Patent Application
20220306490
This present disclosure relates to a method for isolating carboxylic acid from an aqueous side stream of an organic peroxide production process.
Diacyl peroxides and peroxyesters can be prepared by reacting an anhydride or acid chloride with alkaline solutions of hydro(gen)peroxide, as illustrated by the following equations:
2R—C(═O)—O—C(═O)—R+Na2O2→R—C(═O)—O—O—C(═O)—R+2NaOC(═O)R
R—C(═O)—O—C(═O)—R+ROOH+NaOH→R—C(═O)—O—O—R+NaOC(═O)R
2R—C(═O)Cl+Na2O2→R—C(═O)—O—O—C(═O)—R+2NaCl
R—C(═O)Cl+ROOH+NaOH→R—C(═O)—O—O—R+NaCl
In this reaction scheme, Na2O2 does not refer to a discrete product Na2O2, but to an equilibrium comprising H2O2 and NaOOH.
Acid chlorides are relatively expensive and generate chloride-containing water layers, which lead to waste waters with high salt concentration.
Anhydrides, on the other hand, are even more expensive than acid chlorides and the side stream of the process starting with anhydride contains a high organic load—i.e. a high Chemical Oxygen Demand (COD) value—due to the formed carboxylic acid salt, and is therefore economically and environmentally unattractive.
That would change if the carboxylic acid could be isolated from the aqueous side stream and be re-used; either in a peroxide production process, in another chemical process (e.g. the production of esters), or in any other application, e.g. as animal feed ingredient.
CN108423908 discloses a process to isolate 4-methylbenzoic acid from a bis(4-methylbenzoyl) peroxide production process waste stream by precipitation. However, this process only works for acids with low solubility in water. In addition, the precipitate can cause smearing of the equipment used.
For carboxylic acids that are water-soluble or do not sufficiently precipitate or otherwise separate from the aqueous side stream, isolation is not easy or straightforward.
It is therefore an object of the present disclosure to provide a method for isolating such carboxylic acids from an aqueous side stream of an organic peroxide production process and make it suitable for re-use.
This disclosure provides a method for isolating carboxylic acid from an aqueous side stream of an organic peroxide production process, said method comprising the steps of:
a) providing an aqueous side stream of an organic peroxide production process, said stream comprising at least about 1 wt % of a metal carboxylate, said metal carboxylate being dissolved or homogeneously admixed within said stream,
b) protonating the carboxylate towards carboxylic acid inside the aqueous side stream, thereby forming a biphasic mixture of two liquid phases,
c) separating the biphasic mixture in (i) an aqueous liquid phase comprising water and a minor amount of carboxylic acid and (ii) an organic liquid phase comprising carboxylic acid and a minor amount of water,
d) optionally, separating, preferably distilling, the carboxylic acid from said organic liquid phase,
wherein residual peroxides present in the aqueous side stream are removed by (i) extraction before or after step b) and/or (ii) the addition of a reducing agent, heat or irradiation to said stream, to the biphasic mixture, and/or to the organic liquid phase.
The following detailed description is merely exemplary in nature and is not intended to limit the disclosure or the application and uses of the disclosure. Furthermore, there is no intention to be bound by any theory presented in the preceding background of the disclosure or the following detailed description.
This object is achieved by a process comprising the following steps:
a) providing an aqueous side stream of an organic peroxide production process, said stream comprising at least about 1 wt % of a metal carboxylate, said metal carboxylate being dissolved or homogeneously admixed within said stream,
b) protonating the carboxylate towards carboxylic acid inside the aqueous side stream, thereby forming a biphasic mixture of two liquid phases,
c) separating the biphasic mixture in (i) an aqueous liquid phase comprising water and a minor amount of carboxylic acid and (ii) an organic liquid phase comprising carboxylic acid and a minor amount of water,
d) optionally, separating, preferably distilling, the carboxylic acid from said organic liquid phase,
wherein residual peroxides present in the aqueous side stream are removed by (i) extraction before or after step b) and/or (ii) the addition of a reducing agent, heat or irradiation to said stream, to the biphasic mixture, and/or to the organic liquid phase.
The aqueous side stream is preferably obtained from the production of diacyl peroxides and/or peroxyesters. The organic peroxide production process leading to said aqueous side stream may involve the use of an acid chloride or an anhydride as reactant, preferably an anhydride.
