Process involving cross metathesis of olefins

A method of forming a macrocyclic musk compound comprising the steps of:—

This patent application claims the full priority benefit of PCT/EP2015/055343 filed 13 Mar. 2015, and to the earlier filed priority application, GB 1404468.9 filed 13 Mar. 2014. The entirety of the foregoing documents are herein incorporated by reference.

The present invention is concerned with a process for the preparation of macrocyclic musk compounds utilizing a cross metathesis reaction. The invention is also concerned with novel intermediates useful in said process of forming macrocyclic musk compounds.

The odour of musk is perhaps the most universally appreciated fragrance. Synthetic musks can be divided into three major classes—aromatic nitro musks, polycyclic musk compounds, and macrocyclic musk compounds. The detection of the nitro- and polycyclic chemical groups in human and environmental samples initiated a public debate on the use of these compounds. Some research has indicated that these musk compounds don't break down in the environment and can accumulate in human bodies. As such, macrocyclic musk compounds have increased in importance in recent years.

7-Ambrettolide naturally occurs in musk ambrette seed oil (M. Kerschbaum, Chem Ber. 1927, 60B, 902) and is a valuable perfume base because of its desirable odour. 9-Ambrettolide is likewise a much appreciated perfumery ingredient (C. Collaud, Helv. Chim. Acta 1942, 25, 965). It is currently synthesized industrially from aleuritic acid. However, aleuritic acid is obtained from shellac by saponfication, and due to growing industrial concerns regarding the supply and price of shellac, there is a need to devise new synthetic routes into the highly valued and valuable 9-ambrettolide.

Olefin metathesis has become an important tool in the field of synthetic organic chemistry. A variant of olefin metathesis—so-called cross metathesis—is the reaction of two different olefins in the presence of an organometallic catalyst, in which one olefin double bond changes places with the other. More particularly, it is an organic reaction that entails the redistribution of fragments of olefins by the scission and regeneration of carbon-carbon double bonds.

The mechanism of this reaction is thought to proceed via a 2+2 cycloaddition of an alkene-bearing substrate to a metal alkylidene catalyst, forming a metallocyclobutane intermediate, which undergoes cycloreversion to generate the substrate loaded with a metal carbene, which further reacts with a second alkene to produce the metathesis product and releases the metal alkylidene catalyst.

Schematically, an olefin metathesis reaction can be represented as follows:

The reaction can be used to couple together two olefin substrates to form a new olefin compound, which is a dimer of the two substrates. The reaction is shown schematically, above. The A-containing substrate and the B-containing substrate can react to form a hetero-dimer (shown), however, the both the A-containing substrate and the B-containing substrate can react with itself to form homo-dimers.

Another variant of the olefin metathesis reaction is the so-called ring closure metathesis reaction (RCM). This reaction is widely established as a means of forming ring structures. The reverse reaction can be employed to ring-open a cyclic structure:

RCM is simply an intramolecular olefin metathesis of a diene, yielding a cycloalkene and a volatile alkene by-product (ethylene, in the case of the above schematic). RCM has been widely researched as a means of producing macrocycles. Indeed, a laboratory procedure utilizing a ring closure metathesis (RCM) reaction using a ruthenium alkylidene catalyst has been reported in the literature (J. Am. Chem. Soc. 2013, 135, 94; Chem. Europ. J. 2013, 19, 2726-2740, J. Org Chem. 1996, 61, 3942-3943, and WO 2012167171). However, a problem with RCM is that the intra-molecular ring closing reaction is in competition with inter-molecular polymerisation reactions, and the former is favoured only in high dilution, and so for reasons of economy this chemistry has not found use industrially as a means of producing macrocyclic musk compounds to the best of the applicant's knowledge.

In contrast to the greatly researched ring closure metathesis reaction, the cross metathesis reaction has been relatively under studied. Difficulties abound with this chemistry. Catalyst-induced migration of the double bonds on the starting materials represents a consistent challenge. Furthermore, differences in reactivity of the olefin groups of the starting materials can lead to poor yields of the desired product. Still further, the inevitable complex mixture containing homo-dimers and hetero-dimers can be difficult, time consuming and expensive to separate and isolate in pure form, particularly when the reaction and purification must be industrially scalable.

The present invention addresses the problems in the prior art and provides an efficient and high-yielding synthesis of macrocyclic musk compounds and their open-chain intermediates, utilizing cross metathesis.

Accordingly, the invention provides in a first aspect a method of forming a macrocyclic musk compound comprising the steps of cross metathesizing a first olefin and a second olefin in the presence of a homogeneous transition metal catalyst containing an alkylidene ligand, to form a hetero-dimer intermediate of said first and second olefin, and cyclizing the hetero-dimer intermediate to form the macrocyclic musk compound.

In a particular embodiment of the present invention, one or both of first and second olefins may be olefins with a terminal double bond.

In a particular embodiment of the invention, the first step in the preparation of the macrocyclic musk compound, wherein the first and second olefins are reacted in a cross metathesis reaction to produce the hetero-dimer intermediate is shown schematically below.

The group R contains a protected hydroxyl group containing 3 to 10 carbon atoms; R1is a carboxylic ester group containing 3 to 11 carbon atoms; wherein the number of carbon atoms in the ester group and protected hydroxyl group together should be less than 15; and wherein M=represents a transition metal catalyst containing an alkylidene ligand.

One of said first or second olefins may be represented by the formula (I)

wherein OR2is a protected hydroxyl group, which may be selected from an alkyl ether group; an ester group; a silyl ether group; or a carbonate group; R3is H or methyl; and n is an integer from 1-8.

Suitable ether protecting groups include a branched or non-branched alkyl moiety containing 1 to 5 carbon atoms, for example methyl, ethyl, propyl, i-propyl, t-Bu or t-amyl.

Suitable ester protecting groups include C(O)R4, wherein R4=hydrogen, or a branched or non-branched alkyl moiety containing 1 to 7 carbon atoms, for example methyl, ethyl, propyl, i-propyl, t-butyl or t-amyl. Suitable silyl ether protecting groups include Si(R5)3; wherein R5is a branched or unbranched alkyl moiety, which may include methyl, ethyl and propyl and t-butyl.

Suitable carbonate protecting groups include C(O)OR6, wherein R6is a branched or non-branched alkyl moiety, for example methyl, ethyl or propyl.

The other of said first or second olefins may be represented by the formula (II)

wherein R7is branched or non-branched alkyl moiety containing 1 to 5 carbon atoms, and preferably methyl or ethyl, and m is an integer from 1 to 10, preferably 7.

When first and second olefins specifically referred to above in formula (I) and (II) are subjected to a cross metathesis reaction in accordance with the present invention, the hetero-dimer intermediate can be represented by the formula (III)

wherein R2, R7, m and n are as hereinabove defined, and wherein the configuration of the double bond may be E or Z as desired.

The hetero-dimer intermediates herein defined, as well as their preparation by cross metathesis each represent further aspects of the present invention.

In a particular embodiment of the present invention, the hetero-dimer intermediate is a compound represented by the formula (IV)

wherein R7is as hereinabove defined, in particular methyl.

The advantages of the t-Bu ether protecting group are manifold, and lead to an over-all efficiency of the synthesis of macrocyclic musks. In particular, the t-Bu protecting group is advantageous because it results in a hetero-dimer product that can be relatively easily separated from homo-dimer side products formed in the cross metathesis reaction by distillation at relatively low temperatures, e.g. below about 100 to 220 degrees centigrade at a pressure of about 1 to 10 mbar. Furthermore, this hetero-dimer is relatively easy to cleave under mild conditions during the subsequent macrocyclization step to form the macrocyclic musk.

