DISPROPORTIONATION OF FUNCTIONAL OLEFINS

Abstract: A process for producing internally unsaturated esters from alpha, omega dienes by disproportionation. Also disclosed are functional olefin compositions useful in con­ trolling insects.

Description: DISPROPORTIONATION OF FUNCTIONAL OLEFINS Background of the Invention This invention relates to the disproportionation of functional olefins and to the products resulting therefrom. The disproportionation of olefins containing other functional groups is a very desirable technique for obtaining valuable chemicals that otherwise would require multistep preparations that are costly and often give products that are difficult to purify. The disproportionation of olefins containing ester, halide or ether groups is particularly interesting in that it provides a route to chemicals having potential application in insect control because of the ability of the compounds to disrupt the mating of specific insects. It has been noted by those working in the area of insect pheromones that the microstructure ratio of functional olefins can often have a significant influence upon the effectiveness of a particular functional olefin as an insect control agent. Thus, while some insects are attracted to a trans isomer, others may be attracted to a cis isomer, and still others may be best attracted by a particular molar ratio of cis and trans isomers. A particularly useful catalyst system for the production of functional olefins has been disclosed in U. S. 4,269,780, the disclosure of which is incorporated herein by reference. The present invention is based upon the discovery that by selecting the proper reactants, it is possible to vary the isomer ratio in the recoverable functional olefin disproportionation product. Summary of the Invention In accordance with the present invention, a monoolefin having at least one terminal ester or ether group is reacted with a hydrocarbyl monoolefin consisting essentially of either an internal olefin or an alpha-olefin having at least three carbon atoms in the presence of a catalyst comprising a neutral tungsten carbene and a metal halide promoter. Another embodiment of the present invention involves the disproportionation of a hydrocarbyl olefin and an omega-halo-alpha olefin. Still another aspect of the invention involves the method of preparing internally unsaturated esters from alpha, omega dienes. Also in accordance with the present invention, there are provided certain specific functional olefin compositions useful in insect control. Detailed Description of Invention One embodiment of the present invention deals with the cross-disproportionation of a monoolefin having at least one terminal functional group selected from groups having the formulas EMI2.1 wherein R is a hydrocarbyl group having 1 to 20 carbon atoms or in the case of the first formula hydrogen. Thus, the functional olefins include alkenyl acid esters,-alkenyl esters, and alkenyl ethers. The preferred functional monoolefins are those wherein the olefinic hydrocarbyl portion thereof has the formula R"'-CH=CH(CH2),- wherein n is in the range of 2 to 20, R"' is hydrogen or an alkyl radical having 1 to 20 carbon atoms. It is also within the scope of the present invention to use a functional monoolefin having two terminal functional groups of the types described above. Typically, the preferred functional monoolefins contain no more than about 30 carbon atoms per molecule. The other olefin reactant in the inventive disproportionation consists essentially of either (1) an internal hydrocarbyl monoolefin or (2) a hydrocarbyl alpha-monoolefin having at least three carbon atoms per molecule. When an internal monoolefin reactant is employed, it has been noted that as a general rule the level of trans isomer in the product is higher than that produced using an alpha-monoolefin capable of producing a compound having