Patent Description:
Today, polyolefines are commercially manufactured using continuous processes starting from high-purity olefins, typically called polymer-grade olefins. One reason for using polymer-grade olefins is to minimize purge-streams and losses during manufacturing as well as accumulation of non-reactive compounds in the reactor. Further, purge gas of polymer reactors containing valuable product compounds, e.g. propylene, are often burned as conventional separation technology is not profitable. The purge is necessary to remove non-reactive compounds of the feed from the reactor, e.g. propane. Attempts have been made to use intermediate-grade olefins as a starting material and to optimize purge-and recycle- streams in the polymerisation processes.

<CIT>) describes a process of making polypropylene from intermediate grade propylene. The process described requires downstream of a reactor (<NUM>) a polymer separation system (<NUM>) and a distillation unit (<NUM>) for obtaining a recycle stream comprising <NUM>-<NUM>% propylene to be recycled.

It is apparent that both, distillation step and polymer separation system are disadvantageous, as energy-consuming.

Further, <CIT>) describe membrane-augmented polypropylene manufacturing. The process described requires downstream of a reactor (<NUM>) a separation unit (<NUM>) to obtain a vent stream (<NUM>) and a fraction thereof, typically no more than <NUM>%, are subjected to a membrane separation. The membranes disclosed in Baker et al only allow moderate olefin-increase compared to the feed, typically no more than about <NUM>% or even only <NUM>%. The membrane separation step results in a residue stream typically containing as much as <NUM>% propane or more, which is vented from the polymerization process, and a permeate stream containing <NUM>% or less propylene, which is recirculated to the polymerization reactor.

It is apparent that both, polymer separation (<NUM>) and insufficient membrane separation (<NUM>) are disadvantageous, as they result in large purge- streams and losses (<NUM>, <NUM>).

Further, Stark et al describe gas separation processes using MOF containing membranes. The membranes comprise a composite material which is composed of a polymer matrix exhibiting channel-like structures (<NUM>) and MOFS embedded in these structures. The membranes are suited for gas separation and show selectivities above the Knudsen limit.

<CIT>, <CIT>, <CIT>, <CIT> and <CIT> disclose membranes and methods of production of polypropylene.

In consequence, there is a need for improved manufacturing of polyolefines addressing these shortcomings.

Thus, it is an object of the present invention to mitigate at least some of these drawbacks of the state of the art. In particular, it is an aim of the present invention to provide an improved method for manufacturing polypropylene.

It is a further aim to provide improved membranes, particularly membranes for adapted to these manufacturing processes.

These objectives are achieved by the method as defined in claim <NUM>.

Further aspects of the invention are disclosed in the specification and independent claims, preferred embodiments are disclosed in the specification and the dependent claims. Accordingly, the invention relates.

The present invention will be described in more detail below.

Membrane: The term membrane is known in the field and denotes a device that functions as a selective barrier due to the presence of pores / channels. Membranes may be present in the form of flat sheets or in the form of hollow fibers. In each case, such membrane is defined by two surfaces and channels / pores perpendicular to the membrane surfaces.

Flat sheets are typically manufactured continuously and typically have a width of <NUM>. <NUM> - <NUM> and a thickness of <NUM> - <NUM> micrometers. Hollow fibres are typically manufactured continuously and have an outer diameter of <NUM> - <NUM> and typically have a wall thickness of <NUM> - <NUM> micrometers.

In the context of this invention, the polymer pore size / channel size of the membrane may cover a broad range, typically from <NUM> to <NUM>, preferably from <NUM> to <NUM>. As will become apparent, "polymer pore size" and "molecular sieve pore size" are to be distinguished. Contrary to polymer pore size, the molecular sieve pore size is on another scale, in the subnanometre range.

A membrane is "self-supporting", if the membrane itself is freestanding and / or can be handled manually without a supporting structure. Further, a membrane may be part of a layered structure, i.e. comprise additional layers, such as supporting layers or covering layers. Such additional layers may improve stability of the membrane, allowing reliable manufacturing and / or use at higher pressures.

