• 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:
    The invention relates to an energy storage process in which electric current is generated by water electrolysis H2, further produces CO 2 and is generated from the H2 and CO 2 by methanation CH4 and which is characterized in that: a) the CO 2 is produced next to CH4 in a biogas plant becomes; b) separating the CO 2 and CH 4 in the biogas in a membrane separation system by means of selective gas separation membranes into a CH 4 -rich gas stream and a CO 2 -rich gas stream, the CO 2 -rich gas stream becoming a CH 4, CO 2 and H 2 by methanation with the generated H 2 comprehensive product gas is implemented; c) separating at least a portion of the product gas in a membrane separation system to selectively separate CO 2 and H 2 from CH 4; and d) that the separation of the biogas and the separation of the product gas of the methanation are carried out simultaneously or alternately in the same Membrantrennsys system using gas separation membranes, which are capable of a selective separation of C02 and H2 of CH4.
    公开号:AT514614A1
    申请号:T629/2013
    申请日:2013-08-05
    公开日:2015-02-15
    发明作者:
    申请人:Tech Universität Wien；
    IPC主号:
    专利说明:

    The present invention relates to a method and a system for storing energy.
    Due to climate change and the scarcity of fossil energy resources, the focus of energy supply is increasingly shifting towards renewable energy sources. In addition to biomass, photovoltaics and wind power offer enormous potential for the production of climate-friendly energy. As the specific investment costs of these technologies decrease continuously and the operational stability and conversion rates are constantly improved, more and more photovoltaic and wind power projects are realized. For the near future, an average increase in energy production from wind and solar power of 7% per year is forecast.
    One of the main drawbacks of wind and solar power lies in the periodicity or uncontrollable fluctuation of energy production, which depends on the weather conditions. On windy and sunny days is sometimes overly much energy produced, while cloudy lulls or windless nights falls, however, virtually no energy. The solution to this problem is to store excess energy to use in periods of relative energy shortage.
    Since electrical power can not be " stored ", in the strict sense of the word, and any line (e.g., from one utility network to another) incurs corresponding line losses, storage of the electrical energy into other forms of energy, e.g. thermal or chemical energy.
    For example, it has been proposed to generate hydrogen (H 2) by means of excess current through electrolysis of water, which can be stored and, if necessary, incinerated or released again for the purpose of obtaining thermal energy. It is also known to use this hydrogen for the synthesis of methane (CH4) from carbon oxides (CO, CO2). The CH4 thus obtained is sometimes referred to as " Windgas " or " solar gas " designated.
    WO 2009/019159 A1, WO 2010/115983 A1 and DE 10 2011 013 922 A1 disclose processes and associated systems in which, for example, a carbon-containing gas containing H2, which is produced by water electrolysis by means of excess flow (eg from wind power - or photovoltaic systems) is converted (ie hydrogenated) to CH4 or other combustible hydrocarbons (eg by Fischer-Tropsch synthesis). By combustion of these hydrocarbons, in turn, electricity is generated (" power generation "). The combustion products can be recycled and reused for hydrocarbon synthesis. The carbon contained in the process is thus (at least partially) recycled.
    Among others, biogas or flue gases may be used as C02 source, whether entirely or only containing C02 after separation from the other components of the gas mixtures. Occasionally, the resulting in the generation of hydrocarbons, the flue gas can be separated, i. C02 be deposited therefrom and recycled for hydrocarbon synthesis.
    Furthermore, in the prior art, the possibility of feeding at least a portion of the hydrocarbons produced as additional or replacement gas in a basic gas network (which means especially additional methane or other hydrocarbons instead of methane in a natural gas network) is disclosed, as well as the use of the at Electrolysis of liberated oxygen for combustion in the conversion of CH4 (or other hydrocarbons), ie that also the 02 can be led in a circle.
    For the sake of simplicity, unless the context indicates otherwise, the term " methanation " used as a synonym for all such hydrocarbon syntheses using CO and / or CO 2 and H 2, even if not (only) methane, but (also) higher hydrocarbons are produced. Similarly, " methane " and " CH4 " also commonly used synonymously for " hydrocarbon " and thus also includes higher combustible hydrocarbons such as ethane, propane, etc. Similarly, " CO2 " and " carbon dioxide " also to understand CO or mixtures of CO2 and CO, unless specifically carbon monoxide or mixtures thereof with carbon dioxide are mentioned or the context mandatorily required, as will be apparent to those skilled in the art.