the same chemical formula. The currently preferred hydrocarbyl monoolefins are those having no more than about 20 carbon atoms per molecule. If a symmetrical difunctional monoolefin reactant is used that is substantially all in the trans form, the product obtained consists predominately of the trans isomer regardless of whether an internal or alpha-olefin is used in the cross-disproportionation. By using such a technique, it has been found that it is possible to produce unsaturated functional olefins that are substantially all trans. This is particularly surprising since disproportionation reactions are generally expected to provide a mixture of cis and trans isomers. The catalyst system employed in this embodiment of the present invention comprises a neutral carbene complex and a metal component which acts as a promoter for the neutral carbene complex. Typical neutral carbene complexes for use in the catalyst system are those having the formula EMI4.1 wherein R is selected from the group consisting of alkyl or cycloalkyl radicals containing 1 to 10 carbon atoms per radical and aryl or substituted aryl radicals containing 6 to 30 carbon atoms per radical wherein the substituted radicals can have one or more substituents, each of which can be the same or different and selected from the group consisting of halides, alkoxides, and alkyl radicals containing 1 to 20 carbon atoms; Y is S or O; R" is selected from the group consisting of alkyl, cycloalkyl, aryl, and substituted aryl radicals containing 1 to 30 carbon atoms per molecule and wherein the aryl substituents are as described for R' and wherein if Y is S only one of R' and R" is aryl or substituted aryl; each L is a neutral ligand individually selected from CO, NO, PR'3, PCl3, PF3, and pyridine, where R' is as defined above, and L' is cyclopentadienyl; p is 0 or 1; and n is 5 when p is 0 or 2 when p is 1. The metal component employed as a promoter for the carbene is selected from the group consisting of the chlorides and bromides of the metals of Groups IVa, IVb, Vb, VIb, VIIb, VIII, and Ib and the oxychlorides and oxybromides of molybdenum, tungsten, vanadium, and chromium; wherein if the metal is vanadium it is in an oxidation state of either 4 or its highest, stable, common, ionic oxidation state; if the metal is molybdenum, tungsten, or rhenium it is in an oxidation state of either 5 or its highest, stable, common, ionic oxidation state; and if the metal is not vanadium, molybdenum, tungsten or rhenium the metal is in its highest, stable, common, ionic, oxidation state. The molar ratio of the metal component can vary over a wide range with varying effects upon yield and selectivity. Typically, the molar ratio of the metal component to the carbene complex is in the range of about 1/1 to about 500/1, preferably in the range of about 2/1 to 25/1. In a particularly preferred embodiment, the promoter comprises a combination of a tin tetrahalide and a tetrahalide of either silica or germanium. The molar ratio of silica or germanium tetrahalide to tin tetrahalide is generally in the range of about 0.5/1 to about 20/1, most preferably generally about 2/1. The amount of catalyst employed in the process of this invention can be expressed in terms of the molar ratio of olefin to carbene complex component. Generally, the molar ratio of the total stoichiometric amount of olefinic reactant to carbene complex component is in the range of about 1/1 to about 5000/1 and preferably from about 50/1 to about 2000/1. This term "total stoichiometric amount" is used herein to denote the moles of reactant that could theoretically react so as to distinguish from cases when two or more olefins are employed and one or more is used in a greater amount than will react. Thus, the amount of catalyst is generally based upon the amount of reactive olefins and not on excess olefin. The disproportionation reaction