MOFs (as outlined in further detail below) are embedded in these pores / channels, particularly channels vertical to the membrane plane. Without being bound to theory, it is believed that the MOFs substantially improve the membrane's selectivity. The selectivity of a membrane for the components of a given fluid may be assessed by considering Knudsen-diffusion. Assuming a simple pore / channel, diffusion is dependent on pore radius and molecular mass. The separation of compounds stemming from Knudsen diffusion can be calculated with the following formula, where alpha is the selectivity of compound A over compound B and Ma and Mb is the respective molar mass.

For example, the pair propylene / propane has a value of <NUM> and the pair ethylene / ethane has a value of <NUM>. The inventive membranes show values way above the Knudsen limit, particularly a selectivity for the pair propylene / propane of at least <NUM> and the pair ethylene / ethane of at least <NUM>. This finding indicates that the MOFs incorporated in the membrane significantly influence the selectivity of the membranes. On the other hand, membranes showing a selectivity in the range of the Knudsen limit apparently possess simple pores / channels that only provide moderate selectivity, i.e. a selectivity not influenced by molecular sieving. To distinguish from simple membranes, having a selectivity in the range of the Knudsen limit, the expression "tightly embedded MOFs" is chosen.

Metal-organic frameworks (MOFs): The term MOF is known in the field and denotes chemical entity comprising metal ions (including clusters) cores and ligands (also termed "struts"). The ligands have at least two coordination sites. In the context of this invention MOFs do form a <NUM> dimensional network with open pores. As a characteristic of MOFs, they possess a porous structure, defined by its molecular sieve pore size. Percentages given in this specification, unless otherwise indicated, relate to mass - %.

The present invention will be better understood by reference to the figures.

<FIG> and <FIG> outline the polyolefine manufacturing process described herein. List of references:.

<FIG> outlies the structure of suitable membranes (<NUM>), <FIG> shows an embodiment with backing layer while <FIG> shows an embodiment without backing layer. An optional <NUM>nd functional layer (<NUM>) opposite to the backing layer(<NUM>) may be present (not shown). List of references:.

In more general terms, in a first aspect, the invention relates to a continuous process for making polypropylene (<NUM>), comprising the steps of (a) feeding an olefin stream (<NUM>) to a reactor (<NUM>); (b) contacting the olefin stream (<NUM>) with a polyolefine forming catalyst (<NUM>) in the reactor (<NUM>) to thereby obtain polyolefines (<NUM>) and a first effluent stream (<NUM>); (c) removing the polyolefines (<NUM>) and the first effluent stream (<NUM>) from the reactor (<NUM>) at separate outlets (<NUM>, <NUM>); (d) directly subjecting the first effluent stream (<NUM>) to a membrane separation unit (<NUM>) to thereby obtain an olefin-enriched recycle stream (<NUM>) and a second effluent stream depleted in olefin (<NUM>); (e) feeding the reactor (<NUM>) with the recycle stream (<NUM>). According to this invention, the membrane separation unit (<NUM>) is as defined in claim <NUM>.

As explained in further detail below, the inventive process allows using an intermediate grade monomer stream as feed for a polymerisation reactor (<NUM>). The non-reacted by-products (<NUM>) are fed to a membrane unit (<NUM>) where saturated, non-reactive compounds (<NUM>) are removed while non-converted olefins (<NUM>) are recycled. Thus, the process allows using intermediate grade monomer as a starting material and ensures a constant monomer concentration in the reactor (<NUM>). The inventive process thus allows economical production of polymers from both, polymer-grade monomers and non-polymer-grade monomers.

Without being bound to theory, it is believed that the membranes (<NUM>) described herein play an important role in successfully performing the continuous process described herein. Particularly, the combination of polymer matrix (<NUM>), channels (<NUM>) and molecular sieves (<NUM>) are important. The molecular sieves (<NUM>) remain within said channels (<NUM>) when used, ie. during manufacturing of membrane modules and when in use. To distinguish from simple (and removable) coatings of molecular sieves on membrane surfaces, the expression "tightly embedded" is used.