It may be noted that EP 2 666 763 discloses a process to recover carboxylic acid from a magnesium carboxylate mixture by employing an acidic ion exchanger that replaces the magnesium ions in the carboxylate with a proton and in this way provides carboxylic acid. This document however does not relate to recovery from peroxide process streams and also does not involve any further biphasic liquid-liquid separation to recover the carboxylic acid.
Diacyl peroxides can be symmetrical or asymmetrical.
Examples of suitable symmetrical diacyl peroxides are di-2-methylbutyryl peroxide, di-isovaleryl peroxide, di-n-valeryl peroxide, di-n-caproyl peroxide, di-isobutyryl peroxide, and di-n-butanoyl peroxide.
Examples of suitable asymmetrical diacyl peroxides are acetyl isobutanoyl peroxide, acetyl 3-methylbutanoyl peroxide, acetyl lauroyl peroxide acetyl isononanoyl peroxide, acetyl heptanoyl peroxide, acetyl cyclohexylcarboxylic peroxide, acetyl 2-propylheptanoyl peroxide, and acetyl 2-ethylhexanoyl peroxide.
Examples of suitable peroxyesters are tert-butylperoxy 2-ethylhexanoate, tert-amylperoxy 2-ethylhexanoate, tert-hexylperoxy 2-ethylhexanoate, 1,1,3,3-tetramethyl butyl-1-peroxy 2-ethylhexanoate, 1,1,3,3-tetramethylbutyl 1-peroxyneodecanoate, tert-butylperoxy neodecanoate, tert-amylperoxy neodecanoate, tert-hexylperoxy neodecanoate, 1,1,3,3-tetramethylbutyl 1-peroxyneoheptanoate, tert-butylperoxy neoheptanoate, tert-amylperoxy neoheptanoate, tert-hexylperoxy neoheptanoate, 1,1,3,3-tetramethylbutyl 1-peroxyneononanoate, tert-butylperoxy neononanoate, tert-amylperoxy neononanoate, tert-hexylperoxy neononanoate, tert-butylperoxy pivalate, tert-amylperoxy pivalate, tert-hexyl-peroxy pivalate, 1,1,3,3-tetramethyl butyl-1-peroxy pivalate, tert-butylperoxy 3,3,5-trimethylhexanoate, tert-amylperoxy 3,3,5-trimethylhexanoate, tert-hexylperoxy 3,3,5-trimethylhexanoate, 1,1,3,3-tetramethyl butyl-1-peroxy 3,3,5-trimethylhexanoate, tert-butylperoxy isobutyrate, tert-amylperoxy isobutyrate, tert-hexylperoxy isobutyrate, 1,1,3,3-tetramethyl butyl-1-peroxy isobutyrate, tert-butylperoxy n-butyrate, tert-amylperoxy n-butyrate, tert-hexylperoxy n-butyrate, tert-butylperoxy isovalerate, tert-amylperoxy isovalerate, tert-hexylperoxy isovalerate, 1,1,3,3-tetramethyl butyl-1-peroxy isovalerate, tert-butylperoxy n-valerate, tert-amylperoxy n-valerate, tert-hexylperoxy n-valerate, 1,1,3,3-tetramethyl butyl-1-peroxy n-butyrate, 1,1,3,3-tetramethyl butyl 1-peroxy m-chlorobenzoate, tert-butylperoxy m-chlorobenzoate, tert-amylperoxy m-chlorobenzoate, tert-hexylperoxy m-chlorobenzoate, 1,1,3,3-tetramethyl butyl 1-peroxy o-methylbenzoate, tert-butylperoxy o-methylbenzoate, tert-amylperoxy o-methylbenzoate, tert-hexylperoxy o-methylbenzoate, 1,1,3,3-tetramethyl butyl 1-butylperoxy phenylacetate, tert-butylperoxy phenylacetate, tert-amylperoxy phenylacetate, tert-hexylperoxy phenylacetate, tert-butylperoxy 2-chloroacetate, tert-butylperoxy cyclododecanoate, tert-butylperoxy n-butyrate, tert-butylperoxy 2-methylbutyrate, tert-amylperoxy 2-methylburyrate, 1,1-dimethyl-3-hydroxy butyl-1-peroxy neodecanoate, 1,1-dimethyl-3-hydroxy butyl-1-peroxy pivalate, 1,1-dimethyl-3-hydroxy butyl-1-peroxy 2-ethylhexanoate, 1,1-dimethyl-3-hydroxy butyl-1-peroxy 3,3,5-trimethylhexanoate, and 1,1-dimethyl-3-hydroxy butyl-1-peroxy isobutyrate.
