Apparatus and method for simultaneously treating different fluctuating gas streams - Patents.com

Abstract

The present invention relates to a novel apparatus and method for simultaneously separating multiple gas streams of differing composition using gas separation membranes, in which each gas stream fed to the apparatus and method may vary in their respective volumetric flow rates and compositions.

Description

[Technical field]

[0001] The present invention relates to a novel apparatus and method for simultaneously separating multiple gas streams of differing composition using gas separation membranes, in which each gas stream fed to the apparatus and method may vary in their respective volumetric flow rates and compositions. [Background technology]

[0002] It may be necessary to separate several gas streams with different and variable compositions simultaneously, for example in the case of ex-situ methanation of biogas or equivalent gases with hydrogen, where the hydrogen stream is only available in variable amounts. This is often the case for hydrogen from electrolysis powered by electricity from renewable energy sources such as wind. WO 2015 / 017875 describes a method for the simultaneous or alternating separation of biogas and product gas from methanation. The challenge of variable levels of reactant and product streams is solved by complex gas and liquid storage means.

[0003] An alternative approach for the treatment of different fluctuating gas streams with gas separation membranes is to provide separate separation units for the different gas streams or to mix the gas streams and feed them as a mixed stream to the separation unit. This means that the desired separation result cannot be achieved without significant added complexity. Furthermore, the fluctuations of the gas streams in terms of quantity or composition must be compensated for by interventions in the operating parameters such as pressure, temperature and membrane area, some of which are significant. Providing the corresponding excess capacity or gas storage means is costly.

[0004] Thus, for example, US Patent Application Publication No. 2020 / 0254383 discloses an apparatus for separating gas mixtures having only one supply gas conduit, which cannot efficiently process two different fluctuating gas streams with different compositions and volumetric flow rates without complex control and regulation techniques.

[0005] Therefore, there is a strong need for efficient apparatus and methods for simultaneously separating multiple gas streams of differing composition. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] International Publication No. 2015 / 017875 Brochure [Patent Document 2] US Patent Application Publication No. 2020 / 0254383 Summary of the Invention [Problem to be solved by the invention]

[0007] SUMMARY OF THE PRESENT EMBODIMENTS It is therefore an object of the present invention to provide a novel apparatus and a novel method which reduces the disadvantages, if any, of the prior art apparatus and methods.

[0008] A specific object of the present invention was to provide a novel device and a novel method by which the treatment of different fluctuating gas streams can be achieved in a very simple device or in a simple manner, preferably with as little excess capacity as possible in terms of membrane area and / or gas storage means and / or compressor power and / or temperature control and / or pressure control.

[0009] A more specific object of the present invention was to provide a novel apparatus and a novel method which do not require complex control and regulation techniques.

[0010] A more specific object of the present invention was to provide a novel apparatus and a novel method which are very flexible with regard to the use of the gas stream obtained after separation.

[0011] A more specific object of the present invention was to provide a novel device and a novel method suitable for using renewable energies that are only available in highly variable amounts, thereby contributing to combating climate change.

[0012] A more specific object of the present invention was to provide a novel apparatus and a novel method by which counter-varying gas streams can be brought to the desired target purity of each product stream at all possible operating points, possibly to a significant extent, using the most simplified equipment possible.

[0013] Further objects not expressly described will become apparent from the overall context of the following specification, claims, examples and drawings. [Means for solving the problem]

[0014] The inventors have surprisingly found that the stated object is achieved by an apparatus according to claim 1 and a method according to claim 16. Preferred embodiments are set out in the dependent claims.

[0015] The device and method according to the present invention are characterized by: two or more feed gas streams having different compositions are fed to a membrane separation stage; - the membrane separation stage comprises one membrane block or several membrane blocks; - the membrane block or the membrane blocks each contain a plurality of membrane separation units connected in parallel; - the feed gas stream is fed to a gas distributor at spatially separated locations such that two or preferably three or more membrane separation units are located between the connection points of the feed gas streams; It is.

[0016] To elaborate using the example of a membrane block fed with two feed gas streams 1 and 2, this means that one or more membrane separation units in the membrane block are fed with feed gas stream 1 having composition 1 by the gas distribution system according to the invention, and one or more further membrane separation units in the membrane block are fed with feed gas stream 2 having composition 2 by the gas distribution system according to the invention. Further membrane separation units in the membrane block, different from the aforementioned membrane separation units, can also be fed with a mixed gas stream comprising, preferably only comprising, a mixture of feed gas streams 1 and 2 by the gas distribution system according to the invention. Preferably, the minimum number of membrane separation units in the membrane block are fed with the mixed gas stream. More preferably, no membrane separation units in the membrane block are fed with the mixed gas stream. The maximum number of membrane separation units in the membrane block are fed with either feed stream 1 or feed stream 2.

[0017] The gas distribution system according to the invention can adjust or actively control or regulate the number of membrane separation units to which different gas streams are respectively fed. This adjustment is preferably performed via the volumetric or mass flow rate of each feed gas stream and / or via the inlet pressure of the feed gas streams relative to each other. This means, for example, that when the volumetric and / or mass flow rate and / or pressure of a feed gas stream is reduced, the feed gas stream is fed to fewer membrane separation units in each membrane block, while at the same time another feed gas stream is fed sequentially to more membrane separation units. If the control is performed by the pressure of the feed gas streams, the pressure difference range between the feed gas streams usable according to the invention is limited to the pressure difference resulting from the feeding of each feed gas stream to at least one membrane separation unit in the membrane block. This is because if the pressure difference becomes too large, the feed gas stream with the lower pressure may be completely rejected from the membrane separation stage.

[0018] The device according to the invention and the method according to the invention have the advantage that they react flexibly and quickly when contrary to the capacity requirements of the feed gas streams to be separated, and always make optimum use of the separation capacity of the separation stages and membrane blocks. A particularly great advantage of the device according to the invention and the method according to the invention is that control and regulation can be achieved without the need for large equipment and complex controls, such as a large number of automatic valves, and one feed gas stream can be treated more than another.

[0019] The gas distribution system according to the invention further has the advantage that it can be configured so that the gas streams to be purified can be fed to each membrane separation unit only with a low degree of mixing, if any. This allows the feed gas streams to be charged to the different membrane separation units and separated in their original or almost original composition. Such a system also has the advantage that the different feed gas streams can be treated very substantially separately in a single and identical installation.

[0020] When the individual membrane separation units are fed with different gas streams at their original or near original compositions, this results in permeate and retentate streams within the different membrane separation units that differ in composition and / or volumetric flow rates.

[0021] The apparatus according to the invention and the method according to the invention do not require complex additional equipment or significantly less or smaller additional equipment, such as buffer vessels and / or pressure tanks to mitigate the fluctuations of the different gas streams to be purified. They therefore provide considerable economic benefits. A special feature of the apparatus and method according to the invention is that these fluctuations are compensated for with a minimal level of equipment complexity, resulting in a constant product flow in terms of volumetric flow rate and / or composition.

[0022] For example, if there is a pressure drop of the first feed gas stream, within the limits permitted according to the invention with respect to the pressure difference with respect to the second feed gas stream, this will only affect the device according to the invention or the method according to the invention, in which this feed gas stream is fed to fewer membrane separation units and the second feed gas stream is fed to more membrane separation units in turn. The membrane separation units do not have to be operated at partial loading and the pressure of the permeate and retentate can be kept constant. In contrast, if the device is used as in the comparative example, i.e. the first feed gas stream is fed to the first membrane separation stage and the second feed gas stream is fed to the second membrane separation stage, a reduction in the pressure of the first feed gas stream will simultaneously reduce the pressure of the retentate gas stream of the first membrane separation stage, making it necessary to use a second compressor to recompress these retentate gas streams.

[0023] For example, if the volume of the first feed gas stream is reduced, this only affects the device according to the invention or the method according to the invention, in that this feed gas stream is fed to fewer membrane separation units and at the same time the second feed gas stream is fed to more membrane separation units. The membrane separation units do not have to be operated at partial filling and the pressure of the permeate and retentate can be kept constant. In contrast, if the device is used as in the comparative example, i.e. the first feed gas stream is fed to the first membrane separation stage and the second feed gas stream is fed to the second membrane separation stage, a reduction in the volume of the first feed gas stream makes it necessary to adjust the separation capacity of the first membrane separation stage. Possible measures include shutting down the membrane separation unit by means of a valve, adjusting the operating temperature, increasing the permeate pressure or reducing the retentate pressure. A reduction in the retentate pressure can be achieved with relatively little complexity, but a reduction in the pressure of the retentate gas stream often requires a second compressor or booster to recompress the retentate gas stream. This is because a constant pressure stream of retentate gas is often required to further utilize the retentate.

[0024] The device according to the invention and the method according to the invention are particularly advantageous for increasing the input of renewable energies, which are often only available in highly variable amounts, and therefore make an important contribution to climate change prevention.

[0025] Further advantages not expressly described will become apparent from the overall context of the following specification, claims, examples and drawings.

[0026] Individual features indicated and / or depicted below in relation to specific embodiments are not limited to these embodiments or in combination with other features of these embodiments, but can, where technically possible, be combined with all other variants even if they are not individually described in this document.

[0027] The same reference numbers in the individual figures and pictures of the drawings identify the same or similar components, or components that operate in the same or similar manner. The depictions in the drawings also illustrate features without reference numbers, regardless of whether such features are subsequently described. However, features included in this specification but not visible or depicted in the drawings will also be readily apparent to one of ordinary skill in the art.

[0028] The present invention relates to (a) a first feed gas conduit (7) adapted or designed to transport a first feed gas stream, and a second feed gas conduit (8) adapted or configured to transport a second feed gas stream having a composition different from that of the first feed gas stream; (b) a membrane separation stage comprising one or more membrane blocks (1); (c) Gas distributor and A gas mixture separation apparatus comprising: - each of said membrane blocks (1) comprises a plurality of membrane separation units (2) connected in parallel, - each of the membrane separation units (2) has a gas inlet (3) and a gas separation membrane, the gas mixture fed through the gas inlet (3) being separated by the gas separation membrane into a retentate gas stream and a permeate gas stream; each of said membrane separation units (2) has a retentate gas outlet (30) for the retentate gas stream and a permeate gas outlet (31) for the permeate gas stream; The retentate gas outlet (30) is preferably connected to a retentate gas conduit (9) or to one or two retentate gas outlets (30) of adjacent membrane separation units (2) of the same membrane block (1) by one or more retentate connecting conduits (32); The permeate gas outlet (31) is preferably connected to a permeate gas conduit (10) or to one or two permeate gas outlets (31) of adjacent membrane separation units (2) of the same membrane block (1) by one or more permeate connecting conduits (33); said gas distributor having a connecting conduit (18) and / or one or more distribution conduits (4), each of said connecting conduits (18) connects the gas inlets (3) of two adjacent membrane separation units (2) of the membrane block (1) to each other, preferably directly and immediately; Each of the distribution pipes (4) has a plurality of branch pipes (5) each connected to a gas inlet (3) of an individual membrane separation unit (2) of the membrane block (1) by a supply pipe (6); said branch pipe or pipes (5) may further comprise attachment means for a supply gas conduit, whereby by means of said branch pipe (5) a supply gas conduit and a supply conduit (6) may in each case be simultaneously connected to said respective distribution conduit (4), - if the membrane separation stage comprises several membrane blocks (1), said membrane separation stage has conduits, preferably conduits (19a, 19b, 20a, 20b), connecting the membrane blocks (1) of said membrane separation stages to one another, the first feed gas conduit (7), the second feed gas conduit (8) and, if necessary, further feed gas conduits are each independently and at a spatially separated position, preferably immediately and directly connected to a distribution conduit (4), or to a connecting conduit (18), or to a branch pipe (5), or to a conduit connecting, if present, the membrane blocks (1) of the membrane separation stage to one another, preferably to a conduit (19a, 19b, 20a or 20b), or to a gas inlet (3) of a membrane separation unit (2), the connection points being arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points of the first feed gas conduit (7) and the second feed gas conduit (8).

[0029] The number of branches (5) and / or gas inlets (3) between the connection points of the first feed gas conduit (7) and the second feed gas conduit (8) is preferably at least 3, more preferably at least 4, even more preferably at least 5, particularly preferably at least 7 and very particularly preferably at least 9. The upper limit may for example correspond to the number of membrane separation units per block, but may be further increased if there are several membrane blocks per membrane separation stage, as shown for example in Figures 4a and 5a.

[0030] If the membrane separation stage according to the invention is supplied by three or more feed gas conduits, the junctions of the feed gas conduits are preferably spatially arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located in each case between the junctions of two feed gas conduits, examples of which are shown in figures 4 to 9.

[0031] A "conduit" in the context of this specification is understood to mean a pipe conduit through which a gas stream flows.

[0032] In the context of this specification, "a conduit that is directly and immediately attached to another conduit" means that the moment the gas flow leaves the first of two conduits that are directly and immediately attached to each other, it enters the second conduit that is directly and immediately attached to each other, i.e., the gas flow does not have to pass through a third conduit between the first and second pipe conduits.

[0033] A membrane separation unit is essentially characterized by the presence of an industrially available port (gas inlet (3)) for feeding the gas stream to be separated, called feed or feed stream or feed gas stream, from the pressure side to the membrane material, an industrially available port for removing the so-called retentate or retentate gas or retentate gas stream or retentate stream from the gas pressure side, and an industrially available port for removing the gas(es) that have passed through the membrane material, called permeate or permeate gas or permeate gas stream or permeate stream. If the driving force is generated by a purge gas, there is a permeate side connection option for such a purge gas. It is preferred that the pressure side concentration, pressure and temperature profiles in each main flow direction are discontinuous and that the permeate is obtained in a common permeate space, for example a housing or permeate tube in each membrane separation unit, without intermediate steps.

