• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Apparatus for membrane permeation treatment of a feed gas stream (6) comprising at least methane and carbon dioxide to produce a gas stream (12) enriched in methane comprising: - a first separation unit (1) by membrane for receiving the feed gas stream and producing a first permeate (4) enriched in carbon dioxide and a first retentate (7) enriched in methane, - a second unit (2) membrane separation to receive the first retentate (7) and producing a second permeate (5) enriched in carbon dioxide and a second retentate (8) enriched in methane, - a gas-gas ejector (11) for increasing the pressure of the first permeate ( 4) at a pressure of between 2 and 6 bar, more preferably between 3 and 4 bar. - a third membrane separation unit (3) for receiving the first permeate (4) compressed in the ejector and producing a third retentate (9) enriched in methane and a third permeate (10) enriched in CO2.
    公开号:FR3063437A1
    申请号:FR1751688
    申请日:2017-03-02
    公开日:2018-09-07
    发明作者:Guenael Prince；Nicolas Paget；Golo Zick
    申请人:Air Liquide SA；LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude；
    IPC主号:
    专利说明:

    Holder (s): AIR LIQUIDE, ANONYMOUS COMPANY FOR THE STUDY AND EXPLOITATION OF GEORGES CLAUDE PROCESSES Société anonyme.
    Extension request (s)
    Agent (s): AIR LIQUIDE.
    INSTALLATION AND METHOD FOR THE TREATMENT BY MEMBRANE PERMEATION OF A GAS SUPPLY FLOW COMPRISING METHANE AND CARBON DIOXIDE.
    FR 3 063 437 - A1
    Installation for the treatment by membrane permeation of a feed gas flow (6) comprising at least methane and carbon dioxide to produce a gas flow (12) enriched in methane comprising:
    - a first membrane separation unit (1) making it possible to receive the feed gas flow and to produce a first permeate (4) enriched in carbon dioxide and a first retentate (7) enriched in methane,
    - a second membrane separation unit (2) making it possible to receive the first retentate (7) and to produce a second permeate (5) enriched in carbon dioxide and a second retentate (8) enriched in methane,
    - A gas-gas ejector (11) for increasing the pressure of the first permeate (4) to a pressure between 2 and 6 bar, more preferably between 3 and 4bar.
    - a third membrane separation unit (3) making it possible to receive the first permeate (4) compressed in the ejector and to produce a third retentate (9) enriched in methane and a third permeate (10) enriched in CO2.

    The present invention relates to an installation and a process for the treatment by membrane permeation of a gas stream containing at least methane and carbon dioxide to produce a gas stream rich in methane.
    It relates in particular to the purification of biogas, with the aim of producing biomethane in accordance with the specifications for injection into a natural gas network.
    Biogas is the gas produced during the degradation of organic matter in the absence of oxygen (anaerobic fermentation) also called methanization. It may be natural degradation - this is observed in marshes or household waste dumps - but the production of biogas can also result from the methanisation of waste in a dedicated reactor, called a methanizer or digester.
    Due to its main constituents - methane and carbon dioxide - biogas is a powerful greenhouse gas; it also constitutes, at the same time, an appreciable source of renewable energy in a context of scarcity of fossil fuels.
    Biogas mainly contains methane (CH4) and carbon dioxide (CO2) in variable proportions depending on the method of production, but also, in smaller proportions, water, nitrogen, hydrogen sulfide, oxygen, as well as other organic compounds, in trace amounts.
    Depending on the degraded organic matter and the techniques used, the proportions of the components differ, but on average biogas comprises, on dry gas, from 30 to 75% of methane, from 15 to 60% of CO2, from 0 to 15% of nitrogen, 0 to 5% oxygen and trace compounds.
    Biogas is valued in different ways. After a light treatment, it can be used near the production site to provide heat, electricity or a mixture of the two (cogeneration); the high content of carbon dioxide reduces its calorific value, increases the compression and transport costs and limits the economic interest of its recovery to this local use.
    Further purification of the biogas allows its wider use, in particular, further purification of the biogas makes it possible to obtain a biogas purified to the specifications of natural gas and which may be substituted for it; the biogas thus purified is “biomethane”. Biomethane thus complements natural gas resources with a renewable part produced in the heart of the regions; it can be used for exactly the same uses as natural gas of fossil origin. It can supply a natural gas network, a filling station for vehicles, it can also be liquefied to be stored in the form of liquid natural gas (LNG) ...