Preferred peroxyesters include tert-butylperoxy isobutyrate, tert-amylperoxy isobutyrate, 1,1,3,3-tetramethyl butyl-1-peroxy isobutyrate, tert-butylperoxy n-butyrate, tert-amylperoxy n-butyrate, 1,1,3,3-tetramethyl butyl-1-peroxy n-butyrate, tert-butylperoxy isovalerate, tert-amylperoxy isovalerate, tert-butylperoxy 2-methylbutyrate, tert-amylperoxy 2-methylburyrate, 1,1,3,3-tetramethyl butyl-1-peroxy isovalerate, tert-butylperoxy n-valerate, tert-amylperoxy n-valerate, and 1,1,3,3-tetramethyl butyl-1-peroxy n-valerate.
The aqueous side stream of an organic peroxide production process comprises at least about 1 wt %, preferably at least about 3 wt %, more preferably at least about 5 wt %, more preferably at least about 10 wt %, even more preferably at least about 20 wt %, and most preferably at least about 25 wt % of a metal carboxylate dissolved or homogeneously admixed therein. The metal carboxylate concentration is preferably not more than about 50 wt %, more preferably not more than about 40 wt %, and most preferably not more than about 35 wt %.
The metal carboxylate is dissolved or homogeneously admixed with said stream, meaning that the stream includes a single phase and is not, e.g., a suspension containing metal carboxylate particles. From such a suspension, the carboxylic acid could be easily separated by, e.g., filtration of the metal carboxylate. From the aqueous stream of the present disclosure, however, such easy separation is not possible and more steps are required to isolate the carboxylic acid.
Apart from water and the metal carboxylate, the aqueous side stream will contain some peroxide residues, such as organic hydroperoxide, hydrogen peroxide, peroxyacid, diacyl peroxide, and/or peroxyester. The peroxide content of the aqueous side stream will generally be in the range from about 0.01 to about 3 wt %. The side stream may further contain some residual peroxide decomposition products.
In order to successfully isolate, purify, and re-use the carboxylic acid, any residual peroxides have to be removed from the aqueous side stream. This is done by extraction and/or the addition of a reducing agent. In addition, heating of the side stream may be desired.
Examples of suitable reducing agents are sodium sulfite, sodium (poly)sulfide (Na2Sx), sodium thiosulfate, and sodium metabisulfite.
Reducing agent is added to the aqueous side stream, to the biphasic mixture, and/or to the organic liquid phase. In a preferred embodiment, reducing agent is added to the aqueous side stream, either during step b) or, more preferably, before step b).
The reducing agent will destroy hydrogen peroxide, organic hydroperoxides, and peroxy acids. In order to destroy any other peroxidic species, it may be desired to increase the temperature of the aqueous side stream with from about 10 to about 80° C., preferably from about 10 to about 50° C., and most preferably from about 10 to about 30° C. This temperature increase can be performed before step b) or during step b). If performed during step b), any heat that is liberated by the protonation (e.g. acidification) may be used to achieve this temperature increase.
It should be noted that the temperature of the aqueous side stream before heating or protonation is generally in the range from about 0 to about 20° C., preferably from about 0 to about 10° C., as peroxide production processes are often performed at low temperatures.
Extraction can be performed before or after step b), and is preferably performed before step b). Extraction can be performed with organic solvents, anhydrides, and mixtures of anhydride and solvent.
Examples of suitable solvents for the extraction are alkanes (e.g. isododecane, Spiridane® and Isopar® mineral oils), chloroalkanes, esters (e.g. ethyl acetate, methyl acetate, dimethylphthalate, ethylene glycol dibenzoate, cumene, dibutyl maleate, di-isononyl-1,2-cyclohexaendicarboxylate (DINCH), dioctyl terephthalate, or 2,2,4-trimethylpentanediol diisobutyrate (TXIB)), ethers, amides, and ketones.
Examples of suitable anhydrides are anhydrides that were or can be used in the organic peroxide production process and include symmetrical and asymmetrical anhydrides.