After completion of the metathesis reaction, the hydroxyl protecting group can be cleaved by various synthetic procedures depending on the nature of the protecting group, all of which are well known to a person skilled in the art. The resultant α-ω hydroxy ester can be cyclized to form a macrocyclic lactone. In the particular case of a α-ω hydroxy esters represented in protected form (IV) above, the corresponding macrocyclic musk compound is the lactone E/Z 9-ambrettolide (structure shown below).

When the protecting group is an ester, the hetero-dimer formed by the metathesis reaction can be immediately submitted to the macrocyclization reaction without prior cleavage of the protecting group. Examples of the synthetic steps do not need to be exhaustively explained here, and are more specifically described in the examples, below.

Thereafter, the macrocyclization reaction may be carried out according to techniques known in the art. A particular method of carrying out the cyclization step proceeds via the formation of a polyester from a hydroxy ester, which is the unprotected hetero-dimer of the metathesis reaction, and continuously trans-esterifying the polyester into volatile lactones and removing them at higher temperature and reduced pressure once the lactone is formed according to the well-known Collaud chemistry disclosed U.S. Pat. No. 2,234,551, which is herein incorporated by reference. Further details regarding this chemistry are set forth in the examples hereinbelow.

Whereas a hetero-dimer intermediate described above can be cyclized to form 9-ambrettolide, the skilled person will appreciate that with the appropriate selection of olefin starting materials, in particular unsaturated protected alcohol and unsaturated carboxylic acid ester, the cross metathesis reaction will form hetero-dimers that can be subsequently transformed by macrocyclization to form other macrocyclic musk compounds such as 7-Ambrettolide

or Habanolide

or Nirvanolide

For example, the first and second olefin compounds that can be used to form 7-ambrettolide may be selected from 10-(tert-butoxy)dec-1-ene and methyl oct-7-enoate or dec-9-en-1-yl acetate and methyl oct-7-enoate.

The first and second olefin compounds that can be used to form Habanolide may be selected from trimethyl(pent-4-en-1-yloxy)silane and ethyl dodec-11-enoate.

The first and second olefin compounds that can be used to form Nirvanolide may be selected from 4-methyl-6-(tert-butoxy)hex-1-ene and methyl 9-decenoate, or 4-methyl-6-(tert-butoxy)hex-1-ene and ethyl 9-decenoate, or 3-methylhex-5-en-1-yl propionate and methyl 9-decenoate.

The cross metathesis reaction conditions required to conjoin the two olefins are generally well known in the art. The reaction may proceed at room temperature or at elevated or lowered temperatures, for example between 0 to 60 degrees centigrade.

Whereas in ring closure metathesis reactions to form macrocycles, it is necessary to carry out the reaction in very high dilutions (for example, 10−2to 10−4M solutions), in contrast applicant has found that in the present invention the cross metathesis reaction will proceed at high concentrations, and indeed the reaction may even be carried out with no solvent present. As such, the method of the present invention, whereby a hetero-dimer is first formed by metathesis, and then ring-closed by a macrocyclization step, represents a considerably simpler and cheaper process than RCM to form macrocyclic musk compounds, which is industrially scalable in an economic manner.

Elimination of solvent from a reaction mixture has very obvious economic advantages for the industrialization of a synthetic procedure. An additional advantage related to the reduction or avoidance of a solvent, particularly in relation to the use of metathesis catalysts that may be water and oxygen sensitive, is that there is one less reagent that needs to be conditioned or purified before use to eliminate trace contaminants such as moisture and reactive oxygen, such as in the form of peroxides.

In a particular aspect of the present invention, feed stock containing first or second olefin compounds can be subjected to a purification step prior to their reaction by cross metathesis. Purification entails the removal of contaminants from said feed stocks containing the olefin compounds that could otherwise negatively affect the reactivity of metathesis catalysts. Such contaminants may include water, alcohols, aldehydes, peroxides, hydroperoxides, protic materials, polar materials, Lewis base (basic) catalyst poisons and two or more thereof. Purification may entail a physical purification step, for example, a distillation step, or a step whereby the olefin compounds are separated from unwanted contaminants by a process of absorption. Physical purification means may include heat (such as, in a distillation process), or contact of the feed stocks with absorbent materials selected from molecular sieves, alumina, silica gel, montmorillonite clay, Fuller's earth, bleaching clay, diatomaceous earth, zeolites, kaolin, activated metals, metal sulfates, metal halides, metal silicates, activated carbon, and soda ash.

Additionally or alternatively, purification may entail a chemical purification step, whereby unwanted contaminants are separated from the feed stocks by subjecting the contaminants to a chemical reaction, whereby they are converted to materials that are non-reactive with a metathesis catalyst. Chemical purification means include treating the feed stocks with metal carbonates and metal hydrogen carbonates, acid anhydrides, metal hydrides, phosphorous pentoxide, metal aluminum hydrides, alkyl aluminum hydrides, trialkyl aluminums, metal borohydrides, organometallic reagents, metal amides, and combinations thereof. Contaminants may be compounds that contain at least one proton that can react with a compound selected from the group consisting of metal carbonates and metal hydrogen carbonates, acid anhydrides, metal hydrides, phosphorous pentoxide, metal aluminum hydrides, alkyl aluminum hydrides, trialkyl aluminums, metal borohydrides, organometallic reagents, metal amides, and combinations thereof.

Purification may also be performed by contacting feed stock with materials selected from the group consisting of molecular sieves, activated alumina, activated acidic alumina, neutral alumina, any one of which may be optionally heat treated; and activated basic alumina, alkaline earth metal hydrides, alkaline earth metal sulfates, alkali metal sulfates, alkali earth metal halides, alkali metal aluminum hydrides, alkali metal borohydrides, Grignard reagents; organolithium reagents, trialkyl aluminums, metal bis(trimethylsilyl)amides, and combinations thereof.

Purification may also be carried out by subjecting feed stock to an anhydride of an organic acid. Suitable anhydrides are preferably the anhydrides of aliphatic, cyclic, alicyclic organic acids having from 1 to 10 carbon atoms, or an aromatic organic acid having from 6 to 10 carbon atoms. Such compounds are known in the art or may be produced according to known methods. A particularly useful organic anhydride is acetic anhydride.

Purification may also be carried out by subjecting feed stock to an organometallic compound of aluminum. Said organometallic compound of aluminum may be a tri-substituted aluminium compound wherein the substituents are independently selected from an aliphatic, cyclic, alicyclic residue having from 1 to 10 carbon atoms, or from aromatic residues having from 6 to 10 carbon atoms. Such compounds are known in the art or may be produced according to known methods.

Trioctyl aluminum is particularly preferred since it is stable in contact with air, i.e. is not-flammable in contact with air, which is not the case with triethyl aluminum. This renders it particularly suitable for applications at an industrial scale.

For the practical realization of a chemical purification step, the amount of contaminant may be determined by known methods, such as chromatographic methods. Thereafter, the theoretical amount of purification means needed to react with the contaminant and render it inactive to a catalyst can be easily calculated, and can be employed in slight molar excess in order to ensure that all potentially harmful contaminant is reacted to render it inactive towards a catalyst. If desired, after the reaction with contaminant, any excess purification means can be removed.

After purification, feedstock containing first and/or second olefin compounds useful in the present invention may have a level of purity that is at least 99.9% by weight of the first and/or the second olefin, or at least 99.99% by weight, or at least 99.999% by weight.