    In addition, hereinafter, " biogas " not only, as is common practice, the products of the fermentation of biomass, i. gas mixtures predominantly containing CH4 and C02, but also the gas mixtures obtained in the gasification of solid or liquid starting materials (eg biomass, wood, coal), which primarily CO and as minor constituents, depending on the gasification conditions, sometimes H2, CO2 and / or CH4 and small amounts of water vapor or other gases. If e.g. H2S is a component, the gas mixture can be desulfurized, since sulfur in the methanation is a catalyst poison for the most commonly used nickel catalysts.
    The disadvantages of the prior art methods described above are, in particular, that the hydrocarbons produced, such as e.g. CH4 are often not obtained in sufficient purity, but with more or less large amounts of other gases, especially CO or CO2 and H2, are contaminated. This makes direct use of the hydrocarbons through power generation or feeding into natural gas networks difficult or even impossible. In any case, due to the higher gas volume, the plants must be sized larger, which entails higher construction and operating costs, especially when the methanation one or more gas separation stages must be followed to separate individual accompanying gases from the desired hydrocarbons.
    The prior art offers only a partial solution to this problem by the optional separation of CO2 from biogas or flue gases, to then supply it substantially free of contaminating gases of the methanation. Since the methanation reaction, i. the hydrogenation of CO2 with H2 to hydrocarbons, which is incomplete, inevitably contains at least one starting component, ie CO2 and / or H2, in the product gas, and usually both.
    Against this background, the object of the invention was the development of an improved energy storage method and a corresponding system with which the above disadvantages can be at least partially eliminated.
    DISCLOSURE OF THE INVENTION
    This object is achieved in a first aspect of the present invention by providing a method of storing electricity by using electric current in a known manner to generate H2 by electrolysis of water, further producing CO2, from the generated H2 and CO2 by methanation CH4 is produced; and i) some or all of the generated gases are cached; and / or ii) the generated CH4 is emitted to generate electrical current; and / or iii) the generated CH4 is fed into a natural gas grid; and characterized in that: a) the CO 2 is produced in a biogas plant for producing CO 2 and CH 4 -containing biogas by fermentation of biomass or by gasification; b) the gases C02 and CH4 contained in the biogas produced are separated by means of a membrane separation system using one or more selective gas separation membranes into a CH4 rich gas stream and a CO2 rich gas stream, the CH4 rich gas stream being stored, flowed and / or into Natural gas network is fed and supplied to the C02-rich gas stream of the methanization and mixed with the H2 produced by water electrolysis and reacted to obtain a CH4, CO2 and H2 comprising product gas; c) separating at least a portion of the product gas of the methanation in a membrane separation system to selectively separate C02 and H2 from CH4; and d) that both the separation of the biogas and the separation of the product gas of the methanation are carried out simultaneously or alternately in the same membrane separation system using gas separation membranes capable of selective separation of CO2 and H2 from CH4.
    Thus, not only the CO 2 is separated from biogas by the method according to the present invention in order to be able to use it as a carbon source in the methanation, but also a separation of CO 2 and H 2 from the product gas of the methanation takes place. In principle, it is not decisive for the present invention whether the membrane separation system is provided in the course of the process before or after the methanation, since in both cases a CH4-rich gas stream is obtained whose purity is primarily dependent on the quality of the separation system.
    If the membrane separation is carried out prior to the methanation, most of the CH4 originating from the biogas plant does not even reach methanation, but is separated off in front of it, which enables a correspondingly smaller dimensioning of the later plant parts. If, on the other hand, the gas separation step takes place only after the methanization step, the proportion of contaminating gases in the mainly to be recovered CH4 is significantly lower, in particular the proportion of CO2, which makes it easier to obtain as pure methane as possible in order to exude it and / or be able to feed into natural gas networks.
    Rather, according to the present invention, it is crucial that only a single membrane separation system needs to be provided, which is able to selectively separate both CO 2 and H 2 from CH 4 by selecting appropriate gas separation membranes and operating parameters. The membrane-tensioning system can either alternately or simultaneously with biogas or product gas - which in the consequence always that of the methanation reaction, i. the product gas from step b), is meant to be fed.