This aspect of the invention shall be explained in further details below.

Membrane unit (<NUM>): Membrane units are known per se; a membrane unit (<NUM>) comprises one or more membrane modules (<NUM>). Each membrane module, in turn, comprises one or more membranes (<NUM>). Until now, membranes (<NUM>) as defined herein were not applied in membrane units (<NUM>) for the purpose of olefin/paraffin separation, located downstream a polymerisation reactor (<NUM>). Membrane units (<NUM>) are adapted to elevated temperatures, e.g. <NUM> - <NUM> and elevated pressures, e.g. <NUM> - <NUM> bar.

Typically, membranes (<NUM>) are housed in a membrane module (<NUM>) as known in the field, including Spiral-wound modules, plateframe modules and potted hollow-fiber modules. Flat-sheet membranes in spiral-wound modules are preferred. The making of all these types of modules is well known in the art.

The membranes (<NUM>) may be present in the form of flat sheets or in the form of fibers. Since conventional polymeric materials are used for the membranes, they are relatively easy and inexpensive to prepare and to house in modules, particularly compared with other types of membranes, such as pyrolysed carbon membranes and ceramic membranes. The making of all these types of modules is well known in the art.

According to this invention, membrane (<NUM>) comprises a first functional layer (<NUM>), optionally a backing layer (<NUM>) connected to the first functional layer. The membrane (<NUM>) may further comprise a <NUM>nd functional layer (<NUM>) opposite to said backing layer (<NUM>).

The first functional layer (<NUM>) comprises a polymer matrix (<NUM>) and molecular sieves (<NUM>) and said matrix (<NUM>) comprising channels perpendicular to the membrane surface thereby connecting both surfaces of said membrane and wherein said molecular sieves (<NUM>) are located within said channels. Due to the location of molecular sieves (<NUM>) within said channels, the molecular sieves are tightly embedded and the membranes show a selectivity for a given olefin/paraffin pair above the Knudsen limit.

A membrane unit may or may not comprise one or more washing modules (<NUM>). Such washing module being arrange prior to the membrane module(s) (<NUM>). Suitably, the washing module (<NUM>) is in fluid communication with the reactor (<NUM>) and with all of said one or more membrane modules (<NUM>). The washing module is adapted to receive effluent stream (<NUM>). It is configured to contact effluent stream (<NUM>) with a liquid (<NUM>), also known as scrubber solution, to thereby obtain a purified effluent stream (<NUM>').

A broad range of washing modules for gases is known and may be implemented in the inventive process.

In an embodiment, liquid (<NUM>) contains mineral oil and glycol and the module (<NUM>) is preferably of the liquid-liquid separation type. Such liquids and modules are known and described e.g. in Wo2019/<NUM>.

Preferred are biphasic systems comprising mineral oil (e.g. available as hydrobrite) and propylene glycol in a ratio <NUM>:<NUM> to <NUM>:<NUM>.

In an alternative embodiment, liquid (<NUM>) contains a mixture of liquid hydrocarbon and C<NUM>-<NUM> carboxylic acids. Again, such liquid is adapted to react with catalyst (<NUM>) and is also known as "hydrocarbon scrubbing liquid". In this embodiment, the module (<NUM>) is preferably of the stirred reactor vessel type. Such liquids and modules are known and described e.g. in <CIT>.

Preferred are monophasic systems comprising mineral oil (e.g. diesel fuel oil) and one or more C<NUM>-<NUM> carboxylic acids in a ratio <NUM>:<NUM> to <NUM>:<NUM>.

It was surprisingly found that implementing a washing module (<NUM>) within the membrane unit (<NUM>) improves the overall process for making polypropylene (<NUM>).

A polymer matrix (<NUM>) is polyethersulfone (PES).

The molecular sieve (<NUM>) within said optional second functional layer is selected from the group consisting of ZIF-<NUM>, modified ZIF-<NUM> having an effective molecular sieve pore size of <NUM>, ZIF-<NUM>, and ZIF-<NUM>.