Several different and complementary means of purification of a contaminated feedstock comprising said first and/or said second olefin compounds can be carried out prior to a metathesis reaction according to the invention. The following non-exhaustive and non-limiting list of representative purification methodologies can be usefully employed, for example (a) thermal treatment—for example, heating (and/or distilling) a feed stock at a temperature of between about 100° C. and about 250° C., depending on the boiling point of a feed stock, optionally with a purge of an inert gas or under vacuum, and/or treatment with an adsorbent material referred to hereinabove can be useful both in decomposing peroxide contaminants and/or decomposition products thereof or adsorbing contaminants; (b) treatment with an acid anhydride (e.g., acetic anhydride, Ac2O) can be useful in removing moisture, active hydroxyl-containing materials (e.g., alcohols), and hydroperoxides (via acetylation); (c) treatment with a desiccant (e.g., silica gel, alumina, molecular sieves, magnesium sulfate, calcium sulfate, and the like, and combinations thereof) and/or an organometallic reagent (e.g., t-butyl lithium, triethyl aluminum, tributyl aluminum, triisobutyl aluminum, triisopropyl aluminum, trioctyl aluminum, and the like, and combinations thereof) and/or metal hydrides (e.g., CaH2and the like) and/or acid anhydrides (e.g., acetic anhydride and the like) can be useful in removing moisture; (d) treatment with an adsorbent (e.g., alumina, silica gel, and the like, and combinations thereof) and/or an organometallic reagent (e.g., t-butyl lithium, triethyl aluminum, tributyl aluminum, triisobutyl aluminum, triisopropyl aluminum, trioctyl aluminum, and the like, and combinations thereof) and/or a metal amide (e.g., LDA, KHMDA, and the like) can be useful in removing protic materials; (e) treatment with an adsorbent (e.g., alumina, silica gel, activated charcoal, and the like, and combinations thereof) can be useful in removing polar materials; and (f) treatment with an organometallic reagent (e.g., t-butyl lithium, triethyl aluminum, tributyl aluminum, triisobutyl aluminum, triisopropyl aluminum, trioctyl aluminum, and the like, and combinations thereof) can be useful in removing Lewis basic catalyst poisons or the like.

In some embodiments, the means used to purify said feedstock prior to a metathesis reaction comprises an adsorbent which, may be selected from the group consisting of silica gel, alumina, bleaching clay, activated carbon, molecular sieves, zeolites, Fuller's earth, diatomaceous earth, and the like, and combinations thereof. In some embodiments, the means is selected from the group consisting of optionally heat-treated molecular sieves, optionally heat-treated alumina, and a combination thereof. In some embodiments, the adsorbent comprises optionally heat-treated activated alumina which, may be selected from the group consisting of optionally heat-treated activated acidic alumina, optionally heat-treated activated neutral alumina, optionally heat-treated activated basic alumina, and combinations thereof. In some embodiments, the absorbent comprises optionally heat-treated activated neutral alumina, which can be useful in treating substrates (e.g., olefins) that are susceptible to acid-catalyzed isomerization and/or rearrangement.

For embodiments in which the means for purification comprises an adsorbent (e.g., molecular sieves, alumina, etc.), it is presently believed that the treating of the feedstock with the adsorbent is more effectively performed by flowing the feedstock through the means for purification using a percolation- or flow-type system (e.g., chromatography column) as opposed to simply adding the adsorbent to the substrate in a container. In some embodiments, about 20 wt % of alumina is used in a column. In particular, it may be particularly advantageous to treat a feedstock with alumina on about a 5-to-1 weight-to-weight basis. However, it is to be understood that the amount of alumina used is not restricted and will be both feedstock- and impurity dependent in addition to being impacted by the form of the alumina, its activation process, and the precise treatment method (e.g., flow through a column vs. direct addition to container). In some embodiments, the means used for purifying the feedstock prior to a metathesis reaction comprises a trialkyl aluminum which, in some embodiments, is selected from the group consisting of triethyl aluminum, tributyl aluminum, triisobutyl aluminum, triisopropyl aluminum, trioctyl aluminum, and the like, and combinations thereof.

It has further been unexpectedly found that the purification period of the feed stock may significantly influence efficacy of the chemical purification step. Accordingly, prolonged purification periods may improve catalytic activity of the compounds used as catalysts in the metathesis reactions according to the invention.

In one embodiment, preferably when a trialkyl aluminum compound is used for purification, preferably trioctyl aluminum, the feedstock is subjected to said compound for a period of from 2 to 100 h, preferably 5 to 90 h, more preferred 10 to 80 h, and still more preferred 15 to 70 h.

Catalysts for effecting metathesis reactions are well known in the art. Generally, olefin metathesis catalysts are organometallic catalysts bearing a transition metal atom, such as titanium (Ti), tantalum (Ta), ruthenium (Ru), molybdenum (Mo) or tungsten (W). Whilst varying considerably in terms of the ligands bound to the metal atom, all of the effective catalyst systems share the basic metal alkylidene or alkylidyne ligand structure. Reviews of metathesis catalysts useful in the present invention are described in Michrowska et al Pure Appl. Chem., vol 80, No. 1, pp 31-43 2008; Schrock et al Chem. Rev. 2009, 109, 3211-3226; and Grubbs et al J. Am. Chem. Soc. 2011, 133, 7490-7496. Suitable catalysts are also described in the patent literature, for example in US 2013/0281706 and U.S. Pat. No. 6,306,988.

The variety of substituents or ligands that can be employed in the catalysts means that there are, today, a wide variety of catalysts available. Ligands or substituents may be selected to affect catalyst stability or selectivity (chemo-, regio- and enantio-selectivity), as well as turn over number (TON), and turn over frequency (TOF). As is well known in the art, the TON describes the degree of activity of a catalyst, i.e. the average number of substrate molecules converted per molecule of catalyst, whereas TOF is a representation of catalyst efficiency (in units 0).

Particularly useful catalysts in the metathesis reaction of the present invention are those metal alkylidene catalysts wherein the metal atom is either a Ruthenium, Molybdenum or Tungsten atom. Most preferred are said catalysts wherein the metal atom is Molybdenum or Tungsten.

Preferred Molybdenum or Tungsten catalysts are represented by the general formula

wherein

X═O and R6is aryl, which are optionally substituted; or

X═S and R6is aryl, which are optionally substituted; or

or R4and R5are linked together and are bound to M via oxygen, respectively

Particularly preferred metathesis catalysts are set forth below.

The selection of the catalyst may have significant effects on both the efficiency of the metathesis reaction, characterized by the catalyst loading in ppm, as well as on the diastereoselectivity, i.e. the E/Z ratio of the double bond in the macrocyclic ring. For instance, catalysts X052, X061, X123 and X190 are preferred catalysts for the synthesis of E9-Ambrettolide. These catalysts generally generate high E-selectivities and high conversions. Catalysts X039 and X054, which are characterized by particularly large phenolic ligands, are capable of producing high Z-selectivities in the cross metathesis reaction and are the preferred catalysts for the synthesis of Nirvanolide. The selection of optimized conditions of the cross-metathesis reaction depends on the nature of the individual substrate, the catalyst and its loadings as well as the degree of purification of substrates and solvents (if used), as further described in detail below.

The olefins used as substrates in the metathesis reaction of the present invention may be employed in a molar ratio of 1:X, wherein X is 1 or greater, and may be an integer or a number having a fractional part. More particularly, X is an integer or a number having a fractional part, between 1 and 10.