    Especially with regard to the permissible limit values for the concentration of H2 in CH4 (in accordance with ÖVGW guideline G31 a maximum of 4% by volume and for individual applications even a maximum of 2% by volume), the process of the invention is advantageous Such low H2 contents with other separation methods than membrane separation processes (eg Kryover drive, adsorption and absorption) are not or can be achieved only with considerable effort.
    Of course, for certain applications, higher concentrations of H2 in the methane should be desired, such as e.g. for the production of "Hythan", a mixture of H2 and CH4 with usually 8 to 32% by volume H2, these are likewise readily available by appropriate choice of the process parameters of the membrane separation system (for example pressure, type and interconnection of the membranes).
    In particular, with alternate feeding of the membrane separation system with biogas and product gas, the system parameters, e.g. Operating pressure, membrane areas and interconnection of the membrane stages can be easily changed to achieve the desired degree of purity of the separated CH4. With simultaneous feeding with biogas and product gas, i. Mixing of the two streams in or before the membrane separation system, however, higher throughputs can be achieved.
    Furthermore, the fact that both gas separation steps are carried out in the same membrane separation system causes the CH4 with the desired purity to always occur at the same position in the process or in the system, which considerably simplifies the planning of the entire plant and lowers the construction costs.
    In preferred embodiments of the process according to the invention, the product gas of the methanation in the membrane separation step is separated into a CO 2 and H 2 -rich gas stream and a CH 4 -rich gas stream, the C02 and H 2 -rich gas stream, optionally after intermediate storage, being returned to the methanation and stored on CH4 rich gas stream is emitted and / or fed into a natural gas network. Thus, in these embodiments, in the membrane separation system, H2 and C02 are co-separated from CH4, requiring only membranes having selectivity for the other two gases with respect to CH4. This reduces the installation and operating costs of the plant.
    Alternatively, the methanation product gas in the membrane separation step may be separated into a CO2-rich gas stream, a H2-rich gas stream, and a CH4-rich gas stream, for which either two types of membranes are required, each having selectivity for either H2, and H2 CO2, compared to the other two gases in the mixture, or several stages of the same type of membranes are used and in each stage, a separate gas is selectively separated from the CH4.
    Selectivity is generally understood to mean the quotient of the permeabilities of membranes for different gases. For example, a selectivity of 10 for H2 in terms of CH4 means that hydrogen passes through a membrane labeled 10 times faster than methane.
    According to the invention membranes are used with high selectivity for several gases in relation to CH4, for which, for example, polymer film, metal or ceramic membranes are suitable. For example, dense polymer layers are typically much more permeable to H2 and CO2 than to CH4, and have, for example, H2 / CH4 selectivities of 60 and CO2 / CH4 selectivities of 20. In order to separate corrosive gas mixtures, more resistant ceramic membranes can also be used in this regard. However, because of their usually higher selectivity for the gases of interest, plastic membranes are preferred in the present invention, e.g. Commercially available polyimide membranes. These also often have very high selectivity for water, for example a selectivity H2O / CH4 of> 100, sometimes even 1000 or more, so that in preferred embodiments of the invention in addition to H2 and CO 2 and H20 is separated from the CH4. This means that the methane can also be dewatered at the same time, especially since H2O is produced as a by-product of methanation. In these preferred embodiments of the invention, therefore, the membrane separation step is preferably carried out only after the methanation step.
    By providing multiple membrane stages, overall faster separation is possible, and H2 and CO2, as well as H20 (if present in relevant amounts), can be obtained in separate streams, providing additional options for their use. Thus, for example, a portion of the hydrogen can also be used as a fuel gas instead of for the methanation - alone or, if necessary, even after backmixing with the purified methane (for example in the form of hydrogen).
    When using the above-described polymer film membranes having high selectivities for H 2 O, H 2 and CO 2 in relation to CH 4 (for example> 100, 60 or 20), H20 can be separated off in a first stage in a first stage, in a second stage in a second stage Stage H2 and finally CO2 to obtain purified CH4 as a third stage retentate. The separated amount of the respective component of the gas mixture depends u.a. from the membrane surfaces and the pressure conditions.
    It is understood that in all cases, the number of membranes is not particularly limited, so that in each separation stage and several membranes of the same type can be connected in series or in parallel. Preferably, the smallest possible number is selected, which is sufficient to ensure the desired purity levels of the separate gas streams, in particular of methane.