The molecular sieve (<NUM>) within said functional layer (<NUM>) is modified ZIF-<NUM> having an effective pore size of <NUM>.

The molecular sieve (<NUM>) is a modified ZIF-<NUM> (hereinafter ZIF-<NUM>'). Such ZIF-<NUM>' comprising zinc coordinated to <NUM>-methylimidazole and having an effective pore size of <NUM> Angstroem. Such effective pore size is obtained by the synthetic protocol provided below and combining two different sources of zinc, namely non-soluble ZnO and soluble Zn-salt (preferably zinc nitrate Zn(N03)<NUM>). Thus, chemical composition of ZIF-<NUM> and ZIF-<NUM>' are the same, but crystalline structure differs, resulting in different pore sizes, namely <NUM> - <NUM> Angstroem for ZIF-<NUM> and <NUM> Angstroem for ZIF-<NUM>'. Without being bound to theory, it is believed that ZnO is important for initiating crystal formation in the pores of the membrane while soluble Zn<NUM>+ - salt is important for formation of the appropriate crystal structure of ZIF-<NUM>'with its preferred pore size.

Determination of effective pore size for gas separation membranes is known in the field. Briefly, gas molecules of different size (corresponding to its kinetic diameter) are pressed through a membrane and the permeance (pressure / area corrected flow) being compared. The effective pore size is then determined by comparing the permeance. Example: C3H6 (kinetic diameter: <NUM> Angstroem) permeance of <NUM> GPU, CO2 (kinetic diameter: <NUM> Angstroem) permeance of <NUM> GPU: effective pore size between these molecules, e.g. <NUM> Angstroem. Details may be found e.g. in<NPL>).

The backing layer (<NUM>) is an organic polymer, selected from the group consisting of polypropylenes (PP), polyethylenes (PE), polyamides (PA), polyesterterephtalates (PET) and polyethersulfones (PES), such as a polyamide membrane. The backing layer has a meshlike structure and a thickness of <NUM> - <NUM>. Mesh-like structures may be obtained by woven- or non-woven fabrics, such as a gauze or a fleece.

The second functional layer (<NUM>) may comprise or consist of MOFs as defined herein.

Advantageously, the membrane (<NUM>) comprises or consists of a first functional layer (<NUM>) and a backing layer (<NUM>).

Reactor (<NUM>): Reactors conventional in the field may be used for the present method. Advantageously, fluidized bed reactors are used. Suitable reactors are adapted to convert the olefin into the corresponding polyolefine in the presence of catalyst. The reactor (<NUM>) is adapted to receive feed stream (<NUM>) and recycle stream (<NUM>) via one or more inlets (<NUM>). The reactor is further adapted to release formed polyolefin (<NUM>) via one or more outlets (<NUM>) and first effluent stream (<NUM>) via one or more outlets (<NUM>).

Step (a): Feeding a polymerisation reactor with the starting material is known. Depending on the reactor, the starting material may already contain catalyst. Alternatively, catalyst may be separately fed to the reactor and feed stream (<NUM>) is free of catalyst.

Further, recycle stream (<NUM>) and Feed stream (<NUM>) may be combined prior to feeding the reactor in one inlet; or these streams may be fed via separate inlets into the reactor.

Olefines are classified by its purity including, refinery grade, chemical grade and polymer grade. For propylene, the respective value for refinery grade (RGP) is -<NUM>-<NUM>%, for chemical grade (CGP) is ~<NUM>-<NUM>% and for polymer grade (PGP) is ><NUM>%. Replacing Polymer grade olefins by Chemical grade olefins is apparently beneficial for economic reasons. However, it also has a significant ecological impact, as energy - intense purification is avoided. In one embodiment, the olefin stream (<NUM>) is an intermediate grade olefin stream (e.g. RGP or CGP stream). Depending on the specific process applied, such olefin stream may be pre-treated to thereby remove components that can be critical to the catalyst. Such pre-treatment particularly reduces the concentration of sulfur, alkyne or oxygen containing compounds to acceptable levels.