of this invention can be carried out at temperatures between 350C and about 2000C. While lower temperatures can be used, the reaction rates are generally too low to be of interest. Temperatures above 2000C can be used, but excess decomposition of the reaction components can occur. The preferred reaction temperatures are from about 500C to about 1250C. The pressure during the disproportionation reaction can be from about atmospheric to about 5000 psig (34470 kiloPascals, kPa). Preferably, the pressure is from about atmospheric to about 1000 psig (6894 kPa). The disproportionation reaction can be carried out in the presence of diluents such as saturated hydrocarbons, e.g., hexane, octane, cyclohexane, aromatic hydrocarbons, e.g., benzene, toluene, or halogenated compounds, e.g., chlorobenzene, chloroform, methylene chloride, bromoform, and the like. The amount of diluent can be expressed as a volume ratio of diluent to the olefin. Suitable volume ratios of diluent to olefin can be from about 0/1 to about 500/1 and preferably from about 1/1 to about 300/1. The presence of oxygen and water has been found to be deleterious to the disproportionation reaction and should be substantially avoided during the reaction. Inert gases such as nitrogen, argon or helium can be used to maintain a dry, inert atmosphere during the reaction. The metal compounds used as components of the catalyst system should be pure, free of oxygen or water, and free of any hydrolysis products. In general, the yield of disproportionation product decreases as the metal compound purity decreases. The functional olefins used in the disproportionation reaction should be dry and free of polar materials such as carboxylic acids or alcohols. A purification step to remove impurities by such methods as filtering through silica gel or alumina and storing over molecular sieves or distilling from suitable drying agents is beneficial. The reaction time period depends on the reaction temperature and pressure as well as on the nature of the particular catalyst system and olefinic reactant used. The reaction time is generally from about 30 minutes to about 120 hours. In accordance with yet another embodiment of the present invention, there is provided a technique for producing internally unsaturated alpha esters from alpha-omega dienes. The technique involves the hydrohalogenation of the diene under conditions which favor maximum production of alphabromo-omega olefin. Suitable dienes include those having 6 to 24 carbon atoms. Typical examples include 1,5-hexadiene; 1,6-heptadiene 1,9-decadiene; 1,7-octadiene; 1,10-dodecadiene and the like. A preferred hydrohalogenation technique involves passing HBr through a solution of the diene. The solvent is preferably a nonpolar hydrocarbon or ether solvent having 4 to 12 carbon atoms per molecule such as diethyl ether, hexane or heptane. The optimum reaction temperature and times can vary depending upon the diene selected; however, generally the bromination is conducted at a temperature in the range of about -100C to about 300C and the reaction is terminated prior to the point where formation of dibromide or other undesired products such as oligomers begins to accelerate. For best results, the hydrohydrogenation is conducted in the presence of a small but effective amount of a free radical initiator such as metachloroperbenzoic acid or other peroxide catalysts such as aroyl peroxides, aryl peroxides, alkyl peroxides, hydroperoxides, and ketone peroxides. Other examples of typical free radical initiators include the azo type free radical initiators described in Encyclopedia of Polymer Science and Technology, Vol. 2, page 278 et seq., 1965 or any of the peroxide type free radical initiators described in the same publication at Vol. 9, page 814 et seq., 1968. Illustrative of azo type free radical initiators are 2,2'-azobis(aliphatic nitriles) such