[0034] A preferred membrane separation unit is the following embodiment. A. Gas separation module. B. Housing with one or more gas separation cartridges connected in series. In the case of an embodiment of the membrane separation unit with multiple gas separation cartridges connected in series, it is preferably configured as follows: the retentate gas outlet of each gas separation cartridge is directly connected by a gas conduit to the gas inlet of each downstream gas separation cartridge, and the permeate from all gas separation cartridges is obtained in a directly communicating gas space, e.g., a housing space, or the retentate gas outlet of each gas separation cartridge is connected by a communicating gas space, e.g., a housing space, to the gas inlet of each downstream gas separation cartridge, and each cartridge has a permeate collection pipe directly connected by a gas conduit to the permeate collection pipe of each downstream gas separation cartridge. C. Multiple Gas Separation Modules Connected in Series: With the retentate gas outlet of each gas separation module directly connected by a gas conduit to the gas inlet of each downstream gas separation module, the membrane separation unit is configured such that the permeates from all gas separation modules of the membrane separation unit are combined, e.g., by a permeate pipe of each membrane separation unit. D. A plurality of series-connected housings with one gas separation cartridge or a plurality of gas separation cartridges, where each individual housing is preferably configured as described for embodiment B, the series-connected housings are configured such that the retentate gas outlet of each housing is directly connected, in each case by a gas conduit, to the gas inlet of each downstream housing, and the membrane separation units are configured such that the permeates from all housings of the membrane separation units are combined, for example by a permeate pipe of each membrane separation unit.

[0035] Preferred gas separation cartridges and housings with one or more series-connected gas separation cartridges are disclosed in EP 3307424, the contents of which are incorporated herein by reference.

[0036] Gas separation modules differ from gas separation cartridges in that they constitute a complete separation unit, such as a pressure-resistant housing. In contrast, cartridges are used in a separate pressure-resistant housing, preferably in a housing that is fixedly installed in the separation device. In this case, not only one cartridge but also several cartridges connected in series in series can be used in the housing. Cartridges have the advantage of lower replacement costs compared to modules, since there is no need to replace expensive pressure-resistant housings.

[0037] Generally, in the field of biogas processing, cartridges or modules with small capacity are used, but in the field of natural gas purification, for example, cartridges or modules with large capacity are required, which can handle large amounts of gas. Furthermore, in this field of use, cartridges and modules are required that can be used at relatively high feed gas pressures, preferably between 30 and 100 bar.

[0038] Gas separation modules and cartridges can include flat membranes wrapped around, for example, a permeate pipe in a centralized arrangement.

[0039] Additionally, there are cartridges or modules that contain hollow fiber membranes, examples of which are US Pat. No. 3,422,008, US Pat. No. 3,455,460, US Pat. No. 3,475,331, US Pat. No. 4,207,192, US Pat. No. 4,210,536, US Pat. No. 4,220,489, US Pat. No. 4,430,219, US Pat. No. 4,631,128, US Pat. No. 4,715,953, US Pat. No. 4,865,736, US Pat. No. 4,881,955, US Pat. No. 5,081,956, US Pat. Nos. 4073, 5,160,042, 5,299,749, 5,411,66, 5,702,601, 5,837,032, 5,837,033, 5,897,729, 7,410,580, 7,998,254, 8,747,980, and 8,778,062, the contents of which are expressly incorporated herein by reference.

[0040] In principle, any membrane separation unit known to those skilled in the art can be used in the present invention.Preferred membrane separation units are described in US Patent Application Publication No. 2016 / 0151744, US Patent No. 10,933,378, US Patent Application Publication No. 2018 / 0221824.The contents of these publications are expressly incorporated into the contents of this specification.

[0041] The membrane separation stage according to the invention comprises one or more "membrane blocks", where each of the one or more membrane blocks comprises a number of parallel-connected membrane separation units. Each membrane block of the membrane separation stage according to the invention preferably comprises at least two, more preferably more than five, and most preferably more than ten membrane separation units. The number of membrane separation units per membrane block depends on the gas source, in particular the amount of gas to be treated. In the field of gas separation using membranes, the use of several hundred membrane separation units is possible.

[0042] The apparatus according to the invention further comprises a "gas distributor", which is preferably configured as follows: the feed gas streams are supplied by the gas distributor to the membrane block or to the membrane separation units of each membrane block such that the feed gas streams flow towards each other in conduits inside the membrane block and / or in one or more conduits interconnecting multiple membrane blocks of the membrane separation stage.

[0043] "Flowing towards" each other within a conduit includes the following embodiments (non-exhaustive list): - Two gas streams flow towards each other in a single and identical pipe. - two connecting conduits are attached to the gas inlets of the membrane separation units of the membrane block of the membrane separation stage according to the invention: the two feed gas streams flow towards each other through the two connecting conduits and join at the gas inlet. In a distribution conduit according to the invention with branches, the two feed gas streams flow towards each other and merge into each other between the two branches or in one branch. In a gas conduit according to the invention which connects several membrane blocks of a membrane separation stage to each other and thus has a branch pipe leading to each membrane block, the two feed gas streams flow towards each other and merge into each other between the two branches or in one branch pipe.

[0044] More preferably, the feed gas stream is supplied by a gas distributor to the membrane separation units of the or each membrane block as follows: gas streams of different composition are each supplied to at least two membrane separation units of a membrane block, more preferably to at least two membrane separation units of a plurality of membrane blocks of a membrane separation stage in each case, and most preferably to at least two membrane separation units of all membrane blocks of a membrane separation stage.

[0045] Therefore, in the two preferred embodiments described above, it is more preferred that the connection points of the first supply gas conduit (7) and the second supply gas conduit (8) are arranged spatially independently, as follows: the first and second feed gas streams flow towards each other in one or more membrane blocks (1) of the membrane separation stage, preferably in one or more distribution conduits (4) and / or in connecting conduits (18) and / or in conduits, preferably conduits (19a, 19b, 20a, 20b), connecting the membrane blocks (1) of the membrane separation stage to each other, and / or Gas streams with different compositions are each fed to at least two different membrane separation units (2) in one membrane block (1), preferably in multiple membrane blocks (1), and more preferably in all membrane blocks (1) of the membrane separation stage.

[0046] The gas distributor according to the invention is preferably configured such that the feed gas streams flow towards each other as described above, so that there are contact points in the device according to the invention where the feed gas streams fed to the gas distributor meet. At these contact points the feed gas streams may be mixed to some extent. Preferably, according to the invention, the mixing should be able to be significantly suppressed and / or regulated. This can be achieved by adapted auxiliary structural measures in the device according to the invention at the potential contact points. Preferred structural measures are the reduction of the conduit cross section and / or the enlargement of the conduit cross section and / or the introduction of static mixers and / or the use of pigs in the gas conduit. The pigs used can be passive pigs, i.e. pigs whose position in the gas conduit of the gas distributor is controlled depending on the properties of the feed gas streams, for example their pressure or volumetric flow rate, or actively controlled pigs, i.e. pigs whose position in the gas conduit of the gas distributor is fixed, for example by magnets, regardless of the properties of the feed streams. The use of passive pigs is preferred.

[0047] The permeate stream generated in the membrane separation unit of the membrane block is - thoroughly mixed to produce a permeate gas stream which is then removed and further treated or discarded; or partially combined, thereby producing multiple permeate gas streams which are then removed, further processed or separately disposed of, or partially combined, thereby producing one or more permeate gas streams which are then independently removed, further treated or discarded, and to some extent independently removed, further treated or discarded, or - Everything is removed, further processed or discarded separately.

[0048] It is preferred to mix the permeate gas streams so that the resulting number of permeate gas streams corresponds to the number of feed gas streams and the composition of the permeate gas streams is maximally different. More preferably, all permeate gas streams from the membrane separation units of a membrane block fed with the same feed gas stream are mixed. This results in maximal differences in the permeate gas streams, as shown in Example 1. If some membrane separation units in a membrane block are fed with mixed gas streams produced from different feed gas streams, the permeate streams obtained at these membranes are preferably divided, and each of the partial streams is mixed with one of the above-mentioned permeate gas streams obtained from the membrane separation units fed with pure feed gas streams, as shown in Example 2.

[0049] The procedure for the retentate flow can be similar. This gives the device and method according to the invention a very high flexibility in terms of the gas streams that can be obtained from a single system.

[0050] Preferred configurations of the device and method according to the invention, as well as the general basic principles according to the invention, are explained in detail below with reference to particular embodiments according to FIGS.

[0051] In a first preferred embodiment, the membrane separation stage according to the invention comprises one membrane block (1) or several membrane blocks (1), each of which has a distribution conduit (4) with several branches (5) and a feed conduit (6). The feed conduit (6) in each case connects the branches (5) to the gas inlet (3) of the membrane separation unit (2) and The first supply gas conduit (7) and the second supply gas conduit (8) are separately and independently connected to the distribution conduit (4) and / or the branch pipe (5), preferably at positions having a maximum distance from each other in terms of the flow path, more preferably to each end of the distribution conduit (4).

[0052] An example of this first preferred embodiment of the device or method according to the present invention is shown in FIG. 1. It comprises a plurality of parallel-connected membrane separation units (2 1 )~(2 n The index n corresponds to the serial number, and the number n corresponds to the number of parallel-connected membrane separation units in the membrane block (1), each of which has a gas inlet (3 1 )~(3 n ) Membrane separation unit (2 1 )~(2 n ) gas inlet (3 1 )~(3 n ) are connected to one another by a gas distributor according to the invention.

[0053] The gas distributor is - a distribution conduit (4) having a number of branches (5), - Each branch pipe (5) is connected to a membrane separation unit (2 1 )~(2 n ) gas inlet (3 1 )~(3 n ) supply conduit (6 1 )~(6 n ) Including, In FIG. 1, a first supply gas conduit (7) and a second supply gas conduit (8) are arranged to be connected separately to each end of the distribution conduit (4).

[0054] As a variant of Fig. 1, the first supply gas conduit (7) and / or the second supply gas conduit (8) may be separately connected to the distribution conduit (4) or the branch pipe (5) at different points. The connection points preferably have a maximum distance from each other in terms of the flow path. More preferably, the first supply gas conduit (7) and / or the second supply gas conduit (8) are each connected to one end of the distribution conduit (4).

[0055] When the method according to the invention is carried out in an apparatus according to Fig. 1, in the membrane block according to the invention (1) the first and second feed gas streams of different composition flow towards each other and join in the distribution conduit (4). Only at the point where the two gas streams join does mixing of the gas streams occur.

[0056] To explain the basic principles according to the present invention, consider the following example under simplifying assumptions. The main simplifying assumptions are: - All repeating device sections must be symmetrical and identical in structure. - The flow pressure drop through the two different feed gas streams is independent of density, viscosity and temperature. - The pressure side pressure drop of all membrane separation units is the same.

[0057] In this example, the two gas streams join in the center of the distribution conduit (4) at the same pressure and volumetric flow rate as the first and second feed gas streams. This is because the first feed gas stream is fed to the membrane separation unit (2 1 ) and (2 2 ) where it is separated into a permeate stream and a retentate stream. Similarly, the second feed gas stream is fed to a membrane separation unit (2 n-1 ) and (2 n ) where it is fed to a membrane separation unit (2 1 ) and (2 2) into a retentate and a permeate stream, the composition of which differs from the permeate and retentate streams produced in the membrane block (1). A further membrane separation unit, arranged in the middle of the membrane block (1), is optionally fed with a mixture of the first and second feed gas streams. If thereafter, for example the pressure or the volumetric flow rate of the first feed gas stream is reduced, the meeting point of the two feed gas streams in the distribution conduit (4) moves towards the end of the distribution conduit fed with the first feed gas stream. As a result, more membrane separation units are fed with the second feed gas stream and fewer membrane separation units are fed with the first feed gas stream.

[0058] Preferably, mixing of the feed gas streams at potential contact points is prevented or reduced to a desired extent by reducing the conduit cross section and / or by enlarging the conduit cross section of the distribution conduit (4) and / or by introducing static mixers and / or by using pigs between the different gas streams in the distribution conduit (4). The use of passive pigs is preferred.

[0059] In the method and apparatus according to FIG. 1 )~(2 n The retentate flow from the retentate gas pipeline (9 1 )~(9 n The retentate gas is supplied to the retentate gas recovery pipe (11) in the membrane separation unit (2). 1 At its first end, located near the membrane separation unit (2), a first retentate gas stream, mainly enriched in the retentate gas of the first feed gas stream, is obtained by a suitably adjusted withdrawal volume, which is fed to a first retentate gas discharge conduit (12). n At a second end of the retentate gas recovery pipe (11), located near the second feed gas stream, a second retentate gas stream is obtained that is primarily enriched in the retentate gas of the second feed gas stream, which is fed to a second retentate gas discharge conduit (13).

[0060] Similarly, the membrane separation unit (2 1 )~(2 n The permeate flow from the membrane block (1) is directed to the permeate gas conduit (10) in FIG. 1 )~(10 n The permeate gas is supplied to the permeate gas recovery pipe (14) in the membrane separation unit (21 At its first end, located near the membrane separation unit (2), a first permeate gas stream, mainly enriched in the permeate gas of the first feed gas stream, is obtained by a suitably adjusted withdrawal volume, which is fed to a first permeate gas discharge conduit (15). n At a second end of the permeate gas recovery pipe (14), located near the second feed gas stream, a second permeate gas stream mainly enriched in the permeate gas of the second feed gas stream is obtained, which is fed to a second permeate gas discharge conduit (16).

[0061] Similar to the method in the distribution conduit (4), supplementary measures can also be implemented in the retentate recovery pipe (11) at potential contact points of the retentate streams from the various membrane separation units, in particular at contact points where a retentate stream predominantly enriched in retentate gas of the first feed gas stream meets a retentate stream predominantly enriched in retentate gas of the second feed gas stream, in order to minimize or prevent mixing of the respective streams or to establish an adequate take-off capacity. Adaptation measures are reduction of the conduit cross section and / or enlargement of the conduit cross section and / or the use of pigging, preferably the use of actively controlled pigging.

[0062] Likewise, supplementary measures can be implemented in the retentate recovery pipe (11) at potential contact points of the permeate streams from the various membrane separation units, in particular at contact points where a permeate stream predominantly enriched in the permeate gas of the first feed gas stream meets a permeate stream predominantly enriched in the permeate gas of the second feed gas stream, in order to minimize or prevent mixing of the respective streams or to establish an adequate take-off capacity. Adaptation measures are a reduction in the conduit cross section and / or an increase in the conduit cross section and / or the use of pigs, preferably actively controlled pigs.

[0063] The adjustment of the take-off volume of the permeate or retentate stream can also be effected, for example, by suitable valves in the retentate gas conduit (9) and / or the permeate gas conduit (10) and / or the retentate gas recovery pipe (11) and / or the permeate recovery pipe (14) and / or the first retentate gas discharge conduit (12) and / or the second retentate gas discharge conduit (13) and / or the first permeate gas discharge conduit (15) and / or the second permeate gas discharge conduit (16) and / or in the embodiment according to FIG. 3 described further below the retentate connection conduit (32) and / or the permeate connection conduit (33). Preferably, for this purpose, valves are used in one permeate gas discharge conduit and in all retentate gas discharge conduits, or more preferably in all permeate gas discharge conduits and in all retentate gas discharge conduits, respectively. It is very particularly preferred for this purpose to use controllable valves in all permeate gas discharge conduits and in all retentate gas discharge conduits.