Assuming full conversion, statistically, a 1:1 mixture of olefin substrates will result in a maximum yield of 50% of the desired hetero-dimer product and 25% each of two homo-dimer products. Whereas, at first sight this appears to represent only a moderate yield of the desired hetero-dimer product, it represents a thermodynamic mixture and is the highest yield of hetero-dimer that can be achieved. If X is an integer or a number having a fractional part, which is greater than 1, then a mixture of hetero-dimer to first and second homo-dimers will be obtained in a molar ratio of 2X:1:X2.

Employing a ratio of 1:X, wherein X is a relatively large number would make economic sense if the first homo-dimer (the minor reaction product in the mixture) was a dimer of relatively expensive olefin starting material, and the second homo-dimer (the overwhelmingly major product in the reaction mixture) was the homo-dimer of a relatively inexpensive olefin starting material, or was otherwise an industrially useful by-product in its own right, or was easily and cheaply separable from the other ingredients of the mixture, for example, by re-crystallization.

Irrespective of the molar ratio of olefin starting materials that is employed in the present invention, the result of the metathesis reaction is a complex mixture. In order for such a reaction to be industrially scalable, it should be possible to separate the desired hetero-dimer from the homo-dimers in a cheap and efficient manner. Applicant has surprisingly found that the judicious selection of the protecting group for the hydroxyl group on the olefin starting material of formula (I) above can influence the down-stream purification of the hetero-dimer. More particularly, when the protecting group is an alkyl ether, and more particularly the iso-propyl or t-butyl ether, not only is there is clear separation of the boiling points of the hetero-dimer and the homo-dimers, but all of the dimers in the reaction mixture boil at relatively low temperatures, such that distillation can be employed at relatively low temperatures, e.g. about 100 to 220 degrees centigrade, at easily attainable reduced pressure of about 1 to 10 mbar. Furthermore, the t-butyl protecting group is easily cleavable, which provides that the subsequent macrocyclization step to form the macrocyclic musk can be carried out under relatively mild reaction conditions.

Accordingly, in another aspect of the present invention, the mixture of the hetero-dimer and homo-dimers formed by the cross-metathesis reaction may be separated by distillation, wherein the distillation temperature is between 100 to 220 degrees centigrade at a pressure of between 1 to 10 mbar.

In a particular embodiment of the present invention, in the method of separating the mixture of hetero-dimer from the homo-dimers, the mixture is formed from a first and second olefin employed in a 1:1 molar ratio.

In a particular embodiment of the present invention, in a method of separating the mixture of hetero-dimer from the homo-dimers, the protecting group on the hetero-dimer is an alkyl ether, and more particularly a t-butyl ether.

In order for a process to be industrially scalable, not only must it be possible to easily and cheaply separate the hetero-dimer from the homo-dimers, it should also be possible to recycle the homo-dimer by-products. The homo-dimer by-products can be treated with ethylene and a metathesis catalyst to regenerate the first and second olefin starting materials in a straightforward manner and conventional manner.

Accordingly, in another aspect of the present invention, the homo-dimers formed in a cross-metathesis reaction described herein, are separated from the hetero-dimer, and are treated with ethylene to regenerate first and second olefins.

The ethylenolysis treatment of the homo-dimers can be carried out under an appropriate pressure of ethylene gas. An appropriate pressure of ethylene would be between 1 bar and 20 bar. The reaction may be carried out at a temperature of between 10° C. and 50° C.

Whereas ethylenolysis is an efficient way to re-cycle the homo-dimers, nevertheless, one has to work under a high pressure of ethylene, which adds complexity and cost to the process.

Surprisingly, applicant has found that rather than subjecting the homo-dimers to ethylenolysis to regenerate the first and second olefins, the homo-dimers can be directly re-cycled by adding to them an amount of metathesis catalyst and subjecting them to a metathesis reaction.

In this re-cycling step, the homo-dimers may be mixed together as the sole reactants in a cross-metathesis reaction; or they may singularly, or in combination, be admixed with one or both of first and second olefins, before subjecting this mixture in a cross-metathesis reaction. Different recycling scenarios are schematically presented below. For example, the homo-dimers can be re-cycled alone, as set out in Scenario 1 below, or they can be re-cycled in admixture with first and second olefins (Scenario 2); or one homo-dimer can be reacted with the complementary olefin (Scenario 3 or 4).

The skilled person will appreciate that the homo-dimers can be mixed, optionally with the first and second olefins, to form a a statistical mixture in which the desired hetero-dimer 16ai is again formed with 50% yield. In this way, after a second metathesis step the hetero-dimer can be converted with 75% yield.

Accordingly, in another aspect of the present invention, the cross-metathesis reaction comprises a cross-metathesis step of first and second olefins defined hereinabove, and a subsequent cross-metathesis step of homo-dimers formed from the preceding cross-metathesis step.

The skilled person will appreciate that the recycling of homo-dimers is not limited to single recycling step. Subsequent recycling steps can be carried out, all of which can achieve a statistical mixture containing the desired hetero-dimer with 50% yield. Of course, the absolute amount of hetero-dimer recovered after each recycling step diminishes and so the number of recycling steps one performs is determined by the diminishing economic returns.

The fact that homo-dimers could be re-cycled in this way was surprising. The homo-dimers contain internal double bonds and as such would be expected to react very slowly, if at all, and it was not predictable that a statistical mixture containing the desired hetero-dimer would be formed, at least in a reasonable time that would make sense in the context of an industrial process. However, applicant found that the homo-dimers displayed substantially similar reaction kinetics as the first and second olefins, even when the first and second olefins contained terminal double bonds.

The synthetic methods described herein are particularly atom efficient, and as such represent a very efficient means of producing macrocyclic musk compounds on an industrial scale.

In particular, the use of terminal olefins as starting materials means that ethylene is eliminated as a by-product of the metathesis reaction. Only two carbon atoms are lost in this case, and if desired, the generated ethylene can be recovered and used in any subsequent ethyleneolysis reaction that is carried out on the homo-dimers.

However, notwithstanding the advantages attendant to the use of terminal olefins, applicant found that there are drawbacks associated with their use. In particular, the elimination of ethylene as a by-product can reduce the efficiency of the metathesis catalysts. Without wishing to be bound by any particular theory, it is possible that ethylene could deactivate the catalysts to a certain extent. Still further, certain metathesis catalysts, and in particular the ruthenium-based catalysts, can cause the terminal double bond of each of the starting materials to migrate, and also cause isomerization on the double bond in the hetero-dimer.

Surprisingly, however, applicant found that when using molybdenum and tungsten metathesis catalysts, and particularly those preferred molybdenum and tungsten catalysts referred to specifically hereinabove, there was substantially no double bond migration. Furthermore, there was relatively little isomerization about the double bond of the hetero-dimer. For example, with regard to the molecule 9-Ambrettolide, it was possible to obtain the molecule with high E-specificity. More particularly, it was possible to obtain E/Z 9-Ambrettolide in a ratio of about 80:20 to 90:10, more particularly about 85:15.

There now follows a series of examples, which serves to illustrate the invention.

