is for example as in the form that can be configured to have compressor 12 as shown in Fig. 3 and Fig. 4, and described interchanger 10 obtains heat energy from gas booster compressor 4.This can occur in cooling step, but this also can be by a plurality of gas booster compressors 4 one after the other be connected with heat-exchange equipment 10 front and back cascade ground occur, illustrate as shown in FIG. 1 routinely.
In this made compressed product gas (for example for hydrogen) is stored in schematically illustrated case 16 now compressedly.On the right side, the operation of dehydrogenation also typically illustrates oxygen O outward
2Leave, oxygen is usually not compressed, because the storage of oxygen only is worth in a few cases, but basically can with for hydrogen process in the same manner for oxygen yet, this has still formed the energy balance of the interchanger in the aforementioned system effectively.
In the process described in Fig. 1, heat-eliminating medium 6 moves in the circulation of sealing respectively, at this, process medium, namely arrives in the electrolyzer 2 as reactant and the water that is converted into hydrogen carries out other operation.Illustrate in Fig. 2 the substituting of this situation, wherein heat-eliminating medium 6 is configured to have the form of process water.In the right regions of Fig. 2, be labeled as H
2O
fLiquid water be fed into as heat-eliminating medium 6 in the cooling pipe system of cooling duct 7, described heat-eliminating medium 6 flows through from the hydrogen of compression and obtains the interchanger 10 of heat energy.At this, water is heated, preferably is heated to surpass 100 ℃ temperature, and described water further is in gaseous state now, and be introduced in next interchanger 10 ' along pipeline 7, described interchanger 10 ' can be configured to again to have the favourable structural form of the form of convection recuperator.At this, water (H
2O
g) with awfully hot process gas H
2(〉 500 ℃) meet and carry out with it heat exchange.After process this interchanger 10 ' or 14, the vaporous water that almost is preheating to about 600 ℃ to 800 ℃ process temperature now is introduced in the electrolyzer 2, and then is converted in known manner hydrogen.Certainly, also can additionally heat, with the thermosteresis of compensation to environment.
Hydrogen leaves from electrolyzer, is cooled as described in interchanger 14, then reaches again the temperature between room temperature and 100 ℃, and compressed by compression set 4.Further, in this embodiment according to Fig. 2, different from situation in Fig. 1, direct cooled compressed equipment, but adiabatic as mentioning hereinafter gas booster compressor, so that the hydrogen of heat further is being cooled in interchanger 10 in the circulation as described.Can carry out other cascade compression in other gas booster compressor 4, the hydrogen that then will be fully compressed now is stored in again in the corresponding case 16.The thermal insulation of gas booster compressor and heat exchange then also can be applicable to certainly at the embodiment shown in Fig. 1.
Provided typically illustrating of gas booster compressor 4 in Fig. 3 and Fig. 4, described gas booster compressor 4 has respectively compression space 20 and stroke piston 26.Compression process very schematically is described at this, and Fig. 3 and Fig. 4 do not have the requirement for integrity.The feature of two compressors 12 in Fig. 3 and Fig. 4 is to have hydrogen to supply with part 22 and hydrogen discharge part 23.Stroke piston 26 moves up and down in compression space 20, and this is by the diagram of the double-headed arrow on the stroke piston side.Stroke piston 26 preferably for example passes through camshaft actuated by eccentric equipment.
In Fig. 3, compressor 12 is that the special structural form of general gas booster compressor 4 passage 8 that is cooled passes.Cooling channel 8 obtains the heat that produces in compression process, and this hot type is gone out.Therefore cooling channel 8 is the integral part of heat exchange equipment 10 in concrete structure.
In the structural form according to Fig. 4, gas booster compressor 4 or compressor 12 provide insulation 28, wherein also provide hydrogen to supply with part 22 and hydrogen discharge part 23, compressor 12 is in this process temperature work to raise, and the hydrogen from pipeline 23 that has been in compressed format is cooled by the interchanger 10 that separates now.At this heat energy that obtains as describing for heat-processed water.Certainly, the gas booster compressor 4 among Fig. 3 also can have insulation, with this centralized heat energy ground that is produced is discharged by cooling channel 8.