[0064] In a second preferred embodiment, the membrane separation stage according to the invention comprises one membrane block (1) or a number of membrane blocks, each of which has a number of connecting conduits (18) respectively connecting the gas inlet (3) of a membrane block membrane separation unit (2) to the gas inlet (3) of an adjacent membrane separation unit (2) within that membrane block (1); The first feed gas conduit (7) and the second feed gas conduit (8) are each separately and independently connected to a gas inlet (3) of the membrane separation unit (2) or to multiple gas inlets (3) of the membrane separation unit and / or to a connecting conduit (18) or to multiple connecting conduits (18).

[0065] An example of this second preferred embodiment of the device or method according to the present invention is shown in Figure 2. The membrane block (1) shown in Figure 2 is made up of a number of parallel-connected membrane separation units (2 1 )~(2 n The index n corresponds to the serial number, and the number n corresponds to the number of parallel-connected membrane separation units in the membrane block (1), each of which has a gas inlet (3 1 )~(3 n) Membrane separation unit (2 1 )~(2 n ) are connected to one another by a gas distributor according to the invention.

[0066] In the apparatus or method according to FIG. 2, the gas distributor connects the gas inlet (3) of the membrane separation unit (2) to the gas inlets (3) of both adjacent membrane separation units, respectively, and is arranged at both ends of the membrane block (1) to the gas inlets (3) of the membrane separation units (2). 1 ) and (2 n ), each has a connecting pipe (18) connected to the gas inlet (3) of the adjacent membrane separation unit. 1 ) and the supply gas conduit (8) is connected to the gas inlet (3 n ). From there, the first and second feed gas streams join each other through a connecting conduit (18) and are fed to a membrane separation unit (2 1 ) and (2 n ) is distributed to a membrane separation unit located between the

[0067] In terms of function, the membrane block of Fig. 2 corresponds to the membrane block of Fig. 1, with the difference that the branch pipe (5) of the device of Fig. 1 is integrated into the gas inlet (3) of Fig. 2. Preferably, in the embodiment of Fig. 2, the branch pipe (5), the feed conduit (6) and the gas inlet (3), which are implemented as separate components in Fig. 1, are constructed as part of the pressure housing of the respective membrane separation unit. The explanation of the basic principles of the invention for Fig. 1 is therefore equally applicable to the embodiment of Fig. 2.

[0068] The embodiment of FIG. 2 may be modified within the scope of the present invention. For example, the feed gas conduit (7) and / or the feed gas conduit (8) may be connected to a membrane separation unit (2 1 ) and (2 n ) gas inlet (3 1 ) and (3 n ), but instead, a gas inlet of a membrane separation unit disposed between them, e.g., a gas inlet (3 2 ) and / or (3 n-1) in which case the first supply gas flow is connected via one connecting conduit (18) to the gas inlet (3 2 ) to the membrane separation unit (2 1 ) gas inlet (3 1 ) and via another connecting conduit (18) to a membrane separation unit (2 3 ) gas inlet (3 3 ) in this embodiment. Thus, in each case, the first feed gas stream is sent to the membrane separation unit (2 1 ) and (2 2 ) will be separated.

[0069] A further inventive modification of the embodiment of FIG. 2 is configured as follows: the feed gas conduit (7) and / or the feed gas conduit (8) are connected to a membrane separation unit (2 1 ) and (2 n ) gas inlet (3 1 ) or (3 n ), rather one or both of the feed gas conduits are attached to a connecting conduit (18). For example, the feed gas conduit (7) may be connected to a membrane separation unit (2 1 ) and / or (2 1 ) in a connecting conduit (18) between the gas inlets of the

[0070] In order in any case to fill the individual membrane units with each feed stream as close as possible to its original composition, preferred according to the invention are those embodiments of the device and method which minimize the level of mixing of the feed streams. Therefore, at the potential contact points of the feed gas streams, it is preferred to prevent or reduce to the desired extent the mixing of the feed gas streams by reducing the conduit cross section of the connecting conduit (18) and / or by enlarging the conduit cross section of the connecting conduit (18) and / or by introducing static mixers and / or by using pigs between the different gas streams in the connecting conduit (18). The use of passive pigs is preferred.

[0071] The configuration of the retentate and permeate sides of the device according to the invention shown in FIG. 2, i.e. the further inventive processing of the retentate and permeate streams, takes place in a similar manner to the method described for FIG.

[0072] Further modifications will be apparent to those skilled in the art and to those applying the principles of the present invention.

[0073] Therefore, the device and method according to the invention more preferably comprises a membrane block (1) equipped with a gas distributor. The gas distributor in each membrane block (1) comprises a connecting conduit (18) connecting the gas inlet (3) of the membrane separation unit (2) to the gas inlet (3) of the adjacent membrane separation unit (2) in that membrane block (1), respectively. Each feed gas conduit is separately and independently connected to one gas inlet (3) of the membrane separation unit (2) or to multiple gas inlets (3) of the membrane separation unit (2) and / or to one connecting conduit (18) or to multiple connecting conduits (18). Preferably, via the connecting conduits, two feed gas streams are supplied to the individual membrane separation units, flowing towards each other.

[0074] Furthermore, it is advantageous and desirable to avoid excessively high pressure drops in the gas distributor. Finally, a very low equipment complexity and operating complexity is advantageous for the control and regulation of the system. The embodiments of figures 1 and 2 have all these advantages and are therefore particularly preferred.

[0075] In a further preferred embodiment according to the invention, the principle of combining the branch pipe (5) and the feed conduit (6), as explained above with the example of FIG. 2, is applied to the retentate treatment system and / or the permeate treatment system. Instead of connecting the retentate flow from the membrane separation unit (2) of the membrane block (1) via the retentate gas conduit (9) to the retentate gas recovery pipe (11) as shown in FIGS. 1 and 2, in this embodiment the retentate gas outlet (30) of the membrane separation unit (2) is connected by a retentate connecting conduit (32). The retentate gas discharge conduits (12) and (13) are attached to the retentate gas outlet (30) or to the retentate connecting conduit (32). Preferably, the retentate gas discharge conduit (12) is connected to the retentate gas outlet (30) or to the retentate connecting conduit (32). 1 ), or structurally attached to the retentate connection conduit at or near the retentate outlet, and the retentate discharge conduit (13) is connected to the retentate outlet (30 n ), or structurally attached to the retentate gas connection conduit at or near the retentate gas outlet. A corresponding embodiment in combination with the gas distribution system of Figure 2 is shown in Figure 3. Similarly, the retentate treatment system of Figure 3 may alternatively be combined with the gas distribution system of Figure 1.

[0076] As described above for the retentate treatment system, the permeate treatment system can be treated in a similar manner. Both the embodiment with the retentate and permeate collection pipes in the membrane block and the retentate and permeate connection conduits in the membrane block, and the embodiment with the retentate and permeate collection conduits in the membrane block and the retentate and permeate collection conduits in the membrane block are included in the present invention. Also, combinations of the embodiments, for example, where part of the retentate gas from the membrane block is fed to the retentate collection conduit and the other is removed via the retentate connection conduit, are included in the present invention and can be easily found by the skilled person. The same applies to the corresponding combinations for the permeate flow in the membrane block.

[0077] The above-described device according to the present invention and its preferred configurations can be scaled by increasing or decreasing the number "n" of parallel-connected membrane separation units (2) in a membrane block (1). It is therefore possible to adjust the separation capacity of each membrane block (1) and thus of each membrane separation stage without changing the membrane separation units themselves.

[0078] Alternatively or additionally, it is also possible to vary the membrane separation unit itself, for example by adjusting the membrane separation area and / or the membrane selectivity and / or the membrane permeability.

[0079] It is also possible to use different membranes in the membrane separation units (2) within one membrane block (1). Depending on the composition of the feed gas streams to be separated, it may be desirable to use a membrane optimized for a first feed gas stream in the membrane separation unit where only or mainly a first feed gas stream is separated, and to use a membrane optimized for the second feed gas stream in the membrane separation stage where only or mainly a second feed gas stream is separated.

[0080] Since the gas distributor according to the invention, as described above, controls the supply of the feed gas stream or mixtures thereof to the individual separation stages, preferably depending on the properties of the feed gas streams, e.g. depending on the current volumetric and / or mass flow rate and / or pressure of each feed gas stream, it may be the case that at some point during the operation of the apparatus or method, a membrane separation unit is supplied with a gas mixture having as main component the first feed gas stream and at a later point in time with a gas mixture mainly composed of the second feed gas stream. It is therefore preferred to use the same membranes in all membrane separation units (2) of a separation stage (1).

[0081] Alternatively or additionally, it is possible to adjust the capacity and selectivity of the membrane separation unit by the operating temperature. In a preferred embodiment, the feed gas stream has a different inlet temperature. The controlled adjustment of the operating temperature can be utilized, for example, to achieve a specified value for one or more retentate and / or permeate gas compositions, or for the yield of at least one gas component.

[0082] Further preferred embodiments for adjusting the separation capacity of the membrane separation stage according to the invention are shown in Figures 4 and 5. In the membrane separation stage, in each case, parallel-connected membrane blocks (1) are used. All membrane blocks described above can be used. The use of multiple parallel-connected membrane blocks rather than enlarging the membrane block itself, i.e., using four membrane blocks with 10 membrane separation units each instead of one block with 40 parallel-connected membrane separation units, offers advantages in terms of pressure control, especially the avoidance of pressure drops, and a simplified rack design.

[0083] FIG. 4 uses "o" membrane blocks (1) from FIG. 1 connected in parallel. The index (o) indicates the number of membrane blocks (1) connected in parallel. Each of these membrane blocks (1 1 )~(1 o ) are the distribution pipes (4 1 )~(4 o Each membrane block has a membrane separation unit (2 1 ) 1 )~(4 o ) are similarly connected to each other by gas conduits (19a), respectively. For the sake of simplicity, FIG. 4 merely shows the supply gas conduits (7 and (8), the distribution conduits (4 1 )~(4 o 4. Only the feed conduits (4) and branch pipes (5) are shown. Feed conduits (6) extend from each of the branch pipes (5) as shown in Figure 1 for the individual membrane separation units (2). The permeate and retentate treatment systems, also not shown in Figure 4, are preferably implemented as further described above, and more preferably as shown in any of Figures 1-3.

[0084] As shown in FIG. 4 in a non-exhaustive representation of the options represented by the interconnection of membrane blocks, the feed gas stream may be provided in a variety of ways.

[0085] FIG. 4a shows a first feed gas conduit (7) connected to a first membrane block (1 1) membrane separation unit (2 1 ) and a second supply gas conduit (19a) is connected to the last membrane block (1 o ) membrane separation unit (2 n 3 shows the interconnection and the manner in which the gas conduit (19b) is connected to the gas conduit (19b) going to the

[0086] FIG. 4b shows a first feed gas conduit (7) connected to a first membrane block (1 1 ) membrane separation unit (2 1 ) and a second supply gas conduit (8) is connected to a gas conduit (19a) leading to the first membrane block (1 1 ) membrane separation unit (2 n 3 shows the interconnection and the manner in which the gas conduit (19b) is connected to the gas conduit (19b) going to the

[0087] FIG. 4c shows a first feed gas conduit (7) leading to a membrane separation unit (2 1 ), and the second feed gas conduit (8) is connected to the opposite side, i.e. in each case to the membrane separation unit (2) between the two membrane blocks. n 3 shows an interconnection connected to a gas conduit (19b) disposed toward the

[0088] FIG. 4d shows a configuration in which the first supply gas conduit (7) is arranged in the middle of the distribution conduit (41) and the second supply gas conduit (8) is arranged opposite the distribution conduit (41). o ) is shown as an interconnect located in the center of the

[0089] In this preferred embodiment, the device according to the invention more preferably has the following features: - the membrane separation stage comprises a plurality of membrane blocks (1). the gas distributor comprises, for each membrane block (1), one distribution conduit (4) with a number of branches (5) and a supply conduit (6), in each case the supply conduit (6) connecting the branches (5) to the gas inlets (3) of the membrane separation units (2). the distribution conduits (4) of each membrane block (1) of the membrane separation stage are connected to one another by conduits (19a, 19b). the first supply gas conduit (7) and the second supply gas conduit (8) are independently connected to the distribution conduit (4) or the branch pipe (5) or the conduit (19a, 19b) at spatially separate locations, the connection points being arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8).

[0090] In FIG. 5, “o” membrane blocks from FIG. 2 connected in parallel are used. Each membrane block (1 1 )~(1 o ) membrane separation unit (2 1 ) membrane inlet (3 1 ) (shown by the dotted oval in FIG. 5) are connected to each other by a gas conduit (20a). 1 )~(1 o ) membrane inlet (3 n ) are likewise connected to each other by gas conduit (20b). For the sake of simplicity, FIG. 5 merely shows the feed gas conduits (7) and (8), the connecting conduit (18) and the gas inlet (3). The permeate and retentate treatment systems not shown in FIG. 5 are preferably implemented as further described above, and more preferably as shown in any of FIGS. 1 to 3.

[0091] The feed gas stream may be supplied in a variety of ways, as shown in FIG. 5 in a non-exhaustive representation of the options represented by the interconnections of the membrane blocks.