SYNTHESIS OF OLEFIN SUBSTRATES

Under inert atmosphere sodium hydride (20.60 g, 858 mmol, 2.2 equiv.) was suspended in dry THF (300 mL) and a solution of oct-7-en-1-ol (1) (50.00 g, 390 mmol) was added dropwise to the suspension over a 20-minute period, then it was stirred at rt for 30 min. After completion of the salt formation, iodomethane (66.4 g, 468 mmol, 1.2 equivalent) was added to the reaction mixture and it was stirred at rt overnight. After completion of the reaction the reaction mixture was concentrated to ⅓ and the residue was dissolved in chloroform (500 mL). The organic phase was washed with water (3×100 mL) and brine (2×100 mL), dried over magnesium sulphate and evaporated. The crude product was purified by distillation (65-70° C./25 Hg mm) to yield 26.50 g (47.80%) methyl ether (3h) as a colorless liquid.1H-NMR (200 MHz, CDCl3): δ 1.24-1.44 (m, 6H), 1.46-1.60 (m, 2H), 2.04 (q, J=7.0 Hz, 2H), 3.28 (s, 3H), 3.45 (t, J=7.0 Hz, 2H), 4.90-5.08 (m, 2H), 5.70-5.90 (m, 1H). GC-MS: 96.3% MS (EI): 142.

Phosphorus tribromide (27.21 g, 97.5 mmol, 0.5 equiv.) was added dropwise to a solution of oct-7-en-1-ol (1) (25.00 g, 195 mmol) in dry dichloromethane (200 mL) at 0° C. After completion of the addition it was allowed to warm up to rt and stirred for 2 h, then the reaction mixture was poured into saturated aqueous solution of NaHCO3to adjust the pH to 7.0. Phases were separated and the organic phase was washed with water (3×75 mL), brine (3×75 mL), dried over magnesium sulphate and evaporated. The crude product was purified by vacuum distillation (59-61° C./7 Hg mm) to yield 6.20 g (16.60%) 3k as a colorless liquid.1H-NMR (200 MHz, CDCl3): δ 1.20-1.50 (m, 6H), 1.76-1.92 (m, 2H), 1.96-2.14 (m, 2H), 3.14 (t, J=7.0 Hz, 2H), 4.90-5.08 (m, 2H), 5.70-5.92 (m, 1H). GC-MS: 96.8% MS (EI): 190, 192.

Under inert atmosphere a 2.5M solution of butyllithium (93.6 mmol, 25.95 g, 37.4 mL) was added dropwise to a solution of oct-7-en-1-ol (1) (10.00 g, 78 mmol) in dry THF (100 mL) at 0° C. then it was stirred at the same temperature for 30 min. After completion of the salt formation, methyl chloroformate (8.85 g, 93.6 mmol, 7.23 mL) was added to the reaction mixture and it was stirred at rt overnight. After completion of the reaction the reaction mixture it was quenched with saturated aqueous solution of ammonium chloride and it was extracted with dichloromethane (3×100 mL). The organic phase was washed with water (2×50 mL) and brine (50 mL), dried over magnesium sulphate and evaporated. The crude product was purified by distillation (105-107° C./20 Hgmm) to yield 7.72 g (53.10%) carbonate (3l) as a colorless liquid.1H-NMR (300 MHz, CDCl3): δ 1.21-1.48 (m, 6H), 1.55-1.70 (m, 2H), 1.95-2.05 (m, 2H), 3.78 (s, 3H), 3.88 (t, J=7.1 Hz, 2H), 4.90-5.06 (m, 2H), 5.70-5.90 (m, 1H). GC-MS: 97.2% MS (EI):

Decenoic acid (12) (32.60 g, 192 mmol) was dissolved in dry methanol (300 mL) and 0.1 equiv. of sulfuric acid (1.96 g, 1.07 mL, 19.2 mmol) was added to the reaction mixture and it was refluxed for 20 h. After completion of the reaction it was quenched with saturated aqueous solution of NaHCO3(25 mL) and evaporated. The residue was dissolved in chloroform (300 mL) and washed with water (3×75 mL) and brine (2×75 mL), dried over magnesium sulphate and evaporated. The crude product was purified by flash column chromatography (n-Heptane-Ethyl acetate; 20:1) gave 25.50 g (72.30%) of the title compound (11a) as a colorless liquid. GC-MS: >98.1% MS (EI): 184.

Decenoic acid (12) (30.60 g, 180 mmol) was dissolved in dry methanol (300 mL) and 0.1 equivalent of sulfuric acid (1.84 g, 0.99 mL, 18 mmol) was added to the reaction mixture and it was refluxed for 20 h. After completion of the reaction it was quenched with saturated aqueous solution of NaHCO3(25 mL) and evaporated. The residue was dissolved in chloroform (300 mL) and washed with water (3×75 mL) and brine (2×75 mL), dried over magnesium sulphate and evaporated. The crude product was purified by flash column chromatography (n-Heptane-Ethyl acetate; 20:1) to yield 23.50 g (65.90%) of the title compound (11b) as a colorless liquid. GC-MS: >98.5% MS (EI): 198.

Decenoic acid (12) (15.00 g, 88.1 mmol) was dissolved in dry 2-propanol (200 mL) and 0.1 equiv. of sulfuric acid (0.9 g, 0.49 mL, 8.81 mmol) was added to the reaction mixture and it was refluxed for 20 h. After completion of the reaction it was quenched with saturated aqueous solution of NaHCO3(25 mL) and evaporated. The residue was dissolved in chloroform (300 mL) and washed with water (3×75 mL) and brine (2×75 mL), dried over magnesium sulphate and evaporated. The crude product was purified by distillation (98-104° C./8 Hg mm) to yield 14.56 g (77.80%) of the title compound (11c) as a colorless liquid. GC-MS: >99.0% MS (EI): 212.

Cross metathesis of oct-7-enol and 3-methylhex-5-enol derivatives

All metathesis reactions were carried out in a nitrogen-filled glovebox in oven dried glassware.
General Procedure of Cross Metathesis Reactions without Trioctylaluminum (Procedure A):

In an open screw cap vial the 0.1 M solution of metathesis catalyst (in dry benzene) (25-1000 ppm) was added to the mixture of decenoate (11a-c) (10.9 mmol) and octenol derivative (3a-q and 13) (10.9 mmol) and the reaction mixture was stirred at rt for 4-20 h, then it was quenched with 0.2 mL diethyl ether (Analysis: ca. 100 μL of the reaction mixture was filtered through a silica pad (ca. 4-5 mL) the pad was washed with a mixture of n-heptane and EtOAc (7:3, 15 mL) and the filtrate was analyzed by GC-MS.).

General Procedure of Cross Metathesis Reactions in the Presence of Trioctylaluminum (Procedure B):

In an open screw cap vial 0.5 mol % of trioctylaluminum was added to the mixture of decenoate (11a-c) (10.9 mmol) and octenol derivative (3a-q and 13) (10.9 mmol) and the reaction mixture was stirred at rt for 1 h, then the 0.1 M solution of metathesis catalyst (in dry benzene) (25-1000 ppm) was also added to the reaction mixture and stirring was continued for 4-20 h, then it was quenched with 0.2 mL diethyl ether (Analysis: ca. 100 μL of the reaction mixture was filtered through a silica pad (ca. 4-5 mL), the pad was washed with the mixture of n-heptane and EtOAc (7:3, 15 mL) and the filtrate was analyzed by GC-MS.).

In an open screw cap vial the 0.1 M solution of X052 in dry benzene (10.9 μL, 50 ppm) was added to the mixture of purified methyl decenoate (11a) (2.00 g, 10.9 mmol, 2.28 mL) and purified tert-butyl ether (3i) (2.00 g, 10.9 mmol, 2.52 mL) and the reaction mixture was stirred at rt for 20 h, then it was quenched with 0.2 mL of diethyl ether (Analysis: ca. 100 μL of reaction mixture was filtered through silica pad (ca. 4-5 mL) and washed with the mixture of n-heptane and EtOAc (7:3, 15 mL) and the filtrate was analyzed by GC-MS.). The CM reaction of 11a with 3i afforded a statistical mixture of 14i, 16ai and 18a (1:2:1) with 95% conversion for both starting olefins and E/Z ratios were found to be 85/15 for all three compounds.