    The raw biogas may also be desulfurized or otherwise pre-treated before being fed to the membrane separation system to remove potential catalyst poisons, water, particulates, etc.
    Furthermore, the electric current used for water electrolysis preferably, although not necessarily, from plants for generating renewable energy from wind power or solar energy, since particularly strong fluctuations in power generation occur, which can be at least partially offset by the method of the invention. However, the origin of the stream is not limited to this. This can rather come from any (external) power sources.
    According to the present invention, it is thus possible, with a relative excess of electric current from the power source, to store mainly H2 and CH4 which, if required, can be emitted or fed into a natural gas network or else combined to Hythan. With a relative shortage of electrical current, however, mainly CO2, as a product of biogas production, stored, which is preferably supplied to the methanation, as soon as enough electricity and thus sufficient hydrogen from the water electrolysis are available.
    In a second aspect, the invention provides an energy storage system with which the method defined above can be carried out and which comprises, in a manner known per se, the following: at least one current source; - at least one hydrogen production plant for the production of H2 by water electrolysis; - at least one plant producing C02; at least one methanisation plant for producing CH 4 from CO 2 using the generated H2; - if necessary, gas storage for the gases produced; - where appropriate, a power plant for generating electricity by combustion of the CH4 produced; and - means for conducting electrical power and corresponding gas flows from one plant to another or to and from the gas reservoirs or for introduction into a natural gas network.
    The energy storage system according to the invention is characterized compared with the prior art in that: a) the plant for the production of CO 2 is a plant for the production of CO 2 and CH 4 -containing biogas by fermentation of biomass or gasification; b) the plant for producing CO 2 is followed by a membrane separation system comprising one or more gas separation membranes capable of selective separation of CO 2 and H 2 from the generated CH 4; c) means are provided for directing at least a portion of the product gas from the methanation plant to the membrane separation system; and d) means for recycling the separated in the membrane separation system CO2 and / or H2 are provided to Methanisierungsanlage.
    Thus, as described above, the membrane separation system can be fed both with biogas from the plant for the production of CO 2 and with product gas from the methanation plant - and this in turn alternately or simultaneously, which the person skilled in the art can achieve by means of appropriate piping, valve technology, etc. In general, the person skilled in the art, on the basis of his general knowledge, is aware of how the individual systems and other components of such an energy storage system according to the invention by means of corresponding lines, valves, flow dividers, compressors, pumps, etc., previously as " middle " are designated to connect and operate. This is also standard in the field of plant design as well as the determination of the type and number of gas storage tanks to be provided at which position in the overall system, in order to allow optimum operation depending on given boundary conditions.
    As with the analog method according to the first aspect, the advantages of the energy storage system according to the invention are, above all, that only a membrane separation system for cleaning, i. Separation, two process streams is required and that CH4 obtained with the desired purity always at the same position in the system. Again, the position of the membrane separation system - between biogas plant and methanation plant or only after the latter - is not critical, as long as it is ensured by appropriate wiring and interconnection that both the biogas and the product gas of methanation can be purified in the same membrane separation system. If, in addition to CO 2 and H 2, H 2 O are also to be separated off at the same time, a subsequent connection of the membrane separation system to the methanation plant is currently preferred.
    The power source is not particularly limited and may be both an integral part of the energy storage system and an external power source. In both cases, it is preferably a wind or solar power plant with corresponding fluctuations of the power generation, which are at least partially compensated by the energy storage system. The system for generating CO2 is again preferably followed by a device for desulfurization or other gas pretreatment to remove catalyst poisons.
    As also already mentioned in connection with the method according to the first aspect of the invention, the membrane separation system can be a single membrane separation stage for the simultaneous separation of CO2 and H2 from CH4 or two or more membrane separation stages for the sequential separation of CO2 and H2, and preferably also H20 , of CH4 - with the same advantages as mentioned above.
    BRIEF DESCRIPTION OF THE DRAWINGS
    Embodiments of the invention will now be described in detail with reference to the accompanying drawings, in which:
    Figures 1 to 3 are schematic representations of preferred embodiments of the method and apparatus of the invention.