    The methods of valorization of biomethane are determined according to the local contexts: local energy needs, possibilities of valorization as biomethane fuel, existence close to networks of distribution or transport of natural gas in particular. Creating synergies between the various actors working on a territory (farmers, industrialists, public authorities), the production of biomethane helps the territories to acquire greater energy autonomy.
    Several steps must be taken between the collection of biogas and the obtaining of biomethane, the final product capable of being compressed or liquefied.
    In particular, several steps are necessary before the treatment which aims to separate the carbon dioxide to produce a stream of purified methane. A first step consists in compressing the biogas which has been produced and conveyed at atmospheric pressure, this compression can be obtained - conventionally - via a lubricated screw compressor. The following stages aim to rid the biogas of the corrosive components that are hydrogen sulfide and volatile organic compounds (VOCs), the technologies used are conventionally pressure-modulated adsorption (PSA) and trapping on activated carbon. Then comes the step which consists in separating the carbon dioxide in order to have methane in fine at the purity required for its subsequent use.
    Carbon dioxide is a contaminant typically found in natural gas which it is common to have to remove. Various technologies are used for this depending on the situation; among these, membrane technology is particularly effective when the CO2 content is high; it is therefore particularly effective in separating the CO2 present in biogas, and in particular in landfill gas.
    The membrane gas separation processes used for the purification of a gas, whether they use one or more stages of membranes, must allow the production of a gas of the required quality, at a low cost, while minimizing the losses of the gas that we want to develop. Thus, in the case of the purification of biogas, the separation carried out is mainly a CH4 / CO2 separation, which should allow the production of a gas containing, depending on its use, more than 85% of CH4, preferably more than 95% of CO2, more preferably more than 97.5% of CH4, while minimizing the losses of CH4 in the waste gas and the cost of purification, the latter being for a large part linked to the electrical consumption of the gas compression device upstream of the membranes.
    We know the solution consisting in using a three-stage membrane system (FIG. 1), in which the permeate 4 of the 1st stage undergoes a second separation in the third stage of membranes, before being mixed with the permeate 5 of the 2nd stage, to be recycled. This three-stage system is used without recompression of the permeate from the 1st stage, the permeate from the 2nd stage and the residual from the 3rd stage are recycled at the entrance to the membrane system. This three-stage membrane system improves the methane yield compared to a two-stage membrane system.
    A key parameter of the 3-stage configuration is the pressure of the permeate of the first stage which is the supply pressure of the third stage. Suddenly two contradictory objectives oppose:
    1. The pressure must be minimized in order to increase the performance of the first stage;
    2. The pressure must be maximized in order to increase the performance of the third stage or to reduce the number of membrane modules to be installed.
    To demonstrate the influence of the pressure of the permeate of the first stage, FIG. 2 shows the evolution of the yield CH4 and the specific cost normalized as a function of the pressure of the permeate of the first stage.
    Figure 2 shows that the pressure minimization is more important if all the other parameters are kept.
    In order to benefit from maximum performance from the third stage, it would nevertheless be desirable to increase its supply pressure, as can be achieved using a mechanical compressor.
    A solution according to the invention is an installation for the treatment by membrane permeation of a feed gas flow 6 comprising at least methane and carbon dioxide to produce a gas flow 12 enriched in methane comprising:
    a first membrane separation unit 1 making it possible to receive the feed gas flow and to produce a first permeate 4 enriched in carbon dioxide and a first retentate 7 enriched in methane,
    a second membrane separation unit 2 making it possible to receive the first retentate 7 and to produce a second permeate 5 enriched in carbon dioxide and a second retentate 8 enriched in methane,
    - A gas-gas ejector 11 for increasing the pressure of the first permeate 4 to a pressure between 2 and 6 bar, more preferably between 3 and 4bar.
    a third membrane separation unit 3 making it possible to receive the first permeate 4 compressed in the ejector and to produce a third retentate 9 enriched in methane and a third permeate 10 enriched in CO2.