Claims (15)
1. method of utilizing the high-temperature electrolysis device to produce hydrogen from water, described method comprises the steps:
-water is heated to 500 ℃ the process temperature of surpassing of electrolyzer (2),
-in electrolyzer (2) brine electrolysis to produce product gas hydrogen (H
2O) and oxygen (O
2),
-pass through gas booster compressor (4) with product gas hydrogen (H
2) compression,
-by heat-eliminating medium (6) with the hydrogen (H that compresses
2) cooling, and
-the heat energy that will put aside in heat-eliminating medium (6) is provided in the heat-processed to water.
2. method according to claim 1 is characterized in that, to hydrogen (H
2) be compressed in a plurality of compression steps and carry out, described compression step again with a plurality of process of cooling associatings.
3. method according to claim 1 and 2 is characterized in that, gas booster compressor (4) is by heat-eliminating medium (6) cooling, and the heat energy of described heat-eliminating medium (6) is provided for the heat-processed to hydrogen.
4. described method in 3 according to claim 1 is characterized in that gas booster compressor (4) is adiabatic with respect to its environment at least in part.
5. according to claim 3 or 4 described methods, it is characterized in that gas booster compressor (4) passage (8) that is cooled passes.
6. according to described method in the aforementioned claim, it is characterized in that the water that is used for reaction that is provided to electrolyzer (2) comprises heat-eliminating medium at least in part.
7. according to described method in the aforementioned claim, it is characterized in that hydrogen (H
2) leaving electrolyzer (2) afterwards and before compression, be cooled by heat transfer process.
8. method according to claim 7 is characterized in that, hydrogen (H
2) after leaving electrolyzer (2), be cooled by convection recuperator.
9. according to claim 7 or 8 described methods, it is characterized in that, the water that is provided to electrolyzer (2) with vapor form as heat-eliminating medium in heat transfer process with hydrogen (H
2) cooling and be heated simultaneously.
10. according to described method in the aforementioned claim, it is characterized in that, except product gas hydrogen (H
2) outside, oxygen (O
2) as other product gas also compressed, cooling, and simultaneously the heat energy of discharging is offered heat-processed to water.
11. the equipment for generation of hydrogen, described equipment comprise that high-temperature electrolysis device (2) is to be converted into water hydrogen (H
2), and the gas booster compressor (4) that is used for the hydrogen compressed that will produce, wherein gas booster compressor (4) comprises heat exchange equipment (10), and described heat exchange equipment (10) is used for being transferred in the heat of compression that compression process occurs the water that supplies to high-temperature electrolysis device (2).
12. equipment according to claim 11 is characterized in that, gas booster compressor (4) is configured to the form of compressor (12).
13. according to claim 11 or 12 described equipment, it is characterized in that gas booster compressor (4) is insulated at least in part.
14. described equipment in 13 is characterized in that gas booster compressor (4) is surrounded by heat-exchange equipment (10) at least in part according to claim 11.
15. described equipment in 14 is characterized in that heat-exchange equipment (10) passes gas booster compressor (4) with the form of cooling channel (8) at least in part according to claim 11.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102010020265.7 | 2010-05-11 | ||
| DE102010020265A DE102010020265A1 (en) | 2010-05-11 | 2010-05-11 | Process for producing hydrogen from water by means of a high-temperature electrolyzer |
| PCT/EP2011/054768 WO2011141221A1 (en) | 2010-05-11 | 2011-03-29 | Method for producing hydrogen from water by means of a high temperature electrolyzer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102884226A true CN102884226A (en) | 2013-01-16 |
Family
ID=44168190
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011800232431A Pending CN102884226A (en) | 2010-05-11 | 2011-03-29 | Method for producing hydrogen from water by means of a high temperature electrolyzer |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20130126360A1 (en) |
| EP (1) | EP2569463A1 (en) |
| CN (1) | CN102884226A (en) |
| DE (1) | DE102010020265A1 (en) |