The olefin stream (<NUM>) is a propylene stream and the polyolefine (<NUM>) is a polypropylene.

Step (b): Catalytic polymerisation of olefins to obtain polyolefines is a known process. Typically, the catalyst is present in the form of solid particles. The reaction may take place in a slurry or gas phase; at present gas phase polymerisation is preferred. Suitable reaction conditions for polypropylene are <NUM> - <NUM> / <NUM>-<NUM> bar; for polyethylene <NUM>-<NUM> / <NUM>-<NUM> bar and for polyisobutene <NUM>-<NUM>, <NUM>-<NUM> bar.

A number of reactor types and reaction conditions are known to the skilled person. It is an advantage of the present invention that reactors and plants currently in use may be adapted to implement the continuous process described herein. An upgrade of existing reactors / plants thereby improves both, the economics and the ecological balance sheet of existing reactors / plants. As discussed in the prior art cited above, the whole reaction mixture is removed from the reactor and subjected to an individual separation step. According to this invention, such individual separation can be avoided. Rather, the polyolefine (<NUM>) formed in this step (b) is removed via outlet (<NUM>), while a first effluent stream (<NUM>) is removed via outlet (<NUM>) from the reactor (<NUM>).

Step (c): In line with the inventive method, the polyolefine is separately removed via outlet (<NUM>) while the first effluent stream (<NUM>) is removed via outlet (<NUM>). Reactors adapted to such process step are known in the art. The layout avoids an additional separation unit, as required in the prior art discussed above.

In an embodiment, outlet (<NUM>) contains a means for removing / passivating catalyst (<NUM>). Such catalyst may be present in effluent stream (<NUM>) and may result in a negative influence on the performance of membrane unit (<NUM>).

Step (d): Separation step (d) is of key relevance for the inventive method. Due to the beneficial properties of the membranes described herein, it is possible to perform the synthesis using chemical grade olefins and / or to essentially avoid, or avoid, purge streams. In view of the membranes used, recycle stream (<NUM>) is the permeate while second effluent stream (<NUM>) is the residue.

It is considered advantageous that step (d) uses process parameters similar to reaction conditions (c), i.e. Temperatures +/- <NUM> compared to the reactor and pressure +/- <NUM> bar compared to the reactor (<NUM>).

In one embodiment, the second effluent stream (<NUM>) comprises at most <NUM> %, preferably at most <NUM>% olefin.

In one embodiment, the recycle stream (<NUM>) comprises at least <NUM>%, preferably at least <NUM>% olefin.

Separation step (c) follows directly past removal of effluent stream (<NUM>) from the reactor. Thus, between reactor (<NUM>) and membrane unit (<NUM>), no separation unit is required. This distinguishes from the above cited prior art where always a separation unit is required past the reactor. Apparently, avoiding such additional separation unit is a benefit to the process.

The first effluent stream of step (c) may be subjected to the step (d) in total, i.e. without a split. Alternatively, effluent stream (<NUM>) may be split into a stream subject to step (d) (stream <NUM>') and a stream directly recycled to the reactor (stream <NUM>'). Allowing such split improves process control and flexibility. Typically, more than <NUM>%, preferably more than <NUM>%, much preferably more than <NUM>% of the first effluent stream are subjected to step (d). Thus, only a small fraction, if any, is directly recycled. Compared to the prior art, the highly effective membranes allow subjecting a large fraction to the separation unit (<NUM>).

In an exemplary embodiment, the first effluent (<NUM>) contains <NUM> - <NUM>% olefin and the recycle stream (<NUM>) contains <NUM> - <NUM>% olefine.

In an exemplary embodiment, the olefin stream (<NUM>) is polymer grade propylene, the membrane (<NUM>) is a PES membrane and the molecular sieve (<NUM>) is ZIF-<NUM>'.

In a further exemplary embodiment, the olefin stream (<NUM>) is chemical grade propylene, the membrane (<NUM>) is a PES membrane, and the molecular sieve (<NUM>) is ZIF-<NUM>'.