In an open screw cap vial 0.5 mol % of trioctylaluminum (25 w % in hexane) (80 mg, 5.45*10−2mmol, 114 μL) was added to the mixture of methyl decenoate (11a) (2.00 g, 10.9 mmol, 2.28 mL) and tert-butyl ether (3i) (2.00 g, 10.9 mmol, 2.52 mL) and the reaction mixture was stirred at rt for 1 h, then the 0.1 M solution of X190 in dry benzene (5.45 μL, 25 ppm) was also added to the reaction mixture and stirring was continued for 20 h, then it was quenched with 0.2 mL of diethyl ether (Analysis: ca. 100 μL of the reaction mixture was filtered through silica pad (ca. 4-5 mL) and washed with the mixture of n-heptane and EtOAc (7:3, 15 mL) and the filtrate was analyzed by GC-MS.). The CM reaction of 11a with 3i afforded a statistical mixture of 14i, 16ai and 18a (1:2:1) with 95% conversion for both starting olefins and E/Z ratios were found to be 84/16 for all three compounds.

Methyl decenoate (11a) (51.2 g, 278 mmol, 58.0 mL) and tert-butyl octenyl ether (3i) (50.4 g, 273 mmol, 63.0 mL) were charged in a 500 mL round-bottom flask and the mixture was stirred for ten minutes, then 0.1 M solution of X039 in dry benzene (560 μL, 100 ppm) was added in one portion. The reaction vessel was connected to a vacuum pump and the reaction mixture was stirred at room temperature under 50 mbar dynamic vacuum for 4 hours. GC-MS analysis of the crude product found 90% conversion for both starting olefins. Non-anhydrous ethyl acetate (10 mL) was added to the reaction mixture to quench the metathesis reaction. The quenched mixture was passed through a pad of silica (approx. 20 mL) using 500 mL ethyl acetate as eluent. Volatiles were removed in vacuo to afford the crude product as a practically colourless oil (92.4 g). Metathesis products 14i, 16ai and 18a were formed in the statistical (1:2:1) ratio and E/Z ratios were found to be 9/91 for all three compounds.

Methyl decenoate (11a) (0.675 g, 3.66 mmol, 765 μL) and octenyl acetate (3m) (0.623 g, 3.66 mmol, 700 μL) were charged in a 30 mL glass vial and the mixture was homogenized, then 0.1 M solution of X054 in dry benzene (74 μL, 1000 ppm) was added in one portion. The vial was connected to a vacuum pump and the reaction mixture was stirred under 50 mbar dynamic vacuum at room temperature for 6 hours (90% conversion for both starting olefins according to GC-MS). Non-anhydrous diethyl ether (10 mL) was added to it to quench the metathesis reaction. The mixture was passed through a silica pad (10 mL) using n-Heptane-Ethyl acetate; 1:1 solvent mixture as eluent. Approximately 75 mL filtrate was collected. Solvent was removed in vacuo to afford the metathesis product mixture as a slightly brownish oil (1.18 g). Metathesis products 14m, 16am and 18a were formed in the statistical (1:2:1) ratio and E/Z ratios were found to be 11/89 for all three compounds.

Methyl decenoate (11a) (21.4 mg, 0.116 mmol, 24.2 μL) and octenyl acetate (3m) (19.6 mg, 0.115 mmol, 22.0 μL) were charged in a 4 mL glass vial and the mixture was homogenized, then 0.1 M solution of X038 in dry benzene (11.5 μL, 5000 ppm) was added in one portion. The vial was closed with a pierced cap and the reaction mixture was stirred under atmospheric pressure at room temperature. (Analysis: 20 μL of the reaction mixture was mixed with 200 μL of non-anhydrous diethyl ether within the glovebox to quench the metathesis reaction, then the quenched sample was passed through a silica plug (approx. 2 cm thick layer in a Pasteur-pipette) using 4 mL n-Heptane-Ethyl acetate; 1:1 solvent mixture as eluent and the filtrate was analyzed by GC-MS. Sample taken after 2 hours showed 57% conversion for both starting olefins (11a, 3m) and cross metathesis products 14m, 16am and 18a were formed in the statistical (1:2:1) ratio. E/Z ratios were found to equal to 3/97 for all three cross metathesis products. A sample was taken after 2.5 days to find only 68% conversion of both starting olefins and E/Z=4/96 ratios for all three metathesis products.

In an open screw cap vial the 0.1 M solution of X190 in dry benzene (26.2 μL, 400 ppm) was added to the mixture of purified methyl decenoate (11a) (600 mg, 3.27 mmol, 683 μL) and purified carbonate (3l) (609 mg, 3.27 mmol) and the reaction mixture was stirred at rt for 20 h, then it was quenched with 0.2 mL of diethyl ether (Analysis: ca. 100 μL of reaction mixture was dissolved in methanol (1 mL) and a small amount sodium methoxide was added to the solution and it was stirred at rt for 4 h. After that it was diluted with water (0.5 mL) and extracted with dichloromethane (2×2 mL), dried over magnesium sulphate and evaporated. The sample was analyzed by GC-MS.). The CM reaction of 11a with 3l afforded a statistical mixture of 14l, 16al and 18a (1:2:1) with 95% conversion.

In an open screw cap vial 0.5 mol % of trioctylaluminum (25 w % in hexane) (40 mg, 2.72*10−2mmol, 57 μL) was added to the mixture of methyl decenoate (11a) (1.00 g, 5.43 mmol, 1.13 mL) and carbonate (3l) (1.00 g, 5.43 mmol) and the reaction mixture was stirred at rt for 1 h, then the 0.1 M solution of X190 in dry benzene (21.7 μL, 200 ppm) was also added to the reaction mixture and stirring was continued for 20 h, then it was quenched with 0.2 mL of diethyl ether (Analysis: ca. 100 μL of reaction mixture was dissolved in methanol (1 mL) and a small amount sodium methoxide was added to the solution and it was stirred at rt for 4 h. After that it was diluted with water (0.5 mL) and extracted with dichloromethane (2×2 mL), dried over magnesium sulphate and evaporated. The sample was analyzed by GC-MS.). The CM reaction of 11a with 3l afforded a statistical mixture of 14l, 16al and 18a (1:2:1) with 35% conversion.