Examples of symmetrical anhydrides are n-butyric anhydride, isobutyric anhydride, pivalic anhydride, valeric anhydride, isovaleric anhydride, 2-methylbutyric anhydride, 2-methylpentanoic anhydride, 2-methylhexanoic anhydride, 2-methylheptanoic anhydride 2-ethylbutyric anhydride, caproic anhydride, caprylic anhydride, isocaproic anhydride, n-heptanoic anhydride, nonanoic anhydride, isononanoic anhydride, 3,5,5-trimethylhexanoic anhydride, 2-propylheptanoic anhydride, decanoic anhydride, neodecanoic anhydride, undecanoic anhydride, neoheptanoic anhydride, lauric anhydride, tridecanoic anhydride, 2-ethylhexanoic anhydride, myristic anhydride, palmitic anhydride, stearic anhydride, phenylacetic anhydride, cyclohexanecarboxylic anhydride, 3-methyl-cyclopentanecarboxylic anhydride, and mixtures of two or more of the above-mentioned anhydrides.
Examples of suitable mixtures of symmetrical anhydrides are the mixture of isobutyric anhydride and 2-methylbutyric anhydride, the mixture of isobutyric anhydride and 2-methylpentanoic anhydride, the mixture of 2-methylbutyric anhydride and isovaleric anhydride, and the mixture of 2-methylbutyric anhydride and valeric anhydride.
Asymmetrical anhydrides are usually available as a mixture of the asymmetrical and symmetrical anhydrides. This is because asymmetrical anhydrides are usually obtained by reacting a mixture of acids with, e.g., acetic anhydride. This leads to a mixture of anhydrides, including an asymmetrical and at least one symmetrical anhydride. Such mixtures of anhydrides can be used for the extraction. Examples of suitable asymmetrical anhydrides are isobutyric 2-methylbutyric anhydride, which is preferably present as admixture with isobutyric anhydride and 2-methylbutyric anhydride; isobutyric acetic anhydride, which is preferably present as admixture with isobutyric anhydride and acetic anhydride, 2-methylbutyric valeric anhydride which is preferably present as admixture with 2-methylbutyric anhydride and valeric anhydride; and butyric valeric anhydride, which is preferably present as admixture with butyric anhydride and valeric anhydride.
More preferred anhydrides are isobutyric anhydride, 2-methylbutyric anhydride, 2-methylhexanoic anhydride, 2-propylheptanoic anhydride, n-nonanoic anhydride, isononanoic anhydride, cyclohexanecarboxylic anhydride, 2-ethylhexanoic anhydride, caprylic anhydride, n-valeric anhydride, isovaleric anhydride, caproic anhydride, and lauric anhydride. Most preferred are isononanoic anhydride and isobutyric anhydride.
In step b), the carboxylic acid is liberated by protonation. Protonation leads to a biphasic mixture of two liquid phases. In other words: it does not lead to precipitation of the carboxylic acid which could then be easily separated from the mixture by, e.g., filtration. Instead, from the mixture of the present disclosure, such easy separation is not possible, and more steps are required to isolate the carboxylic acid.
In one embodiment, protonation is achieved by acidification of the aqueous side stream.
Preferred acids for acidifying and protonating the carboxylic acid are acids with a pKa below about 5, such as H2SO4, HCl, NaHSO4, KHSO4, formic acid, acetic acid, and combinations thereof. More preferably, an acid with a pKa below about 3 is used; most preferably H2SO4 is used. If H2SO4 is used, it is preferably added as an about 90 to about 96 wt % solution.
Acidification is preferably performed to a pH below about 6, more preferably below about 4.5, and most preferably below about 3. The resulting pH is preferably not lower than about 1.
Depending on the acid used, the temperature of the stream may increase during this step, up to about 80° C.
Acidification leads to the formation of a biphasic mixture comprising (i) an aqueous layer comprising water and a minor amount of carboxylic acid and (ii) an organic liquid phase comprising carboxylic acid and a minor amount of water.
The salt that results from the acidification—e.g. Na2SO4, K2SO4, NaHSO4, KHSO4, NaCl, Na formate, or Na acetate, depending on the acid used for acidification and the base used during the organic peroxide production—will be mainly present in the aqueous liquid phase, although a minor amount may also be present in the organic liquid phase.
In this document a minor amount is defined as from about 0 to about 2 wt % based on total weight, preferably less than about 1 wt %, more preferably less than about 0.5 wt %, more preferably less than about 0.1 wt %, more preferably less than about 0.01 wt % and most preferably less than about 0.001 wt %.