In a further exemplary embodiment, the olefin stream (<NUM>) is polymer grade propylene, the membrane (<NUM>) is a PES membrane, and the molecular sieve (<NUM>) is ZIF-<NUM>' in combination with further ZIFs, either as a mixture in one functional layer or separated in two functional layers.

In a further exemplary embodiment, the olefin stream (<NUM>) is chemical grade propylene, the membrane (<NUM>) is a PES membrane and the molecular sieve (<NUM>) is ZIF-<NUM>' in combination with further ZIFs, either as a mixture in one functional layer or separated in two functional layers.

In a further exemplary embodiment, the olefin stream (<NUM>) is polymer grade ethylene, the membrane (<NUM>) is a PES membrane and the molecular sieve (<NUM>) is ZIF-<NUM>'.

In a further exemplary embodiment, the olefin stream (<NUM>) is chemical grade ethylene, the membrane (<NUM>) is a PES membrane and the molecular sieve (<NUM>) is ZIF-<NUM>'.

Further Steps: It is apparent that the inventive polymer manufacturing process may be embedded in a larger process and / or may be complemented by further process steps. Such steps are known in the field and include the steps described below.

Step (f) In one embodiment, the second effluent stream (<NUM>) may be fed to a heating unit. As stream (<NUM>) is depleted in olefins and rich in alkanes, it may be used to generate heat, e.g. for heating reactor (<NUM>). In one further embodiment, the second effluent stream (<NUM>) may be fed to a gas turbine to thereby generating electrical energy (<NUM>). This energy may be used for a compressor to pressurize stream (<NUM>) before feeding it to reactor (<NUM>).

In a second aspect, the invention relates to the use of specific membranes (<NUM>), membrane modules (<NUM>) and membrane units (<NUM>), all as described herein, in a catalytic propene polymerisation process.

In a third aspect, the invention relates to novel membranes, membrane modules, membrane units and polymerisation plants comprising them as well as the manufacturing of membranes and membrane modules.

In one embodiment, the invention provides for a membrane (<NUM>) as defined in claim <NUM>.

In one embodiment, the invention provides for a membrane as described above, further comprising (iv) a second functional layer containing (<NUM>), ie. comprising or consisting of, molecular sieves (<NUM>) as described herein (preferably ZIF-<NUM>, ZIF-<NUM>, ZIF-<NUM> and combinations thereof). By including such second functional layer (<NUM>), performance of the membrane may be fine-tuned. In an embodiment, the molecular sieves (<NUM>) of first and second functional layer differ.

Said backing layer (<NUM>) has a thickness of <NUM> - <NUM> micron. Further, the material of said backing layer (<NUM>) is selected from the group consisting of polypropylenes, polyethylenes, poylamides, polyethylene-terephtalates, or polyethersulfones. The molecular sieves (<NUM>) within said optional second functional layer are selected from the group consisting of ZIF-<NUM>, modified ZIF-<NUM> having an effective pore size of <NUM>, ZIF-<NUM>, and ZIF-<NUM>. The material of the polymer matrix (<NUM>) is selected from the group of Polyethersulfones (PES). It was found that the combination of modified ZIF-<NUM> (<NUM>) and backing layer in the form of a mesh (<NUM>) provides particularly good selectivities under conditions applied in commercial scale production of polyolefines.

In one embodiment, the invention provides for a membrane module (<NUM>), comprising one or more membranes as described herein. Advantageously, the membrane modules are adapted to gas separation processes as described herein. Such modules are known per se, but not containing the membranes as described herein. It is considered an advantage that present membrane modules may be replaced by the inventive membrane modules, thereby improving polyolefine production. Inventive membrane modules may be selected from the group of "flat sheet" membrane modules and "hollow fibre" membrane modules. Such membrane modules may comprise one or more membranes (<NUM>) as described herein.

In one embodiment the membrane module is a flat sheet membrane module, selected from spiral wound membrane modules, plate frame modules, and tubular modules, particularly tubular modules.

In one further embodiment, the membrane module is selected from hollow fibre membrane modules.