    Depending on the case, the installation according to the invention may have one or more of the following characteristics:
    - Said installation comprises a means of conveying a part B of the supply gas flow towards the gas-gas ejector and the gas-gas ejector is a gas-gas ejector using as engine gas part B of the gas flow feed,
    said installation comprises a compressor making it possible to increase the pressure of the supply gas flow to a pressure greater than 8 bar, more preferably greater than 13 bar upstream of the first membrane separation unit,
    said installation comprises a fourth membrane separation unit making it possible to receive the third permeate and to produce a fourth retentate enriched in methane and a fourth permeate enriched in CO2,
    said installation comprises means for jointly recycling the third retentate and the second permeate upstream of the compressor,
    said installation includes means for jointly recycling the fourth retentate and the second permeate upstream of the compressor,
    said installation comprises means for evacuating the third permeate outside the installation,
    said installation comprises means for evacuating the fourth retentate outside the installation,
    - the membranes of the three membrane separation units have the same selectivity or different selectivities.
    The present invention also relates to a method of treatment by membrane permeation of a feed gas flow 6 comprising at least methane and carbon dioxide to produce a gas flow 12 enriched in methane, implementing an installation such as defined in the invention and comprising:
    a) a first step of membrane separation of the feed gas flow in the first membrane separation unit 1 producing a first permeate 4 enriched in carbon dioxide and a first retentate 7 enriched in methane,
    b) a second step of membrane separation of the first retentate 7 in the second separation unit 2 by membrane producing a second permeate 5 enriched in carbon dioxide and a second retentate 8 enriched in methane,
    c) a step of compressing the first permeate 4 at a pressure of between 2 and 6 bar by means of the gas-gas ejector 11,
    d) a third step of membrane separation of the first permeate 4 compressed in the ejector 11 in the third membrane separation unit 3 producing a third retentate 9 enriched in methane and a third permeate 10 enriched in CO2.
    Depending on the case, the method according to the invention may have one or more of the characteristics below:
    - The gas-gas ejector 11 uses part B of the supply gas flow as the driving gas.
    - Upstream of the first membrane separation unit 1, the supply gas flow 6 is compressed to a pressure greater than 8 bar, more preferably greater than 13 bar.
    - Said method comprises a fourth step of membrane separation of the third permeate producing a fourth retentate enriched in methane and a fourth permeate enriched in CO2.
    - The third retentate 9 and the second permeate 5 are recycled together upstream of the compressor.
    - The fourth retentate and the second permeate are recycled together upstream of the compressor.
    In the context of the invention, the feed gas flow is preferably biogas from, for example, a digester, a fermenter, a waste reception center or WWTP (STEP = WWTP)
    The installation and the method according to the invention by increasing the pressure of the first permeate to a pressure between 2 and 6 bar, that is to say by carrying out a "slight" increase in pressure, allow either to decrease the surface membrane to be installed at the level of the third stage and as a result to reduce the investment costs while keeping the yield constant, ie to increase the performance of the installation / process according to the invention.
    Since the gas-gas ejector uses the gas flow from the first stage as the working gas, there is no risk of pollution. The ejector also has the advantage of having no moving parts.
    权利要求:
    Claims (15)
    [1" id="c-fr-0001]
    Claims
    1. Installation for the treatment by membrane permeation of a feed gas flow (6) comprising at least methane and carbon dioxide to produce a gas flow (12) enriched in methane comprising:
    - a first membrane separation unit (1) making it possible to receive the feed gas flow and to produce a first permeate (4) enriched in carbon dioxide and a first retentate (7) enriched in methane,
    - a second membrane separation unit (2) making it possible to receive the first retentate (7) and to produce a second permeate (5) enriched in carbon dioxide and a second retentate (8) enriched in methane,
    - A gas-gas ejector (11) for increasing the pressure of the first permeate (4) to a pressure between 2 and 6 bar, more preferably between 3 and 4bar.
    - a third membrane separation unit (3) making it possible to receive the first permeate (4) compressed in the ejector and to produce a third retentate (9) enriched in methane and a third permeate (10) enriched in CO2.
    [2" id="c-fr-0002]
    2. Installation according to claim 1, characterized in that said installation comprises a means for conveying a part B of the supply gas flow from the first membrane separation unit to the gas-gas ejector and the ejector gas-gas is an ejector using as engine gas part B of the supply gas flow.
    [3" id="c-fr-0003]
    3. Installation according to one of claims 1 or 2, characterized in that said installation comprises a compressor making it possible to increase the pressure of the supply gas flow to a pressure greater than 8bar, more preferably greater than 13bar upstream of the first membrane separation unit.