as 2,2'azobisisopropionitrile, 2,2' -azobisisobutyronitrile, 2,2' - azobishexanonitrile, and the like, and azobisalkanes such as 1,l'-azobisbutane, 1, 1'-azobishexane, and 1,1'-azobisoctane. Illustrative of peroxide type free radical initiators are alkyl-aromatic peroxides such as dicumyl peroxide; dialkyl peroxides such as di-t-butyl peroxide, diisobutyl peroxide, diisopropyl peroxide, and diisohexyl peroxide; diperoxy ketals such as 2,2'-bis(t-butyl-peroxy) butane and n-butyl 4,4'-bis(t-butylperoxy) valerate; diacyl peroxides such as dibenzoyl peroxide, diacetyl peroxide, dilauroyl peroxide, and dipropionyl peroxide; peroxy esters such as t-butyl peroxypivalate, t-butyl peroxyacetate, and t-butyl peroxybenzoate; dialkyl peroxydicarbonates such as diisobutyl peroxydicarbonate, and dihexyl peroxydicarbonate; ketone peroxides such as methyl ethyl ketone peroxide, and cyclohexanone peroxide; and hydroperoxides such as cumene hydroperoxide and t-butyl hydroperoxide. The resulting alpha-olefin-omega-halide can then be converted into an internally unsaturated olefin by crossdisproportionation with an alpha or internal hydrocarbyl olefin of the type described previously in this disclosure. Any suitable catalyst system could be employed. Examples of suitable disproportionation catalyst systems include the neutral carbene catalyst systems described previously in this disclosure. Other examples of suitable catalysts are the WCl6 - tetralkyl tin catalyst systems, such as the tungsten hexachloride - tetrabutyl tin catalyst system. The resulting internally unsaturated halide compound can then be readily converted to the ester by a nucleophilic displacement reaction involving the halide and an alkali metal ester, such as sodium acetate or sodium formate. Preferably, such reactions are carried out in the presence of dimethylformamide or a phase transfer agent. In an alternative embodiment, one can first convert the alpha-olefin-omega-halide to an alpha-olefin-omega-ester by such a nucleophilic displacement reaction and then disproportionate the alpha-olefin-omega ester with a hydrocarbyl olefin. Again any suitable catalyst can be employed. The currently preferred catalyst is, however, the carbene catalyst system described above. By using the carbene catalyst system one can take advantage of the fact that the cis to trans ratio in the product can be controlled to some extent depending upon whether the olefin used in the disproportionation is an alpha-olefin or an internal olefin. As indicated above, the alpha-olefin generally gives a higher level of cis isomer than the internal olefin. The alternative techniques disclosed herein involving either the disproportionation of alpha-olefin-omega-esters or alpha-olefin-omega-halides, provides one with the ability to obtain a certain degree of control over the cm trans content of the desired product. By using a disproportionation involving an internal olefin and the unsaturated ester or olefins in general and the unsaturated halide, one can obtain a product having a typically thermodynamic sterochemical isomer ratio. The disproportionation of an alpha olefin and the unsaturated ester, on the other hand, allows one to obtain a product in which the ratio of trans to cis isomer is much lower than that of the typical thermodynamic isomer mixture. The above-described processes followed by traditional chemical transformation steps are particularly useful for forming compounds that either correspond to or are mimics or analogs for the active compounds occurring in the natural pheromone composition of many insects. Examples of the compounds that can be produced according to the present invention which are known to be useful in insect control are Z-13-octadecen-1-ol, Z-5-dodecen-l-ol formate, Z and E-7-dodecen-1-ol formates, Z-9-tetradecene-l-ol formate, Z-ll-hexadecen-l-ol formate, Z-4-decen-1-ol