[0092] FIG. 5a shows a first feed gas conduit (7) connected to a first membrane block (1 1 ) membrane separation unit (2 1 ) and a second feed gas conduit (8) is connected to a distribution conduit (20a) leading to the first membrane block (1 o ) membrane separation unit (2 n 3 shows an interconnection connected to a distribution conduit (20b) leading to the

[0093] FIG. 5b shows a first feed gas conduit (7) connected to a first membrane block (1 1 ) membrane separation unit (2 1 ) and a second feed gas conduit (8) is connected to a distribution conduit (20a) leading to the first membrane block (1 1 ) membrane separation unit (2 n 3 shows an interconnection connected to a distribution conduit (20b) leading to the

[0094] FIG. 5c shows a schematic diagram in which the first feed gas conduit (7) is connected to a connecting conduit (20a) and the second feed gas conduit (8) is connected to the opposite side, i.e. in each case to a membrane separation unit (2) between two membrane blocks. n 3 shows an interconnect connected to a connecting conduit (20b) disposed toward the

[0095] FIG. 5d shows the first feed gas conduit (7) connected to the first membrane block (1 1 ) and a second supply gas conduit (8) is connected to the membrane block (1 o 1 shows the interconnection connected to the connecting conduit (18) of

[0096] In this preferred embodiment, the device according to the invention more preferably has the following features: - the membrane separation stage comprises a plurality of membrane blocks (1). - the gas distributor of each membrane block (1) comprises a connecting conduit (18) connecting the gas inlet (3) of the membrane separation unit (2) to the gas inlet (3) of the adjacent membrane separation unit (2) within that membrane block (1), respectively. - the membrane blocks (1) of the membrane separation stage are connected to each other by conduits (20a, 20b), the conduits (20a, 20b) in each membrane block being respectively connected to one or more connecting conduits (18) and / or to one or more gas inlets (3). Preferably, the conduit (20a) in each membrane block (1) is connected to a connecting conduit (18) or to a gas inlet (3) and the conduit (20b) in each membrane block is connected to another connecting conduit (18) or to another gas inlet (3). the first supply gas conduit (7) and the second supply gas conduit (8) are independently connected at spatially separate locations to one or more connecting conduits (18), or to one or more conduits (20a, 20b), or to one or more gas inlets (3), the connection points being arranged such that two or more gas inlets (3) are located between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8);

[0097] An inventive extension of the embodiment of FIG. 5 is shown in FIG. 6. Supplementary to FIG. 5, a membrane block (1 1 )~(1 o ) gas inlet (3 1 ) and (3 n ) are connected to each other by gas conduits (20a) and (20b), as well as to a membrane block (1 1 )~(1 o ) gas inlet (3 2 )~(3 n-1 ) are also connected to each other at the membrane separation unit level by further gas conduits (20) to form a "complete grid".

[0098] The gas separation apparatus according to the invention is not limited to the simultaneous separation of two feed gas streams of different composition: the principles according to the invention can also be extended to multiple feed gas streams.

[0099] The apparatus according to the invention preferably comprises one, two or three additional feed gas conduits 3(21), 4 and 5 adapted to transport one, two or three additional feed gas streams having a different composition than the first and second feed gas streams. The additional feed gas conduits 3(21), 4 and 5 are connected to a gas distributor such that gas streams 3(21), or 3(21) and 4, or 3(21), 4 and 5 can be fed to the membrane separation unit by the gas distributor.

[0100] In a first preferred embodiment, an additional supply gas conduit is attached to one or more distribution conduits (4), preferably between the connections of the supply gas conduits (7) and (8). An example of such a configuration with an additional third supply gas conduit (21) is shown in Figure 7a).

[0101] In the second and third preferred embodiments, the additional supply gas conduit is attached to one or more connecting conduits (18) and / or one or more gas inlets (3). The connection point is preferably arranged at a gas inlet (3) other than the one or more connecting conduits (18) and / or the gas inlet (3) to which the first supply gas conduit (7) and the second supply gas conduit (8) are attached. The gas inlet (3) is arranged between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8). More preferably, the additional supply gas conduit is attached to one or more gas inlets (3). 2 )~(3 n-1 ) or to a connecting conduit (18) located therebetween. Examples of such embodiments with an additional third supply gas conduit (21) are shown in figures 7b) and 7c).

[0102] In a further preferred embodiment, several membrane blocks (1) according to the invention, fitted with two feed gas conduits through which feed gases of different composition flow respectively, are connected to one another.

[0103] In a preferred embodiment, the membrane blocks may be linearly assembled, i.e., interconnected. Each membrane block (1 1 )~(1 o ) are supplied with two feed gas streams. o corresponds to the serial number of each membrane block. An example of such an apparatus is shown in FIG. 8. The feed gas conduits (7) and (8) run from the first membrane block (1 1 ) is connected to the distribution pipe (41) of the first membrane block (1 1 ) is the second membrane block (1 2 ) and the supply gas conduits (8) and (21) are connected to the second membrane block (1 2 ) distribution pipe (4 2) Such a system can be expanded as required for additional feed gas flow.

[0104] In another equally preferred embodiment, a plurality of membrane blocks (1 1 )~(1 o ) can be combined, i.e., interconnected, to form a ring circuit. In that case, each membrane block (1 1 )~(1 o ) are connected to two supply gas conduits. An example of such an arrangement is shown in FIG. 9. Three membrane blocks (1 1 ), (1 2 ) and (1 3 ) is a distribution pipe (4 1 ), (4 2 ) and (4 3 ) to form a circular circuit. 1 ) connects the supply gas pipes (7) and (8) and the distributor pipe (4 2 ) connects the supply gas pipes (7) and (21), and the distributor pipe (4 3 ) connects the supply gas conduits (8) and (21). Such a loop can be expanded by further membrane blocks according to the invention, forming, for example, four-fold or five-fold interconnections.

[0105] Likewise, the embodiments of Figures 7 to 9 can be combined with each other. For example, in the loop circuit of Figure 9, the fourth supply gas conduit is connected to a distribution conduit (4) between the connection points of the supply gas conduits (7) and (8). 1 ) can be supplied to

[0106] For the sake of simplicity, Figs. 7, 8 and 9 only show the supply gas conduits (7), (8) and (21) and the distribution conduit (4 1 )~(4 3) and the branch pipe (5) are shown. For the individual membrane separation units, a feed conduit extends from each branch pipe as shown in Figure 1. The permeate and retentate treatment systems, also not shown in Figures 7, 8 and 9, are preferably implemented as further described above, and more preferably as shown in any of Figures 1 to 3, and are connected to each other as well as the distribution conduits.

[0107] The embodiment of figures 8 and 9 can of course also be implemented with the membrane blocks of figures 2 and 3, i.e. for example with multiple connecting conduits (18) per membrane block. Corresponding configurations can be easily deduced by the skilled person from the above teachings according to the invention.

[0108] The apparatus and methods according to the invention, in all preferred embodiments as well as in the general embodiments described above, may include one or more valves or other control devices capable of controlling or influencing the gas supply to the individual gas inlets of the membrane separation unit in one or more distribution conduits and / or in one or more supply conduits and / or in one or more connecting conduits.

[0109] The apparatus may be controlled or configured, for example, by valves or other controls to switch one or more membrane separation units on or off when the amount of gas supplied to the supply gas conduit changes.

[0110] The valves used may be shut-off valves and / or needle valves. Alternatively, gas flow within the gas distribution system may be influenced and / or controlled by other regulators such as vacuum, for example an aperture plate.

[0111] In particular, in the embodiment with distribution and / or connecting conduits, the distribution system according to the invention can be almost completely self-regulating, without the use of controllable valves in the membrane blocks, for example via the volumetric and / or mass flow rates and / or pressures of the feed gas streams, due to the merging of the feed streams with one another. In comparison with gas distributors controlled purely by valves, the number of expensive controllable valves can be significantly reduced. Thus, the device according to the invention preferably comprises valves for controlling the gas flows only in the single device, and most preferably none of the distribution and / or supply and / or connecting conduits. However, in an equally preferred embodiment, the membrane separation unit comprises a simple manual valve for rapid separation of the defective membrane from the remaining membranes in case of damage.

[0112] The permeate and retentate streams obtained in the membrane blocks according to the present invention are preferably fed to the permeate and retentate treatment systems of each membrane block, respectively, as shown in Figures 1 to 3. The permeate and retentate treatment systems include retentate and / or permeate recovery pipes, as shown in Figures 1 and 2. Alternatively, they may include retentate and / or permeate connecting conduits between the retentate or permeate outlets of each membrane separation unit in each membrane block, as shown in Figure 3. A combined use, such as the use of a retentate connecting conduit and a permeate recovery tube, as shown in Figure 3, is also possible.

[0113] The retentate or permeate stream is fed to the outlet conduit via the retentate and / or permeate collection pipes and / or the retentate and / or permeate connecting conduits. In a first preferred embodiment, as shown in Figures 1 and 2, two points, preferably two points as far away from each other as possible, more preferably both ends of the collection pipe are connected to the outlet conduit. This allows the permeate or retentate stream, mainly containing the permeate or retentate gas of the first feed stream, to be fed to the membrane separation unit (2 1 The wastewater can be removed from the outlet conduit located near the membrane separation unit (2 n) can be used to remove the permeate or retentate streams that mainly contain the permeate or retentate gas of the second feed stream. The same technical effect can be achieved if a retentate or permeate connecting conduit is used instead of a retentate or permeate recovery pipe. In this case, the membrane separation unit (2 1 ) retentate gas outlet (30 1 ) to the retentate gas outlet of the membrane separation unit or to a connecting pipe, and n ) retentate gas outlet (30 n It is preferred that a second outlet conduit near the first outlet of the membrane separation unit is attached to the gas outlet or to a connecting conduit of the membrane separation unit. A corresponding similar configuration, for example for the permeate stream, can be easily implemented by a person skilled in the art.

[0114] The further discharge conduit can be, for example, in the middle of the retentate or permeate recovery pipe, or, if a retentate or permeate connecting conduit is used, in the connecting conduit or in the membrane separation unit (2), in order to obtain a permeate or retentate stream essentially comprising a mixture of the permeate or retentate gases of the first and second feed streams. 2 ) or (2 n ) in the gas outlet of the membrane block (1). Such further outflow conduits are preferably rather attached to the central region of the membrane block (1).

[0115] The adjustment of the take-off volume of the permeate or retentate stream can also be effected, for example, via suitable valves in the retentate gas conduit (9) and / or the permeate gas conduit (10) and / or the retentate recovery pipe (11) and / or the permeate recovery pipe (14) and / or the first retentate gas discharge conduit (12) and / or the second retentate gas discharge conduit (13) and / or the first permeate gas discharge conduit (15) and / or the second permeate gas discharge conduit (16) and / or in the embodiment of FIG. 3 the retentate connection conduit (32) and / or the permeate connection conduit (33). Preferably, for this purpose, valves are used in one permeate gas discharge conduit and in all retentate gas discharge conduits, or more preferably in all permeate gas discharge conduits and in all retentate gas discharge conduits, respectively. It is very particularly preferred to use controllable valves for this purpose in all permeate gas discharge conduits and in all retentate gas discharge conduits.

[0116] In another, equally preferred embodiment, it is also possible to connect the permeate or retentate collection pipes to the discharge conduit at only one point. In this case, all permeate or retentate streams join in the respective collection pipes and are in each case taken out of the system as a combined mixed stream. The same technical effect can also be achieved if a retentate or permeate connecting conduit is used instead of a retentate or permeate collection pipe. In this case, one outlet conduit is attached to a retentate or permeate connecting conduit or to the retentate or permeate outlet of the membrane separation unit in the membrane block. A person skilled in the art can easily implement a corresponding configuration. It is likewise possible to connect several retentate or permeate discharge conduits to form one conduit to achieve the same technical effect.

[0117] In yet another, equally preferred embodiment, the permeate and retentate collection pipes can each be connected to a discharge conduit at only one point. In this case, all permeate or retentate streams join in the respective collection pipes and are taken out of the system as a combined mixed stream. The same technical effect can be achieved if a retentate or permeate connecting conduit is used instead of a retentate or permeate collection pipe. In this case, one discharge conduit can be connected to a retentate or permeate connecting conduit or to a membrane separation unit (2 in a membrane block). 1 ) at the retentate or permeate outlet of the suction pipe. A person skilled in the art can easily implement a corresponding configuration. It is likewise possible to connect several retentate or permeate outlet conduits to form one conduit in order to achieve the same technical effect.

[0118] More preferably, in the apparatus and method according to the invention, The retentate streams, preferably all of the retentate streams, from the membrane separation units (2) in the membrane block (1) are fed by means of a retentate gas conduit (9) to a retentate gas recovery pipe (11) which is connected to at least one first retentate gas discharge conduit (12), preferably to at least two retentate gas discharge conduits (12) and (13), through which one or more retentate gas streams are removed from the membrane separation stage where they were generated; and / or The permeate streams, preferably all of the permeate streams, from the membrane separation units (2) in the membrane block (1) are fed by means of a permeate gas conduit (10) to a permeate gas recovery pipe (14) which is connected to at least one first permeate gas discharge conduit (15), preferably to at least two permeate gas discharge conduits (15) and (16), through which one or more permeate gas streams are removed from the membrane separation stage where they were generated.

[0119] Equally more preferably, in the device and method according to the invention, the retentate streams, preferably all retentate streams, from the membrane separation units in the membrane block are fed to one or more retentate outlets by means of retentate connecting conduits between the retentate gas outlets, through which one or more retentate gas streams are removed from the membrane block. In this case, the device has a retentate connecting conduit (32) between the retentate gas outlets (30) of the membrane separation units (2) of the membrane block (1) of the membrane separation stage, in which at least one retentate connecting conduit (32) or at least one retentate gas outlet (30) is additionally connected to at least one retentate gas discharge conduit (12). Preferably, one or more retentate connecting conduits (32) and / or one or more retentate gas outlets (30) are connected to two retentate gas discharge conduits (12) and (13) in the membrane block (1) of the membrane separation stage. And / or

[0120] The permeate streams from the membrane separation units of the membrane block, preferably all permeate streams, are fed to one or more permeate outlet conduits by means of permeate connecting conduits between the permeate gas outlets, through which one or more permeate gas streams are removed from the membrane block. In this case, the device has a permeate connecting conduit (33) between the permeate gas outlets (31) of the membrane separation units (2) of the membrane block (1) of the membrane separation stage, where at least one permeate connecting conduit (33) or at least one permeate gas outlet (31) is connected to at least one permeate gas discharge conduit (15). Preferably, one or more permeate connecting conduits (33) and / or one or more permeate gas outlets (31) are connected to two permeate gas discharge conduits (15) and (16) in the membrane block (1) of the membrane separation stage.

[0121] When a membrane separation stage having several membrane blocks is used in the device according to the invention or in the method according to the invention, the permeate and retentate streams from each membrane block of the membrane separation stage are preferably combined to produce one or two permeate streams or one or two retentate streams per membrane separation stage. It is preferred to combine all the first retentate streams obtained at the first retentate gas discharge conduits (12) of each membrane block (1) to produce the first retentate stream from the membrane separation stage.

[0122] If in the membrane blocks (1) a second retentate stream is also obtained in the second retentate gas discharge conduit (13) from each membrane block (1), these second retentate streams are preferably combined to produce a second retentate stream from the membrane separation stage. It is possible to proceed similarly if further retentate streams are obtained within each membrane block.

[0123] As described above for the retentate stream, it is preferred to similarly proceed the permeate stream from each membrane block (1) of the membrane separation stage.