In another embodiment, protonation is achieved by electrochemical membrane separation. Examples of electrochemical membrane separation techniques are membrane electrolysis and bipolar membrane electrodialysis (BPM). BPM is the preferred electrochemical membrane separation method.
Electrochemical membrane separation leads to splitting of the metal carboxylate in carboxylic acid and metal hydroxide (e.g. NaOH or KOH) and separation of both species. It thus leads to (i) a carboxylic acid-containing mixture and (ii) a NaOH or KOH solution, separated by a membrane.
The NaOH or KOH solution can be re-used in the production of organic peroxides or any of the steps of the process of the present disclosure where a base is required or desired.
Depending on the temperature, the salt concentration, and the solubility of the carboxylic acid in water, the carboxylic acid-containing mixture can be a biphasic mixture of two liquid phases or a homogeneous mixture. If a homogeneous mixture is formed under the electrochemical membrane separation conditions (generally from about 40 to about 50° C.), cooling of the mixture to temperatures below about 30° C. and/or the addition of salt will ensure that a biphasic mixture will be formed. The organic liquid layer of this biphasic carboxylic acid-containing mixture can then be separated from the aqueous layer of said biphasic mixture in step c).
Optionally, a solvent is added to the biphasic mixture.
Examples of suitable solvents are (mixtures of) alkanes like isododecane, Spirdane®, Isopar®, octane, decane, toluene, o-, m-, p-xylene, esters like dimethylphthalate, long chain acetates, butyl acetate, ethyl butyrate, cumene, trimethyl pentanyl diisobutyrate (TXIB), adipates, sebacates, maleates, trimellitates, azelates, benzoates, citrates, and terephthalates, ethers like methyl tert-butyl ether (MTBE), and carbonates like diethyl carbonate.
Alkanes and mixtures of alkanes are the preferred solvents. Isododecane is the most preferred solvent.
The addition of solvent is particularly desired if the carboxylic acid is to be re-used in a process in which said solvent is desirably present, so that the solvent does not need to be removed from the carboxylic acid before such re-use. Examples of such processes are organic peroxide production processes, in which safety considerations often require the presence of solvent.
In step c), the liquid phases are separated.
Separation can be performed by gravity, using conventional separation equipment, such as a liquid/liquid separator, a centrifuge, a (pulsed and or packed) counter current column, (a combination of) mixer settlers, or a continues (plate) separator.
In some embodiments, the separation can be facilitated by salting out the organic liquid phase with a concentrated salt solution, e.g. a 20 to about 30 wt % NaCl, NaHSO4, KHSO4, Na2SO4, or K2SO4 solution. The salt reduces the solubility of the carboxylic acid in the aqueous liquid phase. This extraction can be performed in any suitable device, such as a reactor, centrifuge, or mixer-settler.
The preferred separation method in step c) is gravity separation, instead of extraction.
Irrespective of how the phases are separated in step c), a separation or distillation step d) is preferred to further purify the carboxylic acid. Distillation is especially preferred for the purification of carboxylic acids with less than five carbon atoms and for organic liquid phases with a water content of about 5 wt % or more. For lower water contents, drying with a molecular sieve or drying salt can be performed to remove water.
The distillation may serve to evaporate volatile impurities, including water, from the carboxylic acid and/or to distill the carboxylic acid from any impurities with a boiling point higher than that of the carboxylic acid.
The term “distillation” in this specification includes any form of removal of components by vaporization. Hence, it also includes stripping and similar techniques.
Between separation step c) and separation or distillation step d), it may be desired to remove any salts—that resulted from the acidification—from the organic liquid phase, in order to prevent settling of solids in the distillation column.
Removal of salt can be done by washing with water, cooling (e.g. freezing), and separating off the resulting water layer. Cooling is preferably performed to <about 20° C., more preferably <about 10° C., and most preferably <about 5° C. and will force salts into the water layer.
The isolated water layer can be recycled to the protonation step.
The water content of the obtained carboxylic acid is preferably below about 2 wt %, more preferably below 1 wt %, even more preferably below about 0.5 wt %, and most below about 0.1 wt %. This is especially preferred in case the carboxylic acid will be re-used in a peroxide production process. A further distillation of the carboxylic acid may be required to reach this water content.