In one embodiment, the invention provides for a membrane separation unit (<NUM>) adapted to the process of claim <NUM>, said separation unit comprises a membrane as defined in claim <NUM>.

Described herein is a polypropylene-production plant comprising a reactor (<NUM>) and a membrane unit (<NUM>), the reactor (<NUM>) being a fluidized bed reactor adapted to convert chemical grade propylene feed, the membrane unit (<NUM>) comprising one or more membranes (<NUM>) as defined in claim <NUM>, the membrane unit (<NUM>) being in direct fluid communication with the reactor to receive a stream free of polypropylene.

Described herein is a polypropylene-production plant comprising a reactor (<NUM>) and a membrane unit (<NUM>), the reactor (<NUM>) being a fluidized bed reactor adapted to convert chemical grade propylene feed, the membrane unit (<NUM>) comprising one or more membranes (<NUM>) as defined in claim <NUM>, the membrane unit (<NUM>) being in direct fluid communication with the reactor to receive a stream free of polypropylene and the membrane unit (<NUM>) comprising a washing module (<NUM>) being in fluid communication with said reactor (<NUM>) to receive a stream (<NUM>) and in fluid communication with said membrane unit (<NUM>) to provide a purified stream (<NUM>'). It was found that such washing module (<NUM>) ("scrubber") improves performance of the plant, particularly long term selectivity of the membrane unit is ensured.

Described herein is a polyethylene-production plant comprising a reactor (<NUM>) and a membrane unit (<NUM>), the reactor (<NUM>) being a fluidized bed reactor adapted to convert as chemical grade ethylene feed, the membrane unit (<NUM>) comprising one or more membranes (<NUM>) as defined in claim <NUM>, the membrane unit (<NUM>) being in direct fluid communication with the reactor to receive a stream free of polyethylene. In embodiments, this PE-production plant also contains a washing module (<NUM>) as discussed above.

In one embodiment, the invention provides for manufacturing a membrane (<NUM>) as defined in claim <NUM>.

In embodiments, the invention provides for membranes (<NUM>) obtained by or obtainable by the methods of claim <NUM>.

To further illustrate the invention, the following examples are provided. These examples are provided with no intend to limit the scope of the invention.

Characterization: the main important membrane characterization parameters ideal selectivity (preferred transportation of one gas over another through the membrane) and permeance (pressure and area corrected molar flow through the membrane in GPU, <NUM> GPU = <NUM>-<NUM> cm<NUM> (STP) cm-<NUM> s-<NUM> cmHg-<NUM>), where measured in samples of <NUM><NUM> in a pressure cell. Propylene and propane at <NUM> bar(g) was applied.

A computational simulation was performed to illustrate the recovery of monomer losses that occur in a state-of-the-art polypropylene process. In example II. a, polymer-grade propylene is used while in example II. b, chemical-grade propylene is used.

The base case describes the process of <FIG>, without the membrane separation unit (<NUM>). A total feed (<NUM>) of <NUM> t/h is assumed, an average feed amount for this process, taken from Baker (<CIT>). The olefin losses occur because the corresponding unreactive paraffin has to be removed from the system constantly in order to avoid propane build-up. With the paraffin vapour, a portion of the olefin, typically <NUM>-<NUM> % of the total effluent stream, is lost or has to be recycled by other means. The high olefin amount is derived from the olefin concentration in the polymerization reactor (<NUM>), where a certain olefin concentration has to be reached to ensure optimal reaction rate. The effluent stream (<NUM>) value is composed of the paraffin in the total feed (<NUM>), which corresponds to <NUM>% of the stream, while the remaining <NUM>% are the olefin, mirroring a reactor concentration of <NUM>% monomer. The goal of the system is to remove the paraffin, e.g. propane, that is entering the system with the feed.

The inventive case describes the process of <FIG> with the membrane separation unit (<NUM>) while the base case considers direct recycling without the means of such separation unit (not shown in the figures). The membrane parameters used for the simulations where a propylene over propane selectivity of <NUM> and a propylene permeance of <NUM> GPU, as described example <NUM>.