[0124] The permeate and retentate streams obtained from the membrane separation stage according to the invention may be removed as product streams, further processed or discarded, although at least one permeate and / or retentate stream is removed as a product stream or further processed. More preferably, at least two permeate streams or at least two retentate streams are produced in each membrane separation stage, at least one of which is removed as a product stream or further processed.

[0125] The device according to the invention may comprise one membrane separation stage according to the invention or several interconnected membrane separation stages, however, at least one membrane separation stage according to the invention is used together with the gas distributor according to the invention as follows: At least one membrane separation stage according to the invention comprises one membrane block (1) or several membrane blocks (1), each membrane block comprising several membrane separation units (2) connected in parallel. The gas distributor according to the invention is constructed as follows: The gas distributor according to the invention has one or more distribution conduits (3) including a connecting conduit (18) directly and immediately connecting the gas inlets (3) of two adjacent membrane separation units (2) in the membrane block (1) to each other, respectively, and / or one or more branch pipes (5) each connected to the gas inlets (3) of the membrane separation units (2) in the membrane block (1) by a separate supply conduit (6). The branch pipe or pipes (5) may additionally also have a connection means for a feed gas conduit, so that by means of the branch pipe (5) a feed gas conduit and a feed conduit (6) can be simultaneously connected to each distribution conduit (4). If the membrane separation stage comprises several membrane blocks (1), the membrane separation stage has conduits, preferably conduits (19a, 19b, 20a, 20b), connecting the membrane blocks (1) of the membrane separation stage to one another. The first supply gas conduit (7) and the second supply gas conduit (8) are each independently connected at a spatially separate location to the distribution conduit (4), or to the connecting conduit (18), or to the branch pipe (5), or to a conduit, if present, preferably to the conduit (19a, 19b, 20a or 20b), or to a gas inlet (3), the connection points being arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8).

[0126] The present invention also encompasses embodiments in which multiple membrane separation stages according to the present invention are interconnected.

[0127] For example, FIG. 10 shows a two-stage interconnection in which two membrane separation stages A and B of the invention are interconnected on the retentate side. In the apparatus of FIG. 10, two feed gas streams with different compositions are fed by the feed gas conduits (7) and (8) of the first membrane separation stage A. The first membrane separation stage A is preferably constructed as shown in FIG. 1 and further described above. The two permeate streams obtained from the permeate recovery pipe of the first membrane separation stage A are independently taken off as product streams, further processed or discarded by the permeate gas discharge conduits (15) and (16). The two permeate streams may be treated in the same way or independently treated in different ways. The two retentate streams obtained from the retentate recovery pipe of the first membrane separation stage A are fed as new feed streams to the membrane separation stage B by the retentate gas discharge conduits (12) and (13). As described in FIG. 1, the two retentate streams obtained from the retentate recovery pipe of the first membrane separation stage differ in their compositions. The retentate stream removed in retentate gas discharge conduit (12) contains primarily the retentate gas of the first feed stream, and the second retentate stream removed in retentate gas discharge conduit (13) contains primarily the retentate gas of the second feed stream. The retentate gases in the two retentate streams may be the same or different. Even if they are the same, the two retentate gas streams differ in content, i.e., in their quantitative composition.

[0128] Since the two retentate streams from membrane separation stage A differ in composition, the same prerequisites as for membrane separation stage A also apply to the second membrane separation stage B. That is, membrane separation stage B is fed with two feed gas streams, the second feed gas stream being different in composition from the first feed gas stream. Membrane separation stage B is preferably constructed as shown in FIG. 1. The two permeate streams obtained from the permeate recovery pipes of the second membrane separation stage B are recycled to the feed gas conduits (7) and (8) by means of the permeate gas discharge conduits (22) and (23). The two retentate streams obtained from the retentate recovery pipes of the second membrane separation stage B are independently removed as product streams, further processed or discarded by means of the retentate gas discharge conduits (24) and (25).

[0129] The operation of the membrane separation unit requires a partial pressure difference and therefore generally a pressure difference between the retentate and the permeate side. The pressure of the retentate side must be higher than the permeate side. This can be ensured, for example, by generating a high-pressure feed gas stream with a compressor or by depressurizing the permeate side of the membrane, for example by a vacuum pump. Corresponding techniques are known to the skilled person. What this means with respect to the interconnection in FIG. 10 is that the pressure in the permeate gas discharge conduits (22) and (23) is generally lower than the pressure in the feed gas conduits (7) and (8). The recycled permeate stream must therefore be brought to the pressure of the feed stream in the feed gas conduits (7) and (8) in the compression units P1 and P2. The compression units P1 and P2 may be of the same or different configuration. For example, it is possible to use a compressor in one or both of the permeate gas discharge conduits (22) and / or (23). This configuration is preferably selected when one or both of the raw gas streams, not shown in FIG. 10, are already under sufficient pressure.

[0130] Alternatively, one or both of the permeate gas streams recycled in the permeate gas discharge conduits (22) and (23) in the compression units P1 and P2 may be fed to one of the crude gas streams, not shown in Figure 10, respectively. The resulting mixed stream or the two resulting mixed streams may be condensed so that a feed stream or two feed streams are produced in the feed gas conduits (7) and / or (8).

[0131] In yet another alternative, one or both of the permeate streams recycled in the permeate gas discharge conduits (22) and (23) in the compression units P1 and P2 may be fed directly to a compressor that produces one of the two feed streams in the feed gas conduits (7) and (8).

[0132] The two latter alternatives are preferably used when the pressure of the crude gas stream is lower than the pressure of the feed stream.

[0133] Alternatively or additionally, the partial pressure difference may be created or increased by a purge gas flow on the permeate side, a procedure also known to those skilled in the art.

[0134] Devices for increasing the pressure in the permeate gas exhaust conduits (15) and (16) and / or (22) and (23) are recommended to increase the driving force, but are less preferred because of the complexity of the device.

[0135] Alternatively, but equally preferably, it is also possible to configure one or both of the membrane separation stages A and / or B of FIG. 10 as shown in particular in FIG. 2 or FIG. 3, as in other preferred embodiments discussed further above.

[0136] The interconnections of Figure 10 may be modified in a variety of ways, including, for example: - the permeate stream obtained from membrane separation stage B can be taken off independently as a product stream, further processed or discarded, provided that at least one of the two permeate streams from membrane separation stage A or B, or the retentate stream from membrane separation stage B, is taken off as a product stream or further processed. - one, preferably both, of the permeate streams obtained from membrane separation stage B are recycled to the respective original feed stream from membrane separation stage A, provided that at least one of the two permeate streams from membrane separation stage A or the retentate stream from membrane separation stage B is removed as a product stream, while the retentate stream obtained from membrane separation stage B is removed independently as a product stream and either further processed or discarded. - Both permeate streams obtained from membrane separation stage A are fed as feed streams to a second membrane separation stage B, and the two retentate streams obtained from membrane separation stage A are independently removed as product streams, further processed or discarded.

[0137] Those skilled in the art can easily identify further variations of the two-stage interconnection in light of the teachings of the present invention.

[0138] Therefore, more preferably, the device according to the invention and the method according to the invention are characterized in that: - comprising two membrane separation stages A and B, each of the two membrane separation stages A and B comprising one membrane block (1) or a plurality of membrane blocks (1) each comprising a plurality of membrane separation units (2) connected in parallel. the gas distributor of the first membrane separation stage A is configured as follows: in each membrane block (1) of the membrane separation stage A, a first feed gas conduit (7) and a second feed gas conduit (8) are connected to the gas inlets (3) of the membrane separation units (2) of the membrane separation stage A such that gas streams with different compositions are supplied to at least two different membrane separation units (2) of the membrane separation stage A. the first membrane separation stage A is configured such that two different retentate streams are obtained in the first retentate gas discharge conduit (12) and the second retentate gas discharge conduit (13) and / or two different permeate streams are obtained in the first permeate gas discharge conduit (15) and the second permeate gas discharge conduit (16). - the two retentate or the two permeate streams from the first membrane separation stage A are fed as feed streams to a second membrane separation stage B. - the gas distributor of the second membrane separation stage B is configured as follows: in each membrane block (1) of the membrane separation stage B, a first retentate gas discharge conduit (12) and a second retentate gas discharge conduit (13), or a first permeate gas discharge conduit (15) and a second permeate gas discharge conduit (16), are connected to the gas inlets (3) of the membrane separation units (2) of the second membrane separation stage B so that gas streams with different compositions are supplied to at least two different membrane separation units (2).

[0139] More preferably, the second membrane separation stage B is configured such that two distinct retentate streams are obtained in the first retentate gas discharge conduit (24) and the second retentate gas discharge conduit (25) and / or two distinct permeate streams are obtained in the first permeate gas discharge conduit (22) and the second permeate gas discharge conduit (23).

[0140] 11 shows a three-stage interconnection as a further particularly preferred embodiment according to the invention, in which three membrane separation stages according to the invention are interconnected such that two retentate streams from membrane separation stage A are fed as feed streams to membrane separation stage B, and two permeate streams from membrane separation stage A are fed as feed streams to membrane separation stage C.

[0141] In this case, two feed gas streams with different compositions are fed by the feed gas conduits (7) and (8) of the first membrane separation stage A, preferably configured as shown in FIG. 1. The two permeate streams obtained from the permeate collection pipe of the first membrane separation stage A are fed as new feed gas streams to the membrane separation stage C by the permeate gas discharge conduits (15) and (16). The two retentate streams obtained from the retentate collection pipe of the first membrane separation stage A are fed as new feed gas streams to the membrane separation stage B by the retentate gas discharge conduits (12) and (13). As explained above with respect to FIG. 1 and FIG. 10, the two retentate gas streams obtained from the first membrane separation stage A differ in their composition. The same applies to the permeate gas streams obtained from the first membrane separation stage A.

[0142] Since the two retentate streams from membrane separation stage A differ in composition, the same prerequisites as for membrane separation stage A also apply to the second membrane separation stage B. That is, membrane separation stage B is fed with two feed gas streams, the second feed gas stream being different in composition from the first feed gas stream. Membrane separation stage B is preferably structured as shown in FIG. 1. The two retentate streams obtained from the retentate recovery pipes of the second membrane separation stage B are independently removed as product streams, further processed or discarded by the retentate gas discharge conduits (24) and (25). The two permeate streams obtained from the permeate recovery pipes of the second membrane separation stage B are recycled to the feed gas conduits (7) and (8) by the permeate gas discharge conduits (22) and (23).

[0143] The same prerequisites as for membrane separation stage A apply to the third membrane separation stage C, since the two permeate streams from membrane separation stage A differ in composition. That is, the third membrane separation stage C is fed with two feed gas streams, the second feed gas stream being different in composition from the first feed gas stream. Membrane separation stage C is likewise structured as shown in FIG. 1. The two permeate streams obtained from the permeate recovery pipes of the third membrane separation stage C are independently removed as product streams, further processed or discarded, by the permeate gas discharge conduits (26) and (27). The two retentate streams obtained from the retentate recovery pipes of the third membrane separation stage C are recycled to the feed gas conduits (7) and (8) by the retentate gas discharge conduits (28) and (29).

[0144] Alternatively, but equally preferably, it is also possible to configure one, two or all three membrane separation stages A, B and / or C of FIG. 11 as in the other preferred embodiments discussed further above, and in particular as shown in FIG. 2 or FIG. 3.

[0145] In the case of the interconnection according to Fig. 11, the same applies as in Fig. 10: the pressure in the permeate gas discharge conduits (22) and (23) and in the retentate gas discharge conduits (28) and (29) is lower than the pressure in the feed gas conduits (7) and (8). The recycle gas stream must therefore be brought to the pressure of the feed gas stream in the feed gas conduits (7) and (8) in the compression units P1 and P2. The compression units P1 and P2 may be of the same or different construction.

[0146] Thus, the permeate gas discharge conduit (22) is preferably connected to a retentate gas discharge conduit (28) and is fed via a further gas conduit to the compression unit P1. The permeate gas discharge conduit (23) is preferably connected to a retentate gas discharge conduit (29) and is fed via a further gas conduit to the compression unit P2.

[0147] The compressors may be located in one or both of the gas conduits supplying compression units P1 and P2. This configuration is preferably selected when one or both of the crude gas streams, not shown in Figure 11, are already under sufficient pressure.

[0148] Alternatively, in compression units P1 and P2, one or both of the gas streams recirculated in the gas conduits feeding compression units P1 and P2, respectively, may be fed to one of the raw gas streams not shown in Figure 11. The resulting mixed stream or streams may be condensed, thus generating one or more feed streams in feed gas conduits (7) and / or (8).

[0149] In yet another alternative, one or both of the gas streams recirculated in the gas conduits supplying compression units P1 and P2 may be supplied directly to a compressor in compression units P1 and P2 which generates one of the two feed gas streams or feed streams in feed gas conduits (7) and / or (8).

[0150] The latter two alternatives are preferably used when the pressure of the crude gas stream is lower than the pressure of the feed stream.

[0151] Alternatively, the partial pressure difference may be created by a purge gas on the permeate side, a procedure also known to those skilled in the art.

[0152] Devices for increasing the pressure in the permeate gas exhaust conduits (15) and (16), and / or (22) and (23), and / or (26) and (27) are recommended to increase the driving force, but are not preferred due to the complexity of the device.

[0153] Those skilled in the art can easily identify further variations of the three-stage interconnection in light of the teachings of the present invention.

[0154] Therefore, more preferably, the device according to the invention and the method according to the invention are characterized in that: - comprising three membrane separation stages A, B and C, all three membrane separation stages A, B and C each comprising one membrane block (1) or a plurality of membrane blocks (1) comprising a plurality of membrane separation units (2) connected in parallel. - the gas distributor of the first membrane separation stage A is configured as follows: it connects a first feed gas conduit (7) and a second feed gas conduit (8) to the gas inlets (3) of the membrane separation units (2) of the first membrane separation stage A in such a way that in each membrane block (1) of the membrane separation stage A, at least two different membrane separation units (2) are supplied with gas streams of different composition. the first membrane separation stage A is configured such that two different retentate streams are obtained in the first retentate gas discharge conduit (12) and in the second retentate gas discharge conduit (13) and two different permeate streams are obtained in the first permeate gas discharge conduit (15) and in the second permeate gas discharge conduit (16). the two retentate streams from the first membrane separation stage A are fed as feed streams to a second membrane separation stage B, in which the retentate gas discharge conduits (12) and (13) are connected to a gas distributor of the second membrane separation stage B. the two permeate streams from the first membrane separation stage A are fed as feed streams to a third membrane separation stage C, in which the permeate gas discharge conduits (15) and (16) are connected to a gas distributor of the third membrane separation stage C. the gas distributor of the second membrane separation stage B is configured as follows: a first retentate gas discharge conduit (12) and a second retentate gas discharge conduit (13) are connected to the gas inlets (3) of the membrane separation units (2) of the second membrane separation stage B in such a way that in each membrane block (1) of the second membrane separation stage B, at least two different membrane separation units (2) are supplied with gas streams of different composition. - the gas distributor of the third membrane separation stage C is configured as follows: in each membrane block (1) of the third membrane separation stage C, a first permeate gas discharge conduit (15) and a second permeate gas discharge conduit (16) are connected to the gas inlets (3) of the membrane separation units (2) of the third membrane separation stage C in such a way that gas streams of different composition are supplied to at least two different membrane separation units (2).