The aqueous liquid phase formed as a result of protonation step b) may contain some residual carboxylic acid. This holds in particular for lower molecular weight acids, like butyric, isobutyric, pentanoic, and methyl- or ethyl-branched pentanoic acids. This residual acid can be recovered by adsorption, (azeotropic) distillation, or extraction, preferably distillation. Optionally, a salt (e.g. sodium sulfate) can be added to the recovered carboxylic acid as an aqueous liquid distillate, in order to lower the solubility of the carboxylic acid. In order to further optimize the carboxylic acid yield, the recovered residual carboxylic acid distillate can be recycled within the process by adding it to the above-mentioned aqueous side stream, after protonation step b) and before separation step c).
Preferred carboxylic acids to be obtained by the process of the present disclosure include isobutyric acid, n-butyric acid, propionic acid, pivalic acid, neodecanoic acid, neoheptanoic acid, isononanoic acid, 2-methylbutyric acid, cyclohexylcarboxylic acid, lauric acid, isovaleric acid, n-valeric acid, n-hexanoic acid, 2-ethylhexanoic acid, heptanoic acid, 2-propylheptanoic acid, octanoic acid, nonanoic acid, decanoic acid, and lauric acid. More preferred carboxylic acids are isobutyric acid, n-butyric acid, n-heptanoic acid, n-octanoic acid, pivalic acid, isononanoic acid, 2-methylbutyric acid, cyclohexylcarboxylic acid, isovaleric acid, and n-valeric acid.
The carboxylic acid obtained from the process of the present disclosure can be recycled to the organic peroxide production process from which it originated, it can be used in the production of another organic peroxide, and it can be used to make esters (for instance ethyl esters) that find use as, e.g., solvent or fragrance, or in agricultural applications.
The carboxylic acid—or a salt thereof—can also be used in animal feed. For instance, butyric acid salts are known to improve gastrointestinal health in poultry and prevent microbial infections and ailments in poultry, pigs, fishes, and ruminants.
An aqueous side stream of a di-isobutyryl peroxide process containing 23 wt % sodium isobutyrate, 300 ppm di-isobutyryl peroxide and 0.1 wt % perisobutyric acid, having a temperature of 0° C. and a pH of about 10, was treated as follows:
A constant flow of said stream was passed through a column with four stirred sections and kept at a temperature of from about 20-25° C. The residence time was about 5 minutes per section. A 30 wt % Na2SO3 solution was added to said column, thereby reducing the perisobutyric acid in said stream and producing a stream with <50 ppm of residual peroxide.
The resulting stream was collected in a container.
From the container, 8.2 kg of said stream was charged to a 10 l glass reactor, equipped with a cooling mantle, a pitch blade impeller, and a thermometer. To the stirred contents, 810.4 g of H2SO4-96 wt % was added in 2 minutes in order to reduce the pH to 2.3. A temperature increase to 42° C. was noticed. After 5 minutes of stirring, the layers were allowed to separate by gravity. The two phases were separated, thereby obtaining 7.6 kg of aqueous liquid phase and 1.4 kg of organic liquid phase.
Cooling of the organic phase to 2° C. resulted in a separation of 40 g of additional aqueous phase, which was then combined with the 7.6 kg aqueous liquid phase.
The organic liquid phase, mainly comprising wet isobutyric acid, was fed to a continuous distillation column. The bottom stream contained >99 wt % isobutyric acid with a water content of 200 ppm.
The aqueous liquid phase was charged to a 10 l glass reactor and an aqueous solution of isobutyric acid in water was distilled off at 55° C. and <160 mbar. The residue was an aqueous Na2SO4 solution.
In order to further optimize the isobutyric acid yield, this aqueous isobutyric acid solution was recycled within the process by adding it to the above-mentioned aqueous side stream, after the acidification with H2SO4 and before gravity separation of the resulting layers.
While at least one exemplary embodiment has been presented in the foregoing detailed description, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the various embodiments in any way. Rather, the foregoing detailed description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment as contemplated herein. It being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the various embodiments as set forth in the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 19179625.9 | Jun 2019 | EP | regional |
This application is a U.S. National-Stage entry under 35 U.S.C. § 371 based on International Application No. PCT/EP2020/066232, filed Jun. 11, 2020 which was published under PCT Article 21(2) and which claims priority to European Application No. 19179625.9, filed Jun. 12, 2019, which are all hereby incorporated in their entirety by reference.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2020/066232 | 6/11/2020 | WO |