Methyl decenoate (11a) (0.098 g, 0.50 mmol, 104 μL) and 3-methylhex-5-enyl acetate (13) (0.078 g, 0.50 mmol, 85 μL) were measured into a 4 mL vial, 0.1 M solution of X054 in dry benzene (5.0 μL, 500 ppm) was added in one portion, then the vial was connected to a vacuum pump and the reaction was stirred at room temperature under 50 mbar dynamic vacuum. (Analysis: 5.0 μL of the reaction mixture was mixed with 200 μL non-anhydrous diethyl ether to quench the metathesis reaction, then the quenched sample was passed through a silica plug (approx. 2 cm thick layer in a Pasteur-pipette) using 4 mL n-Heptane-Ethyl acetate; 1:1 solvent and the filtrate was analyzed by GC-MS. Sample taken after 19 hours showed 97% conversion for both starting olefins (11a, 13) and cross metathesis products 15, 17 and 18a were formed in the statistical (1:2:1) ratio. Since E- and Z-isomers of the acetate compound 17 separate less readily in GC-MS than isomers of deprotected alcohol 22, the acetate moiety was selectively cleaved via trans-esterification of 20 μL reaction mixture samples with dry methanol/NaOMe (1.0 mL methanol, approx. 5 mg NaOMe) following a protocol analogous to that described in Example 9. The resulting material was analyzed by GC-MS to determine E/Z ratio of compound 17. It was found that the more branched the chain is (2, 1 or no methyl groups in homoallylic position(s) of the double bond, the higher the Z-selectivity is. E/Z ratios for cross metathesis products: 15 (2/98); 17 (5/95); 18a (7/93). A sample taken only after 4 hours showed 89% conversion for 13 and 95% conversion 11a, indicating that the more branched substrate undergoes metathesis less readily. E/Z ratios were the same as those reported for the sample taken after 19 hours.

The experiment described in Example 8 was repeated using catalyst X039. In this case 96% conversion of both starting olefins was achieved within 4 hours. Cross metathesis products 15, 17 and 18a were again formed in the statistical (1:2:1) ratio. E/Z ratios: 15 (2/98); 17 (7/93); 18a (12/88).

Cleavage of a tBu-Ether Protecting Group

Crude product obtained in Example 3 was charged in a 500 mL two-necked round-bottom flask and dissolved in dry dichloromethane (200 mL, freshly distilled from CaH2). The flask was flushed with nitrogen and cooled to 0° C. by applying an ice/water bath. Titanium tetrachloride was added in small portions over 15 minutes and the mixture was stirred for additional 15 minutes. Still at 0° C., under constant cooling, saturated aqueous solution of NH4Cl solution (20 mL) was added dropwise. The mixture was allowed to warm to room temperature and brine was added to ease phase separation (1×100 mL). Phases were separated and the organic phase was washed with brine (2×50 mL) and dried over MgSO4. Volatiles were removed in vacuo. Column chromatographic purification of the resulting oil using silica and n-heptane-diethyl ether; 2:1 as eluent afforded the desired product (21a) as a colorless oil (31.0 g, 109 mmol, 79% overall yield for the cross metathesis and tert-butyl cleavage steps). The E/Z isomer ratio was invariably 9/91.

Cleavage of an Ester Protecting Group

The crude product obtained in Example 4 was dissolved in 3 mL dry methanol, 20 mg sodium methylate was added and the mixture was stirred at room temperature for 2 hours. The mixture was passed through a silica pad (7 mL silica) and the pad was washed with ethyl acetate (75 mL). The filtrate was evaporated to afford 1013 mg crude transesterification product. The desired product was isolated by flash column chromatography using n-heptane-diethyl ether; 2:1. The desired product (21a, R1=Me) was obtained as a yellowish oil (355 mg, 1.25 mmol, 68% overall yield for the cross metathesis and acetate cleavages). The E/Z isomer ratio was invariably 11/89.

GC-MS Analytical Method for Product Identification (Method A):

GC-MS Analytical Method for Product Identification (Method B):

TABLE 1Cross metathesis of decenoic acid esters andprotected oct-7-enol derivatives.LoadingCon-E/ZEntrySubstratesCatalyst(ppm (mol))versionratioProcedure111a and 3mX0072000ppm80%82/18A211a and 3mX0071000ppm15%80/20A311a and 3mX0082000ppm25%81/19A411a and 3mX0012500ppm85%85/15A511a and 3mX0302000ppm50%83/17A611a and 3mX0412000ppm50%83/17A711a and 3mX0422000ppm90%84/16A811a and 3mX0462000ppm90%81/19A911a and 3mX0402000ppm95%85/15A1011a and 3mX0421000ppm80%83/17A1111a and 3mX0521000ppm85%84/16A1211a and 3mX0511000ppm35%85/15A1311a and 3mX0041000ppm60%86/14A1411a and 3mX042500ppm15%85/15A1511a and 3mX123200ppm10%85/15B1611a and 3mX0541000ppm90%11/89Example 41711a and 3mX0385000ppm68%4/96Example 51811a and 3hX0421000ppm95%84/16A1911a and 3hX0521000ppm95%85/15A2011a and 3hX052250ppm95%84/16A2111a and 3hX042250ppm95%85/15A2211a and 3hX052100ppm95%84/16A2311a and 3hX042100ppm95%85/15A2411a and 3hX05250ppm85%85/15A2511a and 3hX04250ppm40%84/16A2611a and 3hX05150ppm75%85/15A2711a and 3hX06150ppm85%84/16A2811a and 3hX06250ppm65%84/16A2911a and 3hX06350ppm40%70/30A3011a and 3gX052100ppm95%84/16A3111a and 3gX042100ppm70%85/15A3211a and 3iX052100ppm90%83/17A3311b and 3iX052100ppm95%85/15A3411c and 3iX052100ppm95%84/16A3511a and 3iX039100ppm90%9/91Example 33611a and 3iX05250ppm90%84/16A3711a and 3iX06150ppm20%83/17A3811a and 3iX05950ppm20%84/16A3911a and 3iX00450ppm20%85/15A4011a and 3iX07650ppm90%60/40A4111a and 3iX11450ppm15%80/20A4211a and 3iX12350ppm85%85/15A4311a and 3iX12325ppm90%85/15B4411a and 3iX14925ppm10%84/16B4511a and 3iX15425ppm85%85/16B4611a and 3iX12317ppm75%84/16B4711a and 3iX12312ppm55%84/16B4811a and 3lX19040095%n/aExample 64911a and 3lX19020032%n/aA5011a and 3lX19020035%n/aExample 75111a and 3lX19010010%n/aA

Recycling of Homodimeric Side Product(s) Via Cross Metathesis:

The homodimer of tert-butyl octenyl ether (14i) (0.085 g, 0.25 mmol, 100 μL, E/Z=85/15) and the homodimer of methyl dec-9-enoate (18a) (0.086 g, 0.25 mmol, 92 μL, E/Z=85/15) were charged in a 4 mL screw cap vial and the mixture was homogenized. Metathesis catalyst X190, (1.0*10−4mmol, 10 μL, 0.01 M in benzene) was added in one portion. The vial was closed with a septum cap and the reaction mixture was stirred at room temperature overnight. The reaction mixture was subjected to air and mixed with 1 mL non-anhydrous ethyl acetate to quench the reaction. The sample was then passed through a silica pad using pure ethyl acetate as eluent (5 mL) and the filtrate was analyzed by GC-MS. The reaction afforded 14i, 16ai and 18a with 95% recycling efficiency. In case of compound 16ai the ratio of E- and Z-isomers was found to correspond to the thermodynamical equilibrium value (E/Z≈85/15).

8-(tert-Butoxy)oct-1-ene (3i) (0.092 g, 0.50 mmol, 114 μL) and methyl dec-9-enoate (11a) (0.092 g, 0.50 mmol, 104 μL) along with the homodimer of tert-butyl octenyl ether (14i) (0.086 g, 0.25 mmol, 100 μL, E/Z=85/15) and the homodimer of methyl dec-9-enoate (18a) (0.086 g, 0.25 mmol, 92 μL, E/Z=85/15) were charged in a 4 mL screw cap vial and the mixture was homogenized. Metathesis catalyst X052 (2.0*10−4mmol, 20 μL, 0.01 M in benzene) was added in one portion. The vial was closed with a pierced cap and the reaction mixture was stirred at room temperature. Samples (10 μL) taken from the reaction mixture after 2 h and 18 h reaction times were subjected to air and mixed with 0.2 mL non-anhydrous diethyl ether to quench the reaction. The samples were then passed through a silica pad using pure EtOAc as eluent (5 mL) and the filtrate was analyzed by GC-MS. For the sample taken at 2 hours reaction time GC-MS analysis found 90% recycling efficiency and in case of compound 16ai the ratio of E- and Z-isomers was found to correspond to the thermodynamical equilibrium value (E/Z≈85/15). The sample taken after 18 hours showed identical values regarding both recycling efficiency and E/Z ratio.