[0155] More preferably, the second membrane separation stage B is configured such that two different retentate streams are obtained in the first retentate gas discharge conduit (24) and the second retentate gas discharge conduit (25) and / or two different permeate streams are obtained in the first permeate gas discharge conduit (22) and the second permeate gas discharge conduit (23), and / or the third membrane separation stage C is configured such that two different retentate streams are obtained in the first retentate gas discharge conduit (28) and the second retentate gas discharge conduit (29) and / or two different permeate streams are obtained in the first permeate gas discharge conduit (26) and the second permeate gas discharge conduit (27).

[0156] As shown above by way of example with two-stage and three-stage interconnections, membrane separation stages constructed according to the invention can be combined to form any kind of multi-stage interconnection, more preferably with two-stage, three-stage, four-stage and five-stage interconnections, most preferably with two-stage, three-stage and four-stage interconnections. For "conventional" membrane separation stages, where only one gas stream is fed for separation, corresponding interconnections are known to those skilled in the art. In the context of the present invention, three-stage interconnections are most preferred.

[0157] In an apparatus according to the invention, a membrane separation stage according to the invention for separating at least two different feed gas streams may be combined with a "conventional" membrane separation stage for separating only one gas stream into a permeate and a retentate stream. For example, a conventional membrane separation stage may be used upstream to produce one or more feed gas streams.

[0158] Alternatively, it is also possible to use a conventional membrane separation stage downstream of the membrane separation stage according to the invention. For example, one of the permeate and / or retentate streams obtained from the membrane separation stage according to the invention can be fed to such a conventional membrane separation stage. Furthermore, as already explained above, it is possible to configure the membrane separation stage according to the invention in such a way that in each case only one permeate and / or one retentate stream is obtained. These permeate or retentate streams can then be further processed in a conventional membrane separation stage.

[0159] As already mentioned for the particular embodiment according to Fig. 10 and Fig. 11, the membrane separation stages included in the device according to the invention and in the method according to the invention require a partial pressure difference between the retentate and the permeate side of the membrane. Therefore, for all embodiments of the invention, it is preferred to use a compressor in the feed gas conduit and / or a vacuum pump on the permeate side of the membrane, if the feed gas stream from each membrane separation stage does not have an appropriate partial pressure difference with the permeate side of the membrane separation stage. It is also preferred, as an alternative or in combination, to feed a purge gas into the permeate space to increase the partial pressure difference. This is known to the skilled person under the term "sweep". It is particularly preferred to use a compressor only in the feed stream or streams upstream of the first separation stage according to the invention.

[0160] The invention encompasses a method for simultaneously purifying two or more gas streams of different composition, as already indicated above. The method according to the invention is carried out in an apparatus according to the invention.

[0161] More preferably, the method according to the invention comprises the steps of: (i) providing a first feed gas stream; (ii) providing a second feed gas stream having a different composition than the first feed gas stream; (iii) feeding the first and second feed gas streams to a membrane separation stage; The membrane separation stage has one membrane separation block (1) or a plurality of membrane separation blocks (1), each of which has a plurality of membrane separation units (2) connected in parallel; the membrane separation stage has a gas distributor including a connecting conduit (18) and / or a distribution conduit (4), Each of the connecting conduits (18) connects the gas inlets (3) of two adjacent membrane separation units (2) of the membrane block (1) to each other, preferably directly and immediately; The distribution conduit (4) includes a plurality of branch pipes (5) each connected to a gas inlet (3) of each membrane separation unit (2) of the membrane block (1) by a separate supply conduit (6); The branch pipe or pipes (5) may further comprise attachment means for a supply gas conduit, whereby the supply gas conduit and the supply conduit (6) may be simultaneously connected to the distribution conduit (4) by means of the branch pipe (5); if the membrane separation stage comprises a plurality of membrane blocks (1), the membrane separation stage has conduits, preferably conduits (19a, 19b, 20a, 20b), which connect the membrane blocks (1) of the membrane separation stage to one another, and the first and second feed gas streams are each connected independently and at a spatially separated position to a distribution conduit (4), or to a connecting conduit (18), or to a branching conduit (5), or to a conduit connecting the membrane blocks (1) of the membrane separation stage, if present, to one another, preferably to conduits (19a, 19b, 20a, 20b), or to a gas inlet (3); the junction of the first and second feed gas streams is arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between said junction points; (iv) supplying the first and second feed gas streams by a gas distributor to a gas inlet (3) of a membrane separation unit (2) of a membrane separation stage; (v) Separating the gas mixture fed to the membrane separation unit (2) through the gas inlet (3) into a retentate gas stream and a permeate gas stream in each case by means of a gas separation membrane in the membrane separation unit (2).

[0162] More preferably, the method of the present invention further comprises the steps of: (vi) combining, preferably all, the retentate streams from the membrane separation units (2) of the membrane block (1) to produce one or more retentate gas streams; and / or (vii) preferably combining all of the permeate streams from the membrane separation units (2) of the membrane block (1) to produce one or more permeate gas streams.

[0163] Mixing of the permeate and / or retentate streams can be preferably achieved by permeate and / or retentate recovery conduits, or via retentate and / or permeate connecting conduits between corresponding gas outlets of the membrane separation units, as further described above.

[0164] Further preferred method steps will be apparent from the above description of the device and method according to the invention, as well as from the examples and claims.

[0165] The device and method according to the invention can be used in particular in processes requiring the simultaneous separation of several gas streams with different compositions using gas separation membranes, especially in processes where the gas streams to be separated can vary in terms of their volumetric flow rate and composition. This is especially true in processes using renewable energies, since they are often only available in highly variable amounts. Further applications include, for example, natural gas fields where different gas sources are processed in a common gas separation device rather than one gas separation device for each source, or helium gas sources where methane is separated from helium in a gas separation device and then the methane is utilized thermally, with the off-gas from the thermal utilization also being separated by gas separation. Examples 1 and 2 show that the device according to the invention can perform the separation of the two gases much more efficiently than separate two-gas separation devices. [Brief description of the drawings]

[0166] [Figure 1] FIG. 1 shows a membrane block according to the invention with gas distribution through distribution and supply conduits and with removal of permeate and retentate gases through collection pipes. [Diagram 2] FIG. 2 shows a membrane block according to the invention with gas distribution through connecting conduits and removal of permeate and retentate gases through collection pipes. [Diagram 3]FIG. 3 shows a membrane block according to the invention with gas distribution through distribution conduits, discharge of permeate gas through collection pipes, and discharge of retentate gas through a retentate connection conduit. [Figure 4] FIG. 4 is a linear semi-bundle of membrane blocks with distribution conduits and two gas sources. [Diagram 5] FIG. 5 is a linear semi-bundle of membrane blocks with connecting conduits and two gas sources. [Figure 6] FIG. 6 is a linear complete bundle of membrane blocks with connecting conduits, cross-distribution conduits and two gas sources. [Figure 7] FIG. 7 shows a membrane block according to the invention equipped with a distributor with respective connecting conduits and three gas sources. [Figure 8] FIG. 8 shows two membrane blocks according to the invention, each equipped with a distribution conduit and three gas sources. [Figure 9] FIG. 9 shows three membrane blocks according to the invention, each with a distribution conduit and three gas sources in a circular circuit. [Figure 10] FIG. 10 is a two-stage interconnection of membrane separation stages according to the present invention. [Figure 11] FIG. 11 is a three-stage interconnection of membrane separation stages according to the present invention. [Figure 12] FIG. 12 compares the product of methane yield and purity in the retentate (retentate from the retentate gas conduit (12) or He / CH4 separation unit) to the maximum achievable values ​​for Example 1 and Example 2, and Comparative Example 1. EXAMPLES

[0167] To establish an example, process simulation calculations were performed in Aspen Custom Modeler (ACM) using the model from Scholz et al., "Modeling Gas Permeation by Linking Nonideal Effects," Industrial & Engineering Chemistry Research, 2013, 52, pp. 1079-1088. The model depth from Scholz et al. used for the simulation is as follows: Ideal countercurrent flow of retentate and permeate Constant permeance and therefore constant separation power (independent of temperature) - Consideration of pressure loss - Consideration of energy balance - Consideration of the Joule-Thomson effect Actual gas behavior according to the Soave-Redlich-Kwong equation - Ignoring concentration polarization and further non-ideal effects The module geometry used is as follows: the outer diameter of the hollow membrane fiber is 415 μm, the wall thickness of the hollow membrane fiber is 74 μm. The fiber length is 1 m, and the module diameter is 0.16 m. In the example, the membrane separation unit corresponds to the membrane module in the simulation. The number of fibers is 76700. The heat transfer coefficient of the fiber is 4 W / (m 2 In the examples, the membrane separation unit corresponds to a membrane module in the simulation.

[0168] Example Series 1 (Example 1.1 to Example 1.9): In series 1 of the examples, a separation system corresponding to Figure 1 is used. The first feed gas stream A is a mixture of 10% by volume of helium (He) and 90% by volume of methane (CH 4 The second feed gas stream B contains 40% by volume of CO 2 and 60% by volume of N 2 Feed gas stream A and feed gas stream B are fed into 10 membrane separation units (MTEs) (2 1 ~2 10 The permeate and retentate from each MTE are fed to a membrane separation stage comprising a membrane block (1) having a permeate gas conduit (10 1 ~10 10 ) into the permeate recovery pipe (14), and the non-permeated gas conduit (9 1 ~9 10 ) to the retentate recovery pipe (11). The individual MTEs are identical and contain hollow polyimide fiber membranes operating in countercurrent flow. Two feed gas streams A and B, at the same feed gas temperature of 25° C., are fed by feed gas conduits (7) and (8) to distribution conduits (4) at either end, from which they are fed via feed conduits (6) and (7) to distribution conduits (4) at either end, from which they are fed via feed conduits (8) and (9) to distribution conduits (5) at either end, from which they are fed via feed conduits (9) and (10) to distribution conduits (11) at either end, from which they are fed via feed conduits (12) and (13). 1 ~6 10) through each MTE (2 1 ~2 10 ). The pressures of the retentate gas streams are kept at the same pressure of 10.00 bar by valves in the retentate gas discharge conduits (12) and (13). The pressure drop due to the change in the volumetric flow rate results in slightly different values ​​of the pressure of the feed gas streams in the feed conduits (7) or (8) ranging from 10.08 to 10.1 bar. The composition, temperature, volumetric flow rate (flow rate) and pressure of the two feed gas streams A and B are given in Tables 1a and 1b. The pressure of the permeate gas stream is set at 1.01 bar by valves in the permeate gas discharge conduits (15) and (16). Under the specified conditions, the separation capacity of each MTE is 40000 GPU*m of helium (He). 2 , CO 2 In the case of 26700 GPU*m 2 , N 2 In the case of 800 GPUs*m 2 , C.H. 4 In the case of 530 GPUs*m 2 Therefore, the selectivity, or the ratio of permeabilities of the membranes used in MTE, is He / CH 4 75, CO 2 / N 2 In this case, the number is 33.

[0169] In this example, the sum of the volumetric flow rates of the two feed gas streams is always 1000 m 3 / hour (STP), where in the example series of Examples 1.1-1.9, the individual volumetric flow rates are varied such that the volumetric flow rate of feed stream A increases from example to example, and the volumetric flow rate of feed stream B decreases by the same amount from example to example.

[0170] In the first series of examples, the different feed gas streams flow into the MTEs without mixing, and the retentate and permeate gas streams are also taken off without mixing. This is ensured by the corresponding pigs in the distribution conduits (4) or the permeate recovery pipes (14) and retentate recovery pipes (11). The pressure drop in the distribution conduits (4) and in the branch pipes (5) in this example is only a few millibars, which means that the feed gases are almost ideally separated between the MTEs in terms of volume.

[0171] In Example 1.1, the volumetric flow rate of feed gas stream A is low, so feed gas stream A is fed through feed conduit (6 1 ) through MTE(2 1 ) and MTE (2 1 ) is discharged exclusively to the retentate gas conduit (9) via the retentate gas discharge conduit (12). 1 ) and MTE(2 1 ) is discharged exclusively through a permeation gas discharge pipe (15) to a permeation gas pipe (10). 1 Similarly, feed gas stream B is taken from feed conduit (6 2 ~6 10 ) through the remaining MTE (2 2 ~2 10 ) and the non-permeated gas pipe (9 2 ~9 10 ) is removed exclusively through the retentate gas discharge conduit (13) and the permeate gas discharge conduit (10) is removed exclusively through the retentate gas discharge conduit (14). 2 ~10 10 ) is withdrawn exclusively via the permeate gas discharge line (16). The separation outcome in all four gas discharge lines (retentate gas discharge lines 12 and 13 and permeate gas discharge lines 15 and 16) is in each case the ideally achievable purity and yield, where the product of purity and yield is maximized.

[0172] The compositions, temperatures, volumetric flows (flow rates), pressures and yields of the two permeate streams (15) and (16) and the two retentate streams (12) and (13) obtained in each of Examples 1.1 to 1.9 are given in Tables 2a and 2d.

[0173] [Table 1a]

[0174] [Table 1b]

[0175] [Table 2a]

[0176] [Table 2b]

[0177] [Table 2c]

[0178] [Table 2d]

[0179] Example Series 2 (Example 2.1 to Example 2.8) Series 2 of examples corresponds to Series 1 of examples, except that the feed gas streams reach the MTE in a less ideally separated form and are removed as retentate and permeate gas in a less ideal manner. In other words, the pig used in the connecting conduit (4) of Example 1 is omitted and the two gas streams may slightly mix where they meet. In Series 2 of examples, 50 m 3 (STP) / hour supply gas flow A, 50 m 3 The feed gas streams A and B are joined in such a way that the feed gas stream B with a flow rate of (STP) / hour is fed to the corresponding MTE via the nearest feed conduit in each case. This is the case for Example 2.1, where the MTE (2 1 ) is fed with pure feed stream A, and MTE (2 2 ) was fed with a mixture of 50% by volume of feed stream A and 50% by volume of feed stream B, and the MTE (2 3 ~2 10 ) is fed with pure feed stream B.