acetate, Z-5-decen-l-ol acetate, Z and E-5-decen-1-ol acetate, Z-5-undecen-l-ol acetate, Z-7 and Z-8 undecen-l-o1 acetate, E and Z-5-dodecen-l-ol acetate, E and Z-7-dodecen-l-ol acetate, E and Z isomers of 7, 8, and 9 dodecen-l-ols, Z isomers of 7, 8, 9, 10 and 1l-tetradecen-l-ols, E isomers of 9 and ll-tetradecen-l-ol, Z and E ll-hexadecen-1-ol, E-6-tetradecen-l-ol acetate, E-7-tetradecen-l-ol acetate, E-9-tetradecen-l-ol acetate, Z-9-hexadecen-1-ol propionate, Z-5-tetradecenal, E-4-tridecen-l-ol acetate, E and Z isomers of ll-hexadecenal, and Z-9-tetradecenal. Some of the cis/trans isomer mixtures produced by the processes disclosed herein have been found to have utility in insect control which to the best of the inventor's knowledge would not have been predicted by those skilled in the art. One particular example is 9-dodecenyl acetate obtained via a disproportionation of the types described herein. A prior art mixture of Z and E isomers having a ratio of 4/1 was known to be effective in disrupting the mating of the Western Pine Shoot Borer, Eucosma sonomana. In view of the fact that it is well recognized that different proportions of E and Z isomers can affect insects differently, it was surprising that the 9-dodecenyl acetate isomer mixture produced in accordance with this invention would also be effective since it contained a much larger proportion of the trans isomer than the prior art mixture. In view of the discovery that even a 2/1 trans to cis ratio mixture was effective, it is considered reasonable to assume that a disruptive effect of varying degree will also be observed for 9-dodecenyl acetate containing isomer ratios greater than 0.25/1 up to about 3/1. Another isomer mixture found to have disruptive activity was the 9-tetradecenyl formate produced by the present invention. While the cis isomer has been recognized as having a disruptive effect upon certain insects, to the best of the inventor's knowledge there has been no indication that a cis/trans isomer mixture of that compound would be effective. In view of the results disclosed below, it is now however considered that a disruptive effect will be obtained on Heliothis spp. with trans to cis mixtures of 9-tetradecenyl formate, particularly those mixtures having trans to cis ratios in the range of about 1/1 to 6/1, and more particularly 2/1 to 5/1. (It is noted that another nomenclature for the 9-tetradecenyl formate is 9-tetradecen-l-ol formate. Similar nomenclature exists for the other products obtained in accordance with this invention. As a matter of convenience, the shortened nomenclature has been used throughout to refer to the internally unsaturated terminally functional products of this invention.) Still another isomer mixture found to have disruptive effect upon the Heliothis zea is that of 9-hexadecenyl alcohol. Still yet another isomer mixture found to have disruptive effect upon the Heliothis species is that of 9-tetradecenal. While the cis form of this compound has been recognized as useful in dealing with Heliothis spp., to the best of the inventor's knowledge there has not heretofore been any recognition of the fact that such a cm trans isomer mixture could be effective as a disruptant. A still better understanding of the present invention and its advantages will be provided by the following examples. The non-functional and functional olefins used in the following examples were commercial materials which were usually distilled, contacted with silica gel or alumina and stored over 4 A molecular sieves. Diluents were usually distilled from the appropriate drying agent and stored over 4 A molecular sieves. The various metal halides and organometallics were commercial materials which were normally used without further purification, but with careful exclusion of moisture and oxygen. In several cases, fresh reagents were found to give better disproportionation