    [4" id="c-fr-0004]
    4. Installation according to claim 3, characterized in that said installation comprises a fourth membrane separation unit making it possible to receive the third permeate and to produce a fourth retentate enriched in methane and a fourth permeate enriched in CO2.
    [5" id="c-fr-0005]
    5. Installation according to claim 3, characterized in that said installation comprises means for jointly recycling the third retentate and the second permeate upstream of the compressor.
    [6" id="c-fr-0006]
    6. Installation according to claim 4, characterized in that said installation comprises means for jointly recycling the fourth retentate and the second permeate upstream of the compressor.
    [7" id="c-fr-0007]
    7. Installation according to claim 3, characterized in that said installation comprises means for evacuating the third permeate outside the installation.
    [8" id="c-fr-0008]
    8. Installation according to claim 4, characterized in that said installation comprises means for evacuating the fourth retentate outside the installation.
    [9" id="c-fr-0009]
    9. Installation according to one of claims 1 to 8, characterized in that the membranes of the three membrane separation units have the same selectivity or different selectivities.
    [10" id="c-fr-0010]
    10. A method of treatment by membrane permeation of a feed gas stream (6) comprising at least methane and carbon dioxide to produce a gas stream (12) enriched in methane, using an installation as defined in one of claims 1 to 9 and comprising:
    a) a first step of membrane separation of the feed gas flow in the first membrane separation unit (1) producing a first permeate (4) enriched in carbon dioxide and a first retentate (7) enriched in methane,
    b) a second step of membrane separation of the first retentate (7) in the second separation unit (2) by membrane producing a second permeate (5) enriched in carbon dioxide and a second retentate (8) enriched in methane,
    c) a step of compressing the first permeate (4) at a pressure of between 2 and 6 bar by means of the gas-gas ejector (11),
    d) a third stage of membrane separation of the first permeate (4) compressed in the ejector (11) in the third membrane separation unit (3) producing a
    5 third retentate (9) enriched in methane and a third permeate (10) enriched in CO2.
    [11" id="c-fr-0011]
    11. Method according to claim 10, characterized in that the gas-gas ejector (11) employs as engine gas a part B of the supply gas flow.
    10
    [12" id="c-fr-0012]
    12. Method according to one of claims 10 or 11, characterized in that upstream of the first membrane separation unit the gas flow (6) supply is compressed to a pressure greater than 8bar, more preferably greater than 13bar .
    [13" id="c-fr-0013]
    13. The method of claim 12, characterized in that said method comprises a
    Fourth stage of membrane separation of the third permeate producing a fourth retentate enriched in methane and a fourth permeate enriched in CO2.
    [14" id="c-fr-0014]
    14. Method according to claim 12, characterized in that the third retentate (9) and the second permeate (5) are recycled jointly upstream of the compressor.
    [15" id="c-fr-0015]
    15. The method of claim 13, characterized in that the fourth retentate and the second permeate are recycled together upstream of the compressor.
    1/3
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    法律状态:
    2018-03-23| PLFP| Fee payment|Year of fee payment: 2 |
    2018-09-07| PLSC| Search report ready|Effective date: 20180907 |
    2020-03-19| PLFP| Fee payment|Year of fee payment: 4 |
    2021-03-23| PLFP| Fee payment|Year of fee payment: 5 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1751688|2017-03-02|
    FR1751688A|FR3063437B1|2017-03-02|2017-03-02|APPARATUS AND METHOD FOR MEMBRANE PERMEATION TREATMENT OF A GAS SUPPLY FLOW COMPRISING METHANE AND CARBON DIOXIDE|FR1751688A| FR3063437B1|2017-03-02|2017-03-02|APPARATUS AND METHOD FOR MEMBRANE PERMEATION TREATMENT OF A GAS SUPPLY FLOW COMPRISING METHANE AND CARBON DIOXIDE|
    EP18156815.5A| EP3369473A1|2017-03-02|2018-02-14|Facility and method for treatment of a feed gas stream comprising methane and carbon dioxide by membrane permeation|
    CN201810170651.3A| CN108530251A|2017-03-02|2018-03-01|Device and method for gaseous feed stream of the film infiltration processing comprising methane and carbon dioxide|
    US15/910,241| US20180250627A1|2017-03-02|2018-03-02|Plant and method for the membrane permeation treatment of a gaseous feedstream comprising methane and carbon dioxide|
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