In Example II. a it is apparent that with the membrane unit the same amount of propane is removed from the system compared to the base case (<NUM>/h each). At the same time, the loss of propylene is more than <NUM> times less (<NUM>/h vs <NUM>/h).

The same applies for example II. Here, the feed is chemical grade propylene with a propylene purity of <NUM> wt%. Again, a base case without membrane separation unit (<NUM>) is compared with an inventive case comprising membrane separation unit (<NUM>), applying the parameters described above in example II.

In Example II. b it is apparent that also by using CGP feed with the membrane unit the same amount of propane is removed from the system compared to the base case (<NUM>/h each). At the same time, the loss of propylene is more than <NUM> times less (<NUM>/h vs <NUM>/h). As can be seen, CGP feed is likewise suitable for the polymerisation reaction.

An experimental set up was established to investigate membrane performance under typical conditions of a state-of-the-art polypropylene process.

To that end, membranes are assembled to a spiral wound module (<NUM> inch in length, membrane area of <NUM> m2). This module was connected to a gas stream comprising propane / propene ( C3H8 <NUM>%/ C3H6 <NUM>% @ <NUM> bar feed pressure). In example III. a, comparative,a propylene membrane (<NUM>) with one functional layer (<NUM>) according to example I. b (ZIF-<NUM>') is used while in example III. b, the same membrane (ZIF-<NUM>') is used, but additional featuring a backing layer (polyamide support layer with a thickness of <NUM> micrometers). The results observed are given in the table below.

Claim 1:
A method for manufacturing a membrane (<NUM>),
the membrane (<NUM>) comprising
• a backing layer (<NUM>) in the form of a mesh and having a thickness of <NUM> - <NUM> micrometers,
• a functional layer (<NUM>) comprising a polymer matrix (<NUM>) and molecular sieves (<NUM>), said functional layer (<NUM>) comprising channels (<NUM>) within said matrix (<NUM>) perpendicular to the membrane surface thereby connecting both surfaces of said membrane and wherein said molecular sieves (<NUM>) are located within said channels (<NUM>),
• optionally a second functional layer containing molecular sieves (<NUM>);
wherein
• the material of said backing layer (<NUM>) is selected from the group consisting of polypropylenes, polyethylenes, poylamides, polyethyleneterephtalates, or polyethersulfones, and
• the material of the polymer matrix (<NUM>) is selected from the group of Polyethersulfones (PES); and
• the molecular sieve (<NUM>) within said functional layer (<NUM>) is modified ZIF-<NUM> having an effective pore size of <NUM>; and
• the molecular sieves (<NUM>) within said optional second functional layer are selected from the group consisting of ZIF-<NUM>, modified ZIF-<NUM> having an effective molecular sieve pore size of <NUM>, ZIF-<NUM>, and ZIF-<NUM>
the method comprising the steps of:
(i) providing a dispersion (<NUM>) consisting of a dispersed phase (<NUM>) and continuous phase (<NUM>)
▪ said dispersed phase (<NUM>) comprising nanoparticles selected from the group consisting of ZnO;
▪ said continuous phase (<NUM>) comprising a polymer, a first solvent and a second solvent;
(ii) coating a substrate (<NUM>) with said dispersion (<NUM>);
(iii) subjecting the obtained material to a phase inversion step by removing said first solvent to thereby obtain a precursor material (<NUM>);
(iv) contacting the obtained precursor material (<NUM>) with a solution (<NUM>) comprising
▪ a solvent selected from the group consisting of water, C1-C8 mono-alcohols optionally in combination with water, dimethylacetamide in combination with water or methanol;
▪ <NUM>-methyl imidazole; and
▪ a Zn-salt soluble in said solvent, preferably Zn(NO3)<NUM>,
(v) optionally removing the obtained composite material (<NUM>) from said substrate (<NUM>) and / or
(vi) optionally further processing the obtained composite material (<NUM>)
to thereby obtain said membrane (<NUM>).