results than older reagents which are believed to have changed in chemical composition, for example by hydrolysis during aging. During the reaction evaluations, it was found that the careful exclusion of oxygen and moisture from the reaction system was extremely important for successful disproportionation results. The carbene complexes were prepared by published procedures. Typically, they were prepared by reacting the appropriate metal carbonyl with an organolithium compound and then adding a trialkyloxonium tetrafluoroborate. For example, tungsten hexacarbonyl was reacted with phenyllithium and was then reacted with trimethyloxonium tetrafluoroborate to form (methoxyphenylcarbene )pentacarbonyltungsten( 0) EMI11.1 The carbene complexes were stored in a desiccator in a freezer before use in a reaction. Some of the runs in the following examples were carried out in 10 oz. or 32 oz. beverage bottles equipped with a magnetic stirrer, a self-sealing elastomeric cap liner, and a three-hole crown cap. The liquid reaction components were charged to the dried, nitrogen flushed bottle by syringe through the cap. Solids were added to the bottle before attaching the cap. The reaction mixture was heated to the desired temperature and stirred at the reaction temperature for the desired time period. Venting was accomplished by means of a syringe needle through the bottle septum. The needle is attached to an oil filled bubble-tube capped with a Drierite filled drying tube. Some of the runs in the following examples were carried out in 300 mL or 1000 mL Hastelloy C magnedrive packless autoclave. A side port on each autoclave was equipped with a ball valve to allow passage of a syringe needle into the autoclave. In some runs the reactions were vented by manually opening a valve to allow the autoclave to vent to the desired lower pressure. In other runs, venting was accomplished by means of a variable pressure relief valve which was self-sealing if the pressure dropped below the set pressures. The autoclave was sealed empty, purged with dry nitrogen and heated to 1500C or higher for at least one hour, then cooled under a nitrogen sweep to room temperature. The autoclave was left sealed under at least 30 psig N2 and left overnight (for convenience the reactor was dried the day before use). The next day a slight N2 sweep was again started and the reagents added by syringe through a ball valve which was also the nitrogen vent. The order of reagent addition does not appear critical but the following order was utilized: 1) solvent; 2) olefins; 3) solution of carbene; and 4) solutions of cocatalysts. GC standards were added prior to the olefins or if the standard could not be tolerated by the catalyst, at the end of reaction. The ball valve was then closed and the reactor pressurized with nitrogen to the desired pressure. Heating by means of an external heater and stirring were then started. (Temperatures were controlled by means of either a Thermoelectric &num;400 or an Eurotherm Temperature Controller. Temperatures were determined with Type J thermocouples placed in the autoclave thermowell and were read from an Acromag Temperature Indicator. Pressure readings were made visually from gauges on the autoclave.) Heating and stirring were continued for 2 to 8 hours. Time of reaction was measured from the point reaction temperature was reached, thus, the overall time the reagents were heated in the reactor was somewhat longer than indicated. When the desired time of reaction was reached the heater was removed and compressed air was used to cool the exterior of the reactor. The reactor was then vented to atmosphere and opened. The reaction mixture was removed. Analysis and work up was the same as that of the beverage bottle reactions. Reactions carried out at atmospheric pressure were run in an oven-dried 3-neck flask (1, 3, 5, and 12 liter flasks were employed). The