[0180] MTE for separating mixed gas (MTE (2 2The retentate gas from the retentate gas conduit of the MTE (10) flows in equal proportions to the retentate gas discharge conduits (12) or (13). The permeate gas from the MTE separating the mixed gas also flows in equal proportions to the permeate gas discharge conduits (15) or (16). The MTE separating only the feed gas stream A (MTE (2) in Example 2.1) 1 The retentate gas from the retentate gas discharge pipe (12) flows completely to the MTE (in Example 2.1, MTE (2 1 The retentate gas from the retentate gas outlet conduits (12) or (13) flows entirely into the retentate gas outlet conduits (13). The situation is similar to the permeate stream from each MTE. The above-mentioned separation of flows between the retentate gas outlet conduits (12) or (13), or the permeate gas outlet conduits (15) or (16), is controlled by appropriate valves in the retentate gas outlet conduits (12) or (13), or the permeate gas outlet conduits (15) or (16).

[0181] The compositions, temperatures, volumetric flows (flow rates) and pressures of the two feed gas streams A and B are given in Tables 3a and 3b. Tables 4a to 4d summarize the results of Examples 2.1 to 2.8. It is clear that in this operating regime, the separation performance is sacrificed due to the low amounts of feed gas streams fed. For example, according to Example 2.1, if the feed gas stream A is very low compared to the feed gas stream B, the separation objective of methane enrichment is not achieved at all. The methane purity in the retentate gas discharge conduit (12) is only 88.6% by volume, instead of the 99.4% by volume achieved in the ideal case of Table 2a. Nevertheless, in Example 2.1, a clear helium enrichment in the permeate gas discharge conduit (15) is achieved, going from 10% to 28.7% helium in the feed gas stream A, although in the ideal case of Example Series 1, 42.1% is achievable.

[0182] In the case of more balanced volumetric flow rates between feed gas streams A and B in Examples 2.3 to 2.7, good separation results are observed in all gas exhaust conduits, despite operation with little mixing of the feed gas streams (12, 13, 15, 16).

[0183] [Table 3a]

[0184] [Table 3b]

[0185] [Table 4a]

[0186] [Table 4b]

[0187] [Table 4c]

[0188] [Table 4d]

[0189] Comparative Example 1 As a non-inventive example, consider the systems of Examples 1 and 2 in which the two feed gas streams A and B are fed separately to separate membrane separation stages 1 or 2, respectively.

[0190] Since the volumetric flow rate of each feed gas stream may vary as in the series 1 and series 2 of the examples, the number of parallel connected MTEs in each membrane separation stage 1 and membrane separation stage 2 needs to be designed for the maximum volumetric flow rate. This means that, compared to the 10 MTEs in the inventive examples 1 and 2, two lots of 10 MTEs are now required, i.e. twice as many MTEs are required. However, since there are variations in the volumetric flow rates of the two feed gas streams, not all MTEs in each membrane separation stage 1 or 2 are at maximum loading at all times of operation. The separation results under these conditions, i.e. the operation of the MTEs under partial loading, are shown in Tables 6a to 6d. The composition, temperature, volumetric flow rate (flow rate) and pressure of the two feed gas streams A and B are listed in Tables 5a and 5b.

[0191] [Table 5a]

[0192] [Table 5b]

[0193] [Table 6a]

[0194] [Table 6b]

[0195] [Table 6c]

[0196] [Table 6d]

[0197] The results in Tables 6a to 6d show that when the MTEs are operated in the partial loading range (caused by fluctuations in the feed stream), satisfactory separation results cannot be obtained in each case, despite using twice the number of MTEs compared to inventive Examples 1 and 2.

[0198] In the system used in the comparative example, it is possible to ensure that the unblocked MTEs always operate in the full-fill range, for example by installing additional valves to block the individual MTEs, however this would obviously further increase the system complexity caused by doubling the number of MTEs, and therefore further increase the control-related complexity.

[0199] Comparison of separation efficiency between Example 1 and Example 2 and Comparative Example 1 In Fig. 12, the results of Example 1 and Example 2 and the Comparative Example are plotted for comparison. The plot shows the product of the methane yield and purity in the retentate (retentate gas conduit (12)) based on the achievable maximum value for the amount of feed gas (unit: m 3 (STP) / hour). Inventive Example 1 always 4 Purity and CH 4 It indicates the maximum achievable product of yields, and therefore the relative value is 100%. In Comparative Example 1, the maximum value is 1000m 3 (STP) / hr full load and then drops off rapidly. Inventive Example 2 maintains a relatively high value over a wide partial load range.

[0200] For example, increasing the number of MTEs in Example Series 2 by utilizing MTEs with lower separation capacities while keeping the total set separation capacity the same can clearly reduce the aforementioned negative effects of partial mixing of the feed gas streams resulting from the dilution effect of the device according to the invention. In the limiting value evaluation, the ideal result of Example 1 is obtained when an unlimited number of MTEs are used.

[0201] In the field of gas separation, the use of hundreds of membrane separation units is entirely practical.

[0202] Example 3 Example 3 considers the inventive operation of a membrane separation stage with a membrane block (19) having ten membrane separation units (2) connected in parallel according to FIG. 1 in the field of helium source gas. The individual membrane separation units (2) have the characteristics described in Example 1. The feed gas streams fed separately to the feed gas conduits (7) and (8) are also ideally separated as in Example 1. In contrast to Example 1, the retentate gas stream (12) and the permeate gas stream (15) are generated by feeding the retentate gas stream or the permeate gas stream from the membrane separation units (2) to the retentate gas recovery pipe (11) or the permeate gas recovery pipe (14) by means of the retentate gas conduit (9) and the permeate gas conduit (10). The retentate gas recovery pipe (11) or the permeate gas recovery pipe (14) are connected only to the retentate gas discharge conduit (12) or the permeate gas discharge conduit (15), respectively. Sampling points were installed in the retentate gas conduits (9) to ascertain the retentate concentrations of the individual membrane separation units (2).

[0203] The helium source gas is a natural gas source containing helium. Depending on the region, and to some extent on the source in the smaller region, the helium concentration may differ significantly. In Example 3, for simplicity, it is assumed that the two sources in question contain exclusively helium and methane. Source 1 (Feed Gas Stream 1) contains 1% helium, and Source 2 (Feed Gas Stream 2) contains 3% helium. The objective of the separation is to achieve a helium content of only 0.2% in the retentate of both feed gas streams in order to achieve a relatively good yield of helium in the permeate. In the feed of the feed gas streams shown in Table 7, it can be seen that the helium concentration in each retentate gas conduit is 0.2%. Table 7 shows the flow rates and concentrations of the retentate and permeate gas streams.

[0204] [Table 7]

[0205] Comparative Example 2 In non-inventive comparative example 2 to Example 3, feed gas stream 1 from source 1 and feed gas stream 2 from source 2 are mixed and then fed as one feed gas stream via a feed gas conduit to ten membrane separation units. Then, each membrane separation unit separates the same feed gas stream. The remaining structure of the membrane separation stage corresponds to Example 3. The results are summarized in Table 8.

[0206] [Table 8]

[0207] Next, comparing Example 3 with Comparative Example 2, it can be seen that the separate supply of the feed gas streams according to Example 3 results in better overall separation results. First, the purity of helium in the permeate and methane in the retentate achieved in Example 3 is higher than that of Comparative Example 2. Furthermore, the yield of helium in the permeate, i.e., the amount of helium in the permeate gas stream relative to the amount of helium in the feed gas stream, is higher in Example 3 than in Comparative Example 2. In other words, more valuable helium is obtained with higher helium purity. Comparing this situation with methane in the retentate gas stream, it can be seen that even the product of methane purity and methane yield in Example 3 is slightly higher than that in Comparative Example 2.

[0208] List of symbols: (1) Membrane block of the present invention (2) Membrane separation unit; each membrane separation unit connected in parallel in the membrane block has (2 1 ) to (2 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (3) Gas inlet of the membrane separation unit; each gas inlet of the membrane separation units connected in parallel in the membrane block has a 1 ) to (3 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (4) Distribution conduits; if there are multiple membrane blocks in a membrane separation stage and therefore multiple distribution conduits, these will have (4 1 ) to (4 o ), where o is a sequential number and the number o indicates the number of distribution conduits present within the membrane separation stage. (5) Branch pipe (6) Supply conduits to the gas inlets of the membrane separation units; each supply conduit of the parallel-connected membrane separation units in the membrane block has a (6 1 ) to (6 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (7) First supply gas pipeline (8) Second supply gas pipeline (9) Refractory gas conduit of the membrane separation unit; Each refractory gas conduit of the membrane separation units connected in parallel in the membrane block has a (9 1 ) to (9 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (10) Permeate gas conduit of the membrane separation unit; each permeate gas conduit of the membrane separation units connected in parallel in the membrane block has a (10 1 ) to (10 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (11) Retardant gas collection pipe (12) First retentate gas discharge pipe (13) Second retentate gas discharge pipe (14) Permeation gas recovery pipe (15) First permeable gas exhaust pipe (16) Second permeable gas exhaust pipe (17) (18) Connecting pipe (19a) Gas pipeline (19b) Gas pipeline (20a) Gas pipeline (20b) Gas pipeline (21) Third supply gas pipeline (22) First permeate gas conduit of the second membrane separation stage B) (23) Second permeate gas conduit of second membrane separation stage B) (24) The first retentate gas conduit of the second membrane separation stage (B) (25) A second retentate gas conduit for the second membrane separation stage (B) (26) The first permeate gas conduit of the third membrane separation stage C) (27) The second permeate gas conduit of the third membrane separation stage C) (28) The first retentate gas conduit of the third membrane separation stage C) (29) The second retentate gas conduit of the third membrane separation stage C) (30) Retent gas outlet of the membrane separation unit; each retentate gas outlet of the membrane separation units connected in parallel in the membrane block has a (3 1 ) to (3 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (31) Permeate gas outlet of the membrane separation unit; each permeate gas outlet of the membrane separation units connected in parallel in the membrane block has a (3 1 ) to (3 n The index n is a serial number, and the number n indicates the number of membrane separation units connected in parallel. (32) A retentate connecting conduit between two retentate gas outlets of two membrane separation units arranged side by side in a membrane block. (33) A permeate connecting conduit between two permeate gas outlets of two membrane separation units arranged side by side in a membrane block.

Claims

1. (a) a first feed gas conduit (7) adapted or designed to transport a first feed gas stream, and a second feed gas conduit (8) adapted or configured to transport a second feed gas stream having a different composition than said first feed gas stream; (b) a membrane separation stage comprising one or more membrane blocks (1); (c) a gas distributor; A gas mixture separation apparatus comprising: - each of said membrane blocks (1) comprises a plurality of membrane separation units (2) connected in parallel, each of said membrane separation units (2) has a gas inlet (3) and a gas separation membrane, the gas mixture fed through said gas inlet (3) being separated by said gas separation membrane into a retentate gas stream and a permeate gas stream; each of said membrane separation units (2) has a retentate gas outlet (30) for the retentate gas stream and a permeate gas outlet (31) for the permeate gas stream; said gas distributor having a connecting conduit (18) and / or one or more distribution conduits (4), Each of the connecting conduits (18) connects the gas inlets (3) of two adjacent membrane separation units (2) of the membrane block (1) to each other; Each of the distribution conduits (4) has a plurality of branch pipes (5) respectively connected to the gas inlets (3) of the individual membrane separation units (2) of the membrane block (1) by supply conduits (6); said branch pipe or pipes (5) may further comprise attachment means for a supply gas conduit, whereby by means of said branch pipe (5) a supply gas conduit and a supply conduit (6) may in each case be simultaneously connected to said respective distribution conduit (4), - if the membrane separation stage comprises a plurality of membrane blocks (1), said membrane separation stage has conduits connecting the membrane blocks (1) of said membrane separation stage to one another, the first feed gas conduit (7) and the second feed gas conduit (8) are each independently connected at a spatially separated position to a distribution conduit (4), or to a connecting conduit (18), or to a branch pipe (5), or to a conduit connecting the membrane blocks (1) of the membrane separation stage, if present, to one another, or to a gas inlet (3), the connection points being arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points of the first feed gas conduit (7) and the second feed gas conduit (8).

2. 2. The apparatus according to claim 1, wherein the connection point between the first feed gas conduit (7) and the second feed gas conduit (8) is arranged such that the first feed gas stream and the second feed gas stream flow towards each other within a membrane block (1) or membrane blocks (1) of the membrane separation stage or within a conduit connecting the membrane blocks (1) of the membrane separation stage to each other.

3. The membrane separation stage comprises one membrane block (1) or a plurality of membrane blocks (1), Each membrane block has a distribution conduit (4) with a number of branches (5) and a feed conduit (6), in each case the feed conduit (6) connecting the branches (5) to the gas inlet (3) of the membrane separation unit (2); 2. The apparatus according to claim 1, wherein the first supply gas conduit (7) and the second supply gas conduit (8) are connected separately and independently to the distribution conduit (4) and / or the branch pipe (5).

4. The membrane separation stage comprises one membrane block (1) or a plurality of membrane blocks (1), Each membrane block includes a plurality of connecting conduits (18) respectively connecting the gas inlets (3) of the membrane separation units (2) to the gas inlets (3) of adjacent membrane separation units (2) in said membrane block (1); and 2. The apparatus according to claim 1, wherein the first feed gas conduit (7) and the second feed gas conduit (8) are each individually and independently connected to a gas inlet (3) of the membrane separation unit (2) or to a number of gas inlets (3) of the membrane separation unit and / or to a connecting conduit (18) or to a number of connecting conduits (18).

5. comprising one, two or three feed gas conduits 3 (21), 4 and 5 adapted to transport one, two or three additional gas streams having a composition different from the first and second feed gas streams; and 2. The apparatus according to claim 1, wherein the additional supply gas conduits 3 (21), 4 and 5 are connected to the gas distributor such that gas stream 3 (21), or gas streams 3 (21) and 4, or gas streams 3 (21), 4 and 5 can be supplied to the membrane separation unit by the gas distributor.