    DETAILED DESCRIPTION OF THE INVENTION
    In Fig. 1, a relatively simple embodiment of the invention is shown as a flow chart. Links on top of a power source 1 is located, which as previously mentioned, may be part of the energy storage system as well as an external power source. In both cases, it is preferably a wind or solar power plant with correspondingly fluctuating power generation, which is at least partially compensated by means of the energy storage system of the invention.
    Electric power from this power source 1 is supplied to a hydrogen production plant 2 for generating H2 by electrolysis of water, i. the electrical energy is converted to 2 into chemical energy in the form of H2. Reference numeral 3 further denotes a plant for the production of CO2, which according to the present invention is preferably a biogas plant in which by fermentation of biomass or by gasification a mixture of CO2 and CH4 is produced. In the embodiment shown in FIG. 1, this is preferably fed to and compressed by a compressor 6.
    The reference numeral 6 of the compressor may be interpreted in the schematic diagrams of the drawings as being representative of all conduits, valves, compressors, pumps, and the like, commonly referred to as " means for conducting " (or for recycling or the like) are subsumable, such. Gas or power lines. In the drawings, gas lines are shown as arrows, the power line between the power source 1 and the hydrogen production plant 2, however, as a simple line. In general, all of these lines can be any components such as e.g. Compressors, which the skilled person considers necessary or preferred for smooth operation.
    The compressed biogas from compressor 6 is forwarded to a methanation plant 4 and mixed on the way there with H2 from hydrogen production plant 2, which in preferred embodiments of the invention can also be compressed to give a mixture together with the biogas from 3 and 6, that has the appropriate pressure for introduction into the methanation 4.
    In the methanation plant 4, CO 2 is reacted with H 2 to form CH 4, so that the fraction of CH 4 already contained in the biogas is generally increased significantly and a product gas is obtained, which is composed for example as follows: CH 4 89.7% by volume; C02 3.5% by volume; H2 6.8% by volume. Via line 6a, this product gas passes to the membrane separation system 7, which is shown in this preferred embodiment as a two-stage system with two separation stages 7a and 7b. In this case, the retentate from stage 7a is further purified in the second stage, the retentate of which is discharged as a substantially pure CH4 from the system of the invention, as indicated by the white arrow on the right. The permeate of stage 7a is fed to a gas storage 5, where it can be stored, if necessary in a liquefied state, before it is recycled for methanation.
    Assuming the use of preferred polyimide membranes as mentioned previously, e.g. those with a selectivity for the separation H2 / CH4 of 60 and with respect to CO2 / CH4 of 20, in both membrane separation stages - depending on the membrane areas and operating pressures of the separation stages - the permeate stream from 7a would mainly comprise H2 (and predominantly H2 and CO2), while the permeate from separation stage 7b, in economic plant design and process management, in addition to C02 and lower amounts of H2 would also comprise more or less high levels of CH4, which may sometimes even exceed 50 vol .-%. Thus, the former, H2-rich permeate stream from 7a could be cached as long as there is sufficient power supply from the power source 1 to the hydrogen production plant 2. Should this no longer be given, (additional) H2 from the storage 5 can be used for methanation.
    On the other hand, in the embodiment of the invention shown in FIG. 1, the permeate from separation stage 7b recycled directly into the stream of raw biogas from the plant 3 and compressed together with this at 6, mixed with H2 and the methanation supplied to the contained in the raw biogas and in the course of a first reaction with H2 in the methanation unit 4, only incompletely reacting CH2-reacted CO 2 one or more times with H2 and, at the same time, recycling the CH4 contained in this process stream so as to increase the overall yield of CH4.
    In cases where the permeate from separation stage 7b comprises mainly CO 2 and only comparatively small amounts of CH 4, this permeate can also be temporarily stored in a memory (not shown), e.g. if a sufficient supply of biogas from the biogas plant 3 is given anyway. In such a buffer, moreover, liquefaction of the CO 2 (for example by cryogenic processes) could be provided, whereby the space requirement is reduced and in particular the CH 4 (and H 2) fractions thereof can be separated off.
    At which point the feed of the permeates from the two separation stages 7a and 7b into the connection line (s) between the biogas plant 3 and the methanation plant 4 takes place is not decisive. However, those skilled in the art will readily be able to define the orifice points as well as the components provided therein (mixers, simple Y-pieces or the like) along with any additional compressors required, and so on.