flask was equipped with a magnetic or a mechanical stirrer, a dry ice or water condenser and a septum inlet. Once sealed, the reactor was flushed with a nitrogen flow and kept under a nitrogen atmosphere while the reagents (carbene plus metal halide catalyst components, solvent, functional olefin reactant) were added. The flask was then heated to the desired reaction temperature, typically about 8O0C, and introduction of the gaseous olefinic reactant was begun via the septum inlet. Alternatively, the carbene plus metal halide catalyst compo-nents and solvent could be charged to the reactor first, then the olefinic reactant introduced and allowed to react for a period of time before the functional olefin reactant is introduced. In this manner, an alphaolefin reactant, such as 1-butene, can be converted, in situ, to an internal olefin (3-hexene) which typically gives a higher trans-content product when cross-disproportionation of a functional and non-functional olefin is carried out. Yields were determined by gas chromatography (G.C.) employing internal standard. Yields are calculated based on the amount of functional olefin charged as that is generally the limiting reagent. A Perkin Elmer Sigma 3 chromatograph with flame ionization detector was used. Either a 1/8 in x 10 ft 10% or225 on Chromosorb P or a 1/8 in x 10 ft 10% Altech CS-8 on Chromosorb W-AW column was employed. Cis-trans determinations were accomplished using a s in x 16 ft 15% Silar lOC glass column, and were confirmed by C-13 analysis of isolated product. For product isolation, the reactor contents were diluted with solvent, then treated with enough 10% aqueous ammonium hydroxide to precipitate the transition metal complexes. The solution, normally yellow in color, was filtered. The organic layer was washed with water, and then with water saturated with sodium chloride, and dried over anhydrous magnesium sulfate. The dried organic layer was then filtered and solvent removed. The residue thus obtained was ready for distillation. Example I 9-Tetradecenyl Acetate from 1-Hexene and 9-Decenyl Acetate A series of runs were carried out for the preparation of 9-tetradecenyl acetate from l-hexene and 9-decenyl acetate. Except as noted in Table I, the carbene employed was (methoxyphenylcarbene )pentacarbonyltungsten (0), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities employed, reaction conditions and reaction results are presented in Table I. Table I 1-Hexane, Acetate, Catalyst, Mol Time Temp., Press., Run &num; Mol Mol Carbene SnCl4/SiCl4 Dilent, mL Hrs. C psig Yield trans/cis 1 0.22 0.22 0.001 0.022/0.044 C6H5Cl 70 4 80 80 8.6 1.8 2 0.22 0.11 0.001 0.022/0.044 C6H5Cl 90 4 82 80 14.4 2.0 3 0.44 0.22 0.004 0.088/0.166 C6H5Cl 180 4.5 82 5 28.3 3.2 4 0.44 0.22 0.001 0.022/0.044 C6H5Cl 90 4.5 84 10 38.6 3.1 5 0.44 0.11 0.001 0.022/0.044 C6H5Cl 90 4.5 85 3 28.4 3.0 6 0.44 0.22 0.001 0.022/0.044 C6H5Cl 90 4.5 82 10 39.6 2.8 7 0.44 0.11 0.001 (WCl6) 0.002 Hexane 115 4 104 60 11.7 1.5 8 0.44 0.22 0.001 0.01/0.02 C6H5Cl 100 4 80 20 6.3 1.6 9* 0.88 0.44 0.002* 0.02/0.04 C6H5Cl 200 5 79 5 3.5 1.9 10** 0.44 0.22 0.002** 0.02/0.04 C6H5Cl 100 5 78 5 0.7 n.d. 11 1.78 0.89 0.0033 0.033/0.099 Hexane 200 5 79 10 24.6 1.8 12 1.88 0.89 0.002 0.04/0.08 C6H5Cl 160 4.5 77 5 10.5 1.3 13 1.78 0.89 0.0022 0.022/0.044 C6H5Cl 210 5 81 5 18.8 1.5 14 0.44 0.22 0.001 0.01/0.02 C6H5Cl 47 7 85 10 29.5 1.7 15 0.44 0.22 0.001 (WCL6) 0.002 C6H5Cl 40 4 81 10 36.5 2.3 16 0.89 0.44 0.002 0.02/0.04 C6H5Cl 200 4.5 83 5 30.7 1.8 17 0.11 0.056 0.00025 0.0025/0.005 Hexane 22 20 80 - 25.2 1.8 18 0.89 0.22 0.001 0.01/0.02 Hexane 50 5 78 30 18.6 1.7 19 0.89 0.22 0.001 0.01/0.02 C6H5Cl 50 5 76 60 9.9 1.5 20 0.89 0.44 0.002 0.02/0.04 Hexane 200 5 78 60 14.4 1.7 21 1.78 1.78 0.004 0.04/0.08 Hexane 80 4 80 35 15.1 1.7 22 0.88 0.44 0.001 0.01/0.02 Hexane 150 5 81 30 15.6 1.7 23 1.78 0.89 0.004 0.04/0.08 Hexane 