Methyl dec-9-enoate (11a) (0.184 g, 1.0 mmol, 208 μL) and the homodimer of tert-butyl octenyl ether (14i) (0.170 g, 0.5 mmol, 200 μL, E/Z=85/15) were charged in a 4 mL screw cap vial along with trioctylaluminum (4.0*10−4mmol, 16.8 μL, 0.024 M in benzene) and the mixture was stirred at room temperature for 3.5 hours, then metathesis catalyst X190 (4.0*10−4mmol, 40 μL, 0.01 M in benzene) was added in one portion. The vial was closed tightly and the reaction mixture was stirred at room temperature for 1.5 hours. The vial was connected to a 50 mbar dynamic vacuum source and its content was stirred for further 2.5 hours. The reaction mixture was subjected to air and mixed with 1 mL non-anhydrous ethyl acetate to quench the reaction. The sample was then passed through a silica pad using pure ethyl acetate as eluent (5 mL) and the filtrate was analyzed by GC-MS. GC-MS analysis found 95% recycling efficiency and in case of compound 16ai the ratio of E- and Z-isomers was found to correspond to the thermodynamical equilibrium value (E/Z≈85/15).

8-(tert-Butoxy)oct-1-ene (3i) (0.186 g, 1.0 mmol, 235 μL) and the homodimeric olefin (18a) (0.170 g, 0.5 mmol, 183 μL, E/Z=85/15) were charged in a 4 mL screw cap vial along with trioctylaluminum (2.0*10−4mmol, 8.4 μL, 0.024 M in benzene) and the mixture was stirred at ca. 30° C. for 3.5 hours, then metathesis catalyst X190 (2.0*10−4mmol, 20 μL, 0.01 M in benzene) was added in one portion. The vial was closed tightly and the reaction mixture was stirred at ca. 30° C. for 1.0 hours. The vial was connected to a 50 mbar dynamic vacuum source and its content was stirred for further 1.5 hours. The reaction mixture was subjected to air and mixed with 1 mL non-anhydrous ethyl acetate to quench the reaction. The sample was then passed through a silica pad using pure ethyl acetate as eluent (5 mL) and the filtrate was analyzed by GC-MS. GC-MS analysis found 95% recycling efficiency and in case of compound 16ai the ratio of E- and Z-isomers was found to correspond to the thermodynamical equilibrium value (E/Z≈85/15).

TABLE 5Selected examples of recycling experiments based on various strategies outlined in Scheme 5.Substrates,Loading (ppm (mol))molarin monomerRecyclingE/Z ratioEntryratiosCatalystequivalentsaefficiency %b(16ai)Procedure114i, 18aX190100 ppm95%85/15Example 1021:1X052100 ppm40%85/15Conditions ofExample 1033i, 11a, 14i,X052100 ppm90%85/15Example 1118a42:2:1:1X190100 ppm70%85/15Conditions ofExample 11511a, 14iX190200 ppm95%85/15Example 122:163i, 18aX190100 ppm95%85/15Example 132:1aMonomeric olefins (3i, 11a) equal to 1, while homodimeric olefins (14i, 18a) equal to 2 equivalents of monomeric units. Loadings are given with respect to the sum of all olefinic starting materials.bRecycling efficiency is calculated in the following way: rec. efficiency % = [n(octenyl units in 16ai)/Σn(octenyl units in any form) + n(octenyl units in 16ai)/Σn(octenyl units in any form)] * 100. Its value is 0% for all starting mixtures and equals to 100% for a statistical mixture of 14i, 16ai, 18a.
Experimental Details on the Recycling of Homodimeric Side Product(s) Via Ethenolysis

TABLE 6Ethenolysis of tert-butyl ether dimer (14i).αEntrySubstrateCatalystLoading (ppm (mol))Conversion114iX041400 ppm65%214iX042400 ppm60%314iX052400 ppm75%414iX076400 ppm60%514iX041200 ppm57%614iX042200 ppm41%714iX052200 ppm52%814iX076200 ppm33%9b14iX041200 ppm91%10b14iX052200 ppm62%aAll reactions were carried out at 0.73 mmol scale, reaction mixtures were stirred at room temperature for 16 h under 11.5 bar ethylene pressure.bn-Heptane was used as solvent to increase the solubility of ethylene.

General Procedure of Ethenolysis (for Results in Table 6.):

In an open screw cap vial the 0.1 M solution of metathesis catalyst (in dry benzene) (200-400 ppm) was added to 14i or 18a (0.73 mmol) and the reaction mixture was stirred at rt under 11.5 bar ethylene for 20 h, then it was quenched with 0.2 mL diethyl ether (Analysis: ca. 100 μL of the reaction mixture was filtered through a silica pad (ca. 4-5 mL) the pad was washed with a mixture of n-heptane and EtOAc (7:3, 15 mL) and the filtrate was analyzed by GC-MS.).

Diether (14i) (2.47 g; 7.25 mmol) was dissolved in 12.0 mL pentane in a 30 mL oven-dried glass vial equipped with a stir bar, stock solution of catalyst X061 (0.1 M in benzene; 72.6 μL; 0.1 mol %) was added to the reaction mixture and the vial was placed into an autoclave (250 mL inner volume). The autoclave was closed and pressurized to 11.5 bar for 30 minutes. Ethylene source was disconnected and the autoclave was chambered out from the glovebox. The reaction mixture was allowed to stir at room temperature for 12 hours. Ethylene was carefully released, the autoclave lid was removed and 1 mL heptane:EtOAc (non-anhydrous solvents) 1:1 solvent mixture was added subsequently to quench the reaction. The quenched reaction mixture was passed through a silica plug (ca. 10 cm silica layer in a 20 mL syringe barrel) using 150 mL heptane:EtOAc 1:1 solvent mixture as eluent. The filtrate was concentrated in vacuo and the oily residue was distilled bulb-to-bulb (3.0-3.3×10−2mbar; 52-55° C.) to afford recovered tert-butyl octenyl ether (3i) as a colorless oil (2.13 g; 11.56 mmol; yield: 80%).

Procedure and workup were identical to those describe in Example A but catalyst X008 was used. Diester (18a) (2.27 g; 6.67 mmol) dissolved in 9.6 mL n-pentane was ethenolyzed in the presence of catalyst X008 (0.1 M in benzene; 66.4 μL; 0.1 mol %). Bulb-to-bulb distillation (8.5-9.0×10−2mbar; 60-61° C.) afforded the title compound as a colorless oil (2.10 g; 11.40 mmol; yield: 86%).

1H-NMR analysis of the crude products before bulb-to-bulb distillation—both for Example 16 and Example 17—showed that crude products consisted of ca. 95% monomer (3i; 11a) and residues of unreacted homodimer (14i; 18a). No signs of undesired side reactions during the ethenolysis or workup were observed. NMR spectra of bulb-to-bulb distilled materials correspond to those of pure 3i and 11a.