    For a better overview, possible operating modes of the system from FIG. 1 for different boundary conditions (again) are briefly summarized. A) excess electricity: in Annex 2 sufficient Ho is generated
    The permeate from 7a, which mainly contains H2 and CO2, is temporarily stored in the memory 5 at least partially. As long as the biogas plant 3 produces sufficient CO 2 for the methanation in Appendix 4, it can be stored in its entirety. If the CO 2 production of the biogas plant 3 is insufficient, the permeate from 7 a can be separated in the storage 5 by means of liquefaction of the CO 2 and essentially only the hydrogen is buffered at 5, while the previously stored CO 2 from the gas storage 5 is continuously fed to the methanation.
    The permeate from 7b, which mainly comprises CH4 and CO2, is fully recycled. B) Electricity shortage: in Annex 2, too little (B1) or no (B2) H generates B1: The buffered hydrogen in memory 5 is used together with the H2 generated at 2 for methanation of the CO 2 from the biogas plant 3.
    The predominantly CH4 and C02 comprehensive permeate from 7b - or at least its largely separated from the CH4 portion of CO2 - is cached. B2: The electrolysis plant 2 and the methanation plant 4 are deactivated (or the latter bridged by means of bypass), and the gas separation system 7 is used exclusively for purifying the biogas from FIG.
    The permeate from 7a, which contains predominantly CO2, is temporarily stored until the power shortage has ended.
    The permeate from 7b is cached in the presence of very high proportions of CO 2, it can also be recycled at very high CH 4 content. In both cases essentially only the CH4 fraction is particularly preferably recycled and the CO.sub.2 component temporarily stored in liquid form.
    Two variants of the method and device of the present invention are shown in FIGS. 2 and 3 for illustrative purposes only. In both drawings, the H2-rich permeate stream is separated from separation stage 7a, one part of which is in turn buffered in storage 5, but the other part is recycled directly to the raw biogas. Such an embodiment has advantages, for example, if there is insufficient power available to continuously produce new hydrogen, or a cryogenic plant (not shown) for separating gases by means of liquefaction of the CO 2 may be provided at the fork point of the streams only the H2 is recycled and the liquefied C02 is temporarily stored in memory 5.
    In Fig. 2, the mixing with the biogas takes place in front of the compressor 6, while the intermediately stored gas as shown in Fig. 1 is then fed into the gas stream to Methanisierungsanlage 4. This is particularly advantageous in the case of intermediate storage of the CO 2 fraction in liquefied form, since the CO 2 then no longer needs to be compressed. In Fig. 3, on the other hand, all the recycled permeate streams are already mixed with the raw biogas prior to the compressor 6, which serves to temporarily store the permeate from 7a under (near) atmospheric pressure, i.e. when e.g. no separation of the C02 content from the H2 component takes place, but simply a part of the permeate from 7a is buffered in memory 5.
    As already mentioned, numerous modifications and variations to the illustrated embodiments of the invention are possible, and are readily apparent to those skilled in the art and provided on the basis of his general knowledge in the field of plant engineering.
    In any event, the invention provides a way in which gas streams of the desired purity, in particular a substantially pure stream of CH4, can be obtained by means of only a single gas membrane separation system in a process for storing energy and fluctuations in the output of a power source, e.g. a plant for the production of renewable energy from wind or solar energy, can be compensated in an economical manner.
    权利要求:
    Claims (14)
    [1]
    PATENT CLAIMS 1. A method of storing energy in which electric power is used to generate H2 by electrolysis of water, further producing CO2, from which generated H2 and CO2 are produced by methanation CH4; and i) some or all of the generated gases are cached; and / or ii) the generated CH4 is emitted to generate electrical current; and / or iii) the generated CH4 is fed into a natural gas grid; characterized in that: a) the CO2 is produced in a biogas plant for the production of biogas comprising CO 2 and CH 4 by fermentation of biomass or by gasification; b) the gases contained in the generated biogas CO2 and CH4 are separated by means of a membrane separation system using one or more selective gas separation membranes in a CH4 rich gas stream and a gas stream rich in CO2, wherein the CH4 rich gas stream stored, flows and / or in a Natural gas network is fed and supplied to the CO2-rich gas stream of the methanation and mixed with the H2 produced by means of water electrolysis and reacted to obtain a CH4, CO2 and H2 comprising product gas; c) separating at least a portion of the product gas of the methanation in a membrane separation system to selectively separate CO2 and H2 from CH4; and d) that both the separation of the biogas and the separation of the product gas of the methanation are carried out simultaneously or alternately in the same membrane separation system using gas separation membranes capable of selective separation of CO2 and H2 from CH4.