| WO (1) | WO2011141221A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108699713A (en) * | 2016-01-04 | 2018-10-23 | 法国电力公司 | Prepare the system of hydrogen and relevant method |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2015052147A (en) * | 2013-09-06 | 2015-03-19 | 株式会社東芝 | Electrochemical apparatus and operation method thereof |
| JP6363471B2 (en) * | 2014-10-31 | 2018-07-25 | 株式会社東芝 | Hydrogen production apparatus and hydrogen production method |
| DE102015206288A1 (en) | 2015-04-09 | 2016-10-13 | Robert Bosch Gmbh | Apparatus, system and method for recovering hydrogen from water using a working agent |
| FR3061496B1 (en) * | 2017-01-05 | 2019-05-31 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | GAS OVERHEATING SYSTEM IN SOEC / SOFC TYPE SOLID OXIDE STRIP ENTRY |
| CN106884182A (en) * | 2017-03-22 | 2017-06-23 | 成都艾欧新能源科技有限公司 | High-temperature solid oxide electrolytic cell |
| EP3489389A1 (en) * | 2017-11-24 | 2019-05-29 | Siemens Aktiengesellschaft | Electrolytic unit and electrolyzer |
| FR3115797B1 (en) * | 2020-10-30 | 2023-01-13 | Commissariat Energie Atomique | High temperature electrolyser system optimized by increasing the pressure at the electrolyser outlet |
| FR3115796B1 (en) * | 2020-10-30 | 2024-03-08 | Commissariat Energie Atomique | High temperature electrolyzer system optimized by coupling to a heat pump |
| FR3115798B1 (en) * | 2020-10-30 | 2022-11-04 | Commissariat Energie Atomique | High temperature electrolyser system optimized by depression of the steam supply |
| FR3122669B1 (en) * | 2021-05-04 | 2023-04-21 | Commissariat Energie Atomique | Compression-optimized high-temperature electrolyser system |
| FR3122670B1 (en) * | 2021-05-04 | 2023-04-21 | Commissariat Energie Atomique | High temperature electrolyser system with optimized energy consumption |
| WO2023139504A1 (en) * | 2022-01-18 | 2023-07-27 | Bloom Energy Corporation | Compressor integration and safe operation start up for atmospheric operation of soec systems |
| CN114574875B (en) * | 2022-03-02 | 2023-09-05 | 上海核工程研究设计院股份有限公司 | Comprehensive utilization system for electrolytic hydrogen production of nuclear power plant |
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|---|---|---|---|---|
| US4087976A (en) * | 1976-08-13 | 1978-05-09 | Massachusetts Institute Of Technology | Electric power plant using electrolytic cell-fuel cell combination |
| US20050284154A1 (en) * | 2004-06-25 | 2005-12-29 | Peter Andrew M | System and method for storing hydrogen at cryogenic temperature |
| US20070000789A1 (en) * | 2005-06-30 | 2007-01-04 | Libby Cara S | Integrated hydrogen production and processing system and method of operation |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3616334A (en) * | 1968-07-05 | 1971-10-26 | Gen Electric | Electrically and chemically coupled power generator and hydrogen generator |
| JP3253985B2 (en) * | 1991-10-11 | 2002-02-04 | 関西電力株式会社 | Power storage device |
| CA2676576A1 (en) * | 2009-04-22 | 2009-11-16 | Hte Water Corporation | System and process for converting non-fresh water to fresh water |
-
2010
- 2010-05-11 DE DE102010020265A patent/DE102010020265A1/en not_active Ceased
-
2011
- 2011-03-29 EP EP11714955A patent/EP2569463A1/en not_active Withdrawn
- 2011-03-29 CN CN2011800232431A patent/CN102884226A/en active Pending
- 2011-03-29 US US13/697,292 patent/US20130126360A1/en not_active Abandoned
- 2011-03-29 WO PCT/EP2011/054768 patent/WO2011141221A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4087976A (en) * | 1976-08-13 | 1978-05-09 | Massachusetts Institute Of Technology | Electric power plant using electrolytic cell-fuel cell combination |
| US20050284154A1 (en) * | 2004-06-25 | 2005-12-29 | Peter Andrew M | System and method for storing hydrogen at cryogenic temperature |
| US20070000789A1 (en) * | 2005-06-30 | 2007-01-04 | Libby Cara S | Integrated hydrogen production and processing system and method of operation |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108699713A (en) * | 2016-01-04 | 2018-10-23 | 法国电力公司 | Prepare the system of hydrogen and relevant method |
| CN108699713B (en) * | 2016-01-04 | 2019-07-30 | 法国电力公司 | Prepare the system and relevant method of hydrogen |
Also Published As
| Publication number | Publication date |
|---|---|
| US20130126360A1 (en) | 2013-05-23 |
| DE102010020265A1 (en) | 2011-11-17 |
| WO2011141221A1 (en) | 2011-11-17 |
| EP2569463A1 (en) | 2013-03-20 |
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Application publication date: 20130116 |