6. The supply gas conduits 3(21), or 3(21) and 4, or 3(21), 4 and 5, each independently - attached to one or more distribution conduits (4), and / or - attached to one or more connecting conduits (18), and / or - attached to a gas inlet (3) or to a number of gas inlets (3), and / or - attached to one gas inlet (3) or to several gas inlets (3) and to one connecting conduit (18) or to several connecting conduits (18); 6. The apparatus of claim 5.

7. 6. The apparatus according to claim 5, wherein the membrane separation stage comprises a plurality of membrane blocks (1) assembled to form a loop circuit.

8. 2. The apparatus according to claim 1, wherein the membrane separation stage comprises a plurality of membrane blocks (1) connected in parallel.

9. The gas distributor comprises, for each membrane block (1), one distribution conduit (4) having a number of branches (5) and a supply conduit (6), in each case the supply conduit (6) connecting the branch (5) to the gas inlet (3) of the membrane separation unit (2); the distribution conduits (4) of each membrane block (1) of the membrane separation stage are connected to each other by conduits (19a, 19b); and the first supply gas conduit (7) and the second supply gas conduit (8) are independently connected at spatially separate positions to a distribution conduit (4) or to a branch pipe (5) or to a conduit (19a, 19b), the connection points being arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8); 9. The apparatus of claim 8.

10. The gas distributor in each membrane block (1) includes a connecting conduit (18) connecting the gas inlet (3) of the membrane separation unit (2) to the gas inlet (3) or gas inlets (3) of adjacent membrane separation units (2) in the membrane block (1), The membrane blocks (1) of the membrane separation stage are connected to each other by conduits (20a, 20b), the conduits (20a, 20b) in each membrane block (1) being connected to one or more connecting conduits (18) and / or one or more gas inlets (3), respectively, the pipe conduits (20b) in each membrane block being connected to another connecting conduit (18) or another gas inlet (3), and 9. The apparatus according to claim 8, wherein the first supply gas conduit (7) and the second supply gas conduit (8) are independently connected at spatially separated positions to one or more connecting conduits (18), or to one or more conduits (20a, 20b), or to one or more gas inlets (3), the connection points being arranged such that two or more gas inlets (3) are located between the connection points of the first supply gas conduit (7) and the second supply gas conduit (8).

11. 2. The apparatus according to claim 1, wherein in the distribution conduit(s) (4), and / or the connecting conduit(s) (18), and / or the conduit(s) (19a, 19b, 20a, 20b), structural measures are taken at likely contact points of the feed gas streams joining in said conduits to control mixing of the feed gas streams and / or to substantially prevent complete mixing of the feed gas streams.

12. the retentate gas conduit (9) of the membrane separation unit (2) of the membrane block (1) of said membrane separation stage is connected to a retentate gas recovery pipe (11), said retentate gas recovery pipe (11) being connected to at least one first retentate gas discharge conduit (12); and / or 2. The apparatus according to claim 1, wherein the permeate gas conduit (10) of the membrane separation unit (2) of the membrane block (1) of the membrane separation stage is supplied to a permeate gas recovery pipe (14), which is connected to at least one first permeate gas discharge conduit (15).

13. between the retentate gas outlets (30) of the membrane separation units (2) of the membrane blocks (1) of said membrane separation stage, there are retentate connecting conduits (32), and at least one retentate connecting conduit (32) or at least one retentate gas outlet (30) is further connected to at least one retentate gas discharge conduit (12); and / or The membrane separation stage has a permeate connection conduit (33) between the permeate gas outlets (31) of the membrane separation units (2) of the membrane block (1), and at least one of the permeate connection conduits (33) or at least one of the permeate gas outlets (31) is further connected to at least one permeate gas discharge conduit (15).

2. The apparatus of claim 1.

14. The process according to claim 1, comprising two membrane separation stages A and B, The first feed gas conduit (7) and the second feed gas conduit (8) are connected to a gas distributor of the first membrane separation stage A according to claim 1, and said first membrane separation stage A is configured such that two different retentate streams are obtained in a first retentate gas discharge conduit (12) and a second retentate gas discharge conduit (13) and / or two different permeate streams are obtained in a first permeate gas discharge conduit (15) and a second permeate gas discharge conduit (16); The first retentate gas discharge conduit (12) and the second retentate gas discharge conduit (13), or the first permeate gas discharge conduit (15) and the second permeate gas discharge conduit (16) are connected to a gas distributor of the second membrane separation stage B according to claim 1.

2. The apparatus of claim 1.

15. The process according to claim 1, comprising three membrane separation stages A, B and C, The first feed gas conduit (7) and the second feed gas conduit (8) are connected to a gas distributor of the first membrane separation stage A according to claim 1, and said first membrane separation stage A is configured such that two different retentate streams are obtained in a first retentate gas discharge conduit (12) and a second retentate gas discharge conduit (13) and / or two different permeate streams are obtained in a first permeate gas discharge conduit (15) and a second permeate gas discharge conduit (16); The first retentate gas discharge conduit (12) and the second retentate gas discharge conduit (13) are connected to a gas distributor of the second membrane separation stage B according to claim 1; and The first permeate gas discharge conduit (15) and the second permeate gas discharge conduit (16) are connected to a gas distributor of the third membrane separation stage C according to claim 1.

2. The apparatus of claim 1.

16. 10. A method for simultaneously purifying two or more gas streams, each of which differs in composition, wherein the gas separation is carried out in an apparatus according to claim 1.

17. (i) providing a first feed gas stream; (ii) providing a second feed gas stream having a different composition than the first feed gas stream; (iii) feeding the first and second feed gas streams to a membrane separation stage; (iv) supplying said first and second feed gas streams to a gas inlet (3) of a membrane separation unit (2) of said membrane separation stage by means of a gas distributor; (v) separating the gas mixture fed to the membrane separation unit (2) through the gas inlet (3) into a retentate gas stream and a permeate gas stream by a gas separation membrane in the membrane separation unit (2); Including, The membrane separation stage may have one membrane separation block (1) or several membrane separation blocks (1), each of which may comprise several membrane separation units (2) connected in parallel. and said membrane separation stage comprises a gas distributor comprising a connecting conduit (18) and / or a distribution conduit (4), Each of the connecting conduits (18) connects the gas inlets (3) of two adjacent membrane separation units (2) of the membrane block (1) to each other; The distribution conduit (4) includes a number of branch pipes (5) each connected to the gas inlets (3) of the individual membrane separation units (2) of the membrane block (1) by separate supply conduits (6); The branch pipe or pipes (5) may further comprise attachment means for a supply gas conduit, whereby a supply gas conduit and a supply conduit (6) may be simultaneously connected to the distribution conduit (4) by means of the branch pipe (5); and - if the membrane separation stage comprises several membrane blocks (1), the membrane separation stage has conduits connecting the membrane blocks (1) of the membrane separation stage to one another, and - said first and second feed gas streams are each connected independently, at a spatially separated location, to a distribution conduit (4), or to a connecting conduit (18), or to a branching pipe (5), or to a conduit connecting the membrane blocks (1) of the membrane separation stage, if present, to one another, or to a gas inlet (3); 17. The method of claim 16, wherein the connection points of the first and second feed gas streams are arranged such that two or more branch pipes (5) and / or two or more gas inlets (3) are located between the connection points.

18. said first feed gas stream and said second feed gas stream flow towards each other within the membrane block (1) or membrane blocks (1) of said membrane separation stage and / or within conduits connecting said membrane blocks (1) of said membrane separation stage to each other; and / or In order to supply gas streams having different compositions to at least two different membrane separation units (2) of one membrane block (1) of the membrane separation stage, the first and second feed gas streams are supplied to the gas inlet (3) of the membrane separation unit (2) of the first membrane separation stage by a gas distributor; 20. The method of claim 17.

19. The membrane separation stage comprises one or more membrane blocks (1), each membrane block (1) having a distribution conduit (4) with a number of branches (5) and a feed conduit (6), in each case the feed conduit (6) connecting the branches (5) to the gas inlet (3) of the membrane separation unit (2), and 18. The method of claim 17, wherein the first and second feed gas streams are fed separately and independently to the distribution conduit (4).

20. The membrane separation stage comprises one or more membrane blocks (1), each of which comprises a number of connecting conduits (18) respectively connecting the gas inlet (3) of a membrane separation unit (2) to the gas inlet (3) of an adjacent membrane separation unit (2) of the membrane block (1); and the first feed gas stream and the second feed gas stream are each individually and independently fed to a gas inlet (3) of the membrane separation unit (2) and / or to a connecting conduit (18) or to a number of connecting conduits (18); 20. The method of claim 17.

21. 18. The method of claim 17, wherein one, two or three additional gas streams having a different composition from the first and second feed gas streams are supplied to the gas distributor by the feed gas conduits 3(21), 3(21) and 4, or 3(21), 4 and 5.

22. Feed gas stream 3, or feed gas streams 3 and 4, or feed gas streams 3, 4 and 5, respectively - fed into one or more distribution conduits (4), and / or - fed into one or more connecting conduits (18), and / or - fed to one gas inlet (3) or to several gas inlets (3) and one or several connecting conduits (18); 22. The method of claim 21.

23. 23. The method according to claim 22, wherein a plurality of membrane blocks (1) of the membrane separation stage are combined to form a loop circuit.

24. 18. The method according to claim 17, wherein the membrane blocks (1) of the membrane separation stage are connected in parallel.

25. The gas distributor has, per membrane block (1), one distribution conduit (4) with a number of branches (5) and a supply conduit (6), which in each case connects the branches (5) to the gas inlets (3) of the membrane separation units (2); the distribution conduits (4) of each membrane block (1) of the membrane separation stage are connected to each other by conduits (19a, 19b); and 25. The method of claim 24, wherein the first and second feed gas streams are fed separately and independently to one or more distribution conduits (4) and / or conduits (19a, 19b).

26. The gas distributor of each membrane block (1) includes a connecting conduit (18) connecting the gas inlet (3) of a membrane separation unit (2) to the gas inlet (3) of an adjacent membrane separation unit (2) of the membrane block (1), The membrane blocks (1) of the membrane separation stage are connected to each other by conduits (20a, 20b), the conduits (20a, 20b) in each membrane block being connected to one or more connecting conduits (18) or to a gas inlet (3); and said first and second feed gas streams are fed separately and independently to a gas inlet (3) or gas inlets (3) of a membrane separation unit (2) and / or to one or more connecting conduits (18) and / or to conduits (20a, 20b) of said respective membrane blocks (1) of said membrane separation stage, with the proviso that said first and second feed gas streams are not fed simultaneously to the same gas inlet (3) or connecting conduit (18) or are fed simultaneously to one or more identical gas inlets (3) or connecting conduits (18) or are fed simultaneously to several different gas inlets (3) or connecting conduits (18); 25. The method of claim 24.

27. 18. The apparatus according to claim 17, wherein in the distribution conduit(s) (4), and / or the connecting conduit(s) (18), and / or the conduit(s) (19a, 19b, 20a, 20b), structural measures are taken at likely contact points of the feed gas streams joining in said conduits to control mixing of the feed gas streams and / or to substantially prevent complete mixing of the feed gas streams.

28. (vi) combining the retentate gas streams from the membrane separation units (2) of the membrane block (1) to obtain one or more retentate gas streams; and / or (vii) combining the permeate streams from the membrane separation units (2) of the membrane block (1) to obtain one or more permeate gas streams.

20. The method of claim 17, further comprising:

29. the retentate streams from the membrane separation units (2) of the membrane block (1) of the membrane separation stage are fed to a retentate gas recovery pipe (11) in which they are combined to form one retentate gas stream and fed to a retentate gas discharge conduit (12) or the retentate streams are separated into at least two retentate gas streams 1 and 2 and fed to at least two retentate gas discharge conduits (12) and (13); and / or 29. The process according to claim 28, wherein the permeate streams from the membrane separation units (2) of the membrane block (1) of the membrane separation stage are fed to a permeate gas recovery pipe (14) in which the permeate streams are combined to form one permeate gas stream and fed to a permeate gas discharge conduit (15) or the permeate streams are separated into at least two permeate gas streams 1 and 2 and fed to at least two permeate gas discharge conduits (15) and (16).

30. the retentate gas streams from the membrane separation units (2) of the membrane blocks (1) of said membrane separation stage are combined by a retentate connecting conduit (32) between the retentate gas outlets (30) of the membrane separation units (2) of the membrane blocks (1) of said membrane separation stage to form one retentate gas stream and fed to a retentate gas discharge conduit (12) or are separated into at least two retentate gas streams 1 and 2 and fed to at least two retentate gas discharge conduits (12) and (13); and / or 29. The process according to claim 28, wherein the permeate gas streams from the membrane separation units (2) of the membrane blocks (1) of the membrane separation stage are combined to form one permeate gas stream and fed to a permeate gas discharge conduit (15) or are separated into at least two permeate gas streams 1 and 2 and fed to at least two permeate gas discharge conduits (15) and (16) by means of a permeate connecting conduit (33) between the permeate gas outlets (31) of the membrane separation units (2) of the membrane blocks (1) of the membrane separation stage.

31. 15. The process according to claim 14, which is carried out in an apparatus having two membrane separation stages A and B, The first and second feed gas streams having different compositions are fed to the membrane separation stage A as described in claim 17, The first membrane separation stage A separates the first and second feed gas streams into first and second retentate gas streams having different compositions and / or into first and second permeate gas streams having different compositions; The two retentate streams or the two permeate streams from the first membrane separation stage A are fed to the second membrane separation stage B as two feed streams of different composition; and the second membrane separation stage B separates the two retentate or permeate streams from the membrane separation stage A into third and fourth retentate gas streams of different composition and / or into third and fourth permeate gas streams of different composition; 20. The method of claim 17.

32. 16. The process according to claim 15, which is carried out in an apparatus comprising three membrane separation stages A, B and C, The first and second feed gas streams having different compositions are fed to the membrane separation stage A as described in claim 17, The first membrane separation stage A separates the first and second feed gas streams into first and second retentate gas streams having different compositions and into first and second permeate gas streams having different compositions; the two retentate streams from the first membrane separation stage A are fed as two feed streams of different composition to the second membrane separation stage B; the second membrane separation stage B separates the two retentate gas streams from the membrane separation stage A into a third retentate gas stream and a fourth retentate gas stream having different compositions; The two permeate gas streams from the first membrane separation stage A are fed to the third membrane separation stage C as two feed streams of different composition; the third membrane separation stage C separates the two permeate gas streams from the membrane separation stage A into a fifth permeate gas stream and a sixth permeate gas stream having different compositions; 20. The method of claim 17.

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