    [2]
    2. The method according to claim 1, characterized in that the product gas of the methanation in the membrane separation step is separated into a gas stream rich in C02 and H2 and a gas stream rich in CH4, wherein the gas stream rich in CO2 and H2 is again fed to the methanation.
    [3]
    3. The method according to claim 1, characterized in that the product gas of the methanation in the membrane separation step is separated into a gas stream rich in CO2, a gas stream rich in H2 and a CH4-rich gas stream.
    [4]
    4. The method according to any one of claims 1 to 3, characterized in that the electric power used for water electrolysis originates from plants for generating renewable energy from wind power or solar energy.
    [5]
    5. The method according to any one of claims 1 to 4, characterized in that the raw biogas is subjected to desulfurization before being fed to the membrane separation system.
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that are stored at a relative excess of electric current mainly H2 and CH4.
    [7]
    7. The method according to any one of claims 1 to 5, characterized in that is stored at a relative shortage of electricity mainly CO2.
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that gas separation membranes are used, which are able to separate in addition to CO2 and H2 and H2O of CH4.
    [9]
    9. An energy storage system operable using a method according to any one of claims 1 to 8 and comprising: - at least one power source (1); - At least one hydrogen generation plant (2) for generating H2 by water electrolysis; - at least one installation (3) for generating CO2; at least one methanization unit (4) for producing CH4 from CO2 using the generated H2; - optionally gas storage (5) for the generated gases; - where appropriate, a power plant for generating electricity by combustion of the CH4 produced; and - means (6) for conducting electrical power and corresponding gas flows from one installation to the other or to and from the gas storage facilities or for introduction into a natural gas network; characterized in that: a) the plant (3) for generating CO2 is a plant for producing biogas comprising CO2 and CH4 by fermentation of biomass or gasification; b) the system (3) for generating CO2 is followed by a membrane separation system (7) comprising one or more gas separation membranes capable of selective separation of CO2 and H2 from the generated CH4; c) means (6a) are provided for conducting at least a portion of the product gas from the methanation plant (4) to the membrane separation system (7); and d) means (6b) for recycling the separated in the membrane separation system (7) CO2 and / or H2 to the methanation system (4) are provided.
    [10]
    10. Energy storage system according to claim 9, characterized in that the power source (1) is a wind or solar power plant.
    [11]
    11. Energy storage system according to claim 9 or 10, characterized in that the system (3) for generating CO2, a desulfurization device is connected downstream.
    [12]
    12. Energy storage system according to one of claims 9 to 11, characterized in that the membrane separation system (7) comprises a single membrane separation stage (7a) for the simultaneous separation of C02 and H2 of CH4.
    [13]
    13. Energy storage system according to one of claims 9 to 11, characterized in that the membrane separation system (7) comprises two or more membrane separation stages (7a, 7b) for the sequential separation of C02 and H2 of CH4.
    [14]
    14 energy storage system according to any one of claims 9 to 13, characterized in that some or all of the gas separation membranes are able to separate in addition to C02 and H2 and H20 of CH4. Vienna, on the '' p. ÄUO. 2013 Vienna University of Technology represented by: Häupl & Ellmeyer KG
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    同族专利:
    公开号 | 公开日
    EP3030636A1|2016-06-15|
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    AT514614B1|2015-05-15|
    WO2015017875A1|2015-02-12|
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    DE102011107631A1|2011-06-30|2013-01-03|Torsten Dahl|Plant useful for using carbon dioxide from different sources, accumulating in temporally variable manner, for ecological energy, comprises e.g. device for producing hydrogen, and device for removing carbon dioxide-containing gases|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA629/2013A|AT514614B8|2013-08-05|2013-08-05|Method and system for storing energy|ATA629/2013A| AT514614B8|2013-08-05|2013-08-05|Method and system for storing energy|
    PCT/AT2014/050160| WO2015017875A1|2013-08-05|2014-07-16|Method and system for storing energy|
    EP14757830.6A| EP3030636A1|2013-08-05|2014-07-16|Method and system for storing energy|
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