80 4 84 35 16.1 1.8 24 0.22 0.11 0.001 0.01/0.02 C6H5Cl 100 4 84 5 39.1 2.8 25 0.22 0.11 0.001 0.01/0.02 C6H5Cl 100 4 87 95 24.0 2.5 26 0.22 0.22 0.001 0.01/0.02 C6H5Cl 100 4.5 88 40 12.7 1.7 27 0.44 0.11 0.001 0.01/0.02 C6H5Cl 100 4 87 20 36.0 2.8 28 0.22 0.11 0.0005 0.01/0.02 C6H5Cl 90 4 81 10 21.9 2.0 29 0.88 0.22 0.002 0.04/0.08 C6H5Cl 140 4 79 60 25.5 1.6 30 15.7 4.1 0.011 0.2/0.4 C6H5Cl 500 42 70 atm. 22.8 1.3 31 0.5 0.05 0.0003 0.002/0.04 C6H5Cl 50 4 101 70 16.3 1.3 32 0.5 0.12 0.0005 0.011/0.022 C6H5Cl 60 2 106 80 11.0 1.6 * (ethoxyphenylcarbene)pentacarbonyltungsten(O). **(methoxymethylcarbene)pentacarbonyltungsten(O). The results in Table I demonstrate that the yield and trans/cis ratio of desired cross-disproportionation product is seen to vary as a function of 1) functional/nonfunctional olefin ratio (compare Runs 1, 2 and 4), 2) olefin/ carbene ratio (compare Runs 12 and 14), 3) carbene/metal halide ratio (compare Runs 6 and 14), 4) the metal halide employed (compare Runs 7 and 20), 5) solvent employed (compare Runs 16 and 22, 20 and 21); 6) the amount of solvent employed (compare Runs 21, and 29); 7) reaction pressure (compare Runs 26 and 27). Example II Synthesis of 5-Decene An oven-dried 2-L, 3-neck round bottom flask was equipped with a magnetic stirrer and a reflux condenser. The condenser outlet was connected to a mercury filled bubble tube capped with a CaSO4 drying tube. The open necks of the reaction flask were capped with septa. The reagents were charged via syringe through the septum, then the vessel was heated to 80C for 24 hours. In an exemplary reaction, 672 g (8 mol) of hexene were reacted in the presence of 0.0045 mol (methoxyphenyl)pentacarbonyltungsten(O), 0.10 mol SnCl4 and 0.15 mol SiC14 with about 100 mL chlorobenzene as solvent. After 24 hours, reaction mixture was treated with aqueous ammonium hydroxide, extracted, and distilled. An isolated yield of 46% was obtained. The 5-decene had a trans to cis ratio of about 4:1. Example III 9-Tetradecenyl Acetate from 5-Decene and 9-Decenyl Acetate A series of runs were carried out for the preparation of 9-tetradecenyl acetate from 5-decene having a trans/cis ratio of about 4:1 and 9-decenyl acetate. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O), and the metal halide catalyst component, unless otherwise noted, consisted of a mixture of SnCl4 and SiCl4. Reagent quantities employed, reaction conditions and reaction results are presented in Table II. Table II 5-Decene, Acetate, Catalyst, Mol Time Temp., Press., Run &num; Mol Mol Carbene SnCl4/SiCl4 Dilent, mL Hrs. C psig Yield trans/cis 1 0.22 0.22 0.0005 0.01/0.02 C6H5Cl 90 4.5 84 40 20.5 5.0 2 0.22 0.22 0.001 0.01/0.02* C6H5Cl 150 4 100 70 23.7 6.0 3 0.55 0.55 0.0025 0.025/0.05 C6H5Cl 325 4.5 101 50 45.3 5.0 4 0.55 0.55 0.0025 0.025/0.05 C6H5Cl 325 4 100 100 59.2 5.1 5 1.11 1.11 0.0025 0.025/0.05 C6H5Cl 125 5 95 130 28.4 7.0 6 0.11 0.11 0.0005 0.01/0.02 C6H5Cl 90 4.5 83 45 30.0 4.7 7 0.22 0.22 0.001 0.01/0.02 C6H5Cl 100 7 84 40 12.9 5.3 8 0.22 0.22 0.005 0.01/0.01* C6H5Cl 70 4 82 35 9.3 11.1 9 0.56 0.0025 0.0025 0.025/0.04 C6H5Cl 315 4 80 60 37.7 4.0 10 0.056 0.056 0.00025 0.0025/0.005 Hexane 22 20 80 - 45.7 5.0. 11 0.42 0.42 0.002 0.02/0.04 Hexane 200 5 84 50 38.0 5.0 12 0.11 0.0005 0.0005 0.0005/0.01* C6H5Cl 100 4 102 50 15.3 4.4 13 0.11 0.11 0.001 0.01/0.02 C6H5Cl 125 4 84 35 13.7 7.2 14 0.11 0.11 0.0005 0.005/0.01 C6H5Cl 100 4 101 50 43.6 4.9 15 0.22 0.22 0.0005 0.005/0.01 Hexane 75 5.5 98 80 12.6 8.0 16 0.11 0.11 0.001 0.01/0.02 C6H5Cl 125 5 95 75 45.0 3.6 17 0.22 0.11 0.001 0.01/0.02 Hexane 125 4 81 40 51.1 4.4 18 0.11 0.11 0.0005 (WCL6) 0.1 C6H5Cl 70 4 108 70 33.6 5.8 19 0.42 0.42 0.002 0.02/0.04 Hexane 180 4.5 77 80 40.5 4.4 20 1.0 1.0 0.0025 0.05/0.1 None 20 20 80 - 23.0 5.0 21 0.4 0.1 0.0005 (WCL6) 0.001 C6H5Cl 50 4 106 20 60.1 > 20.0 22 0.88 0.44 0.001 0.01/0.02 Hexane 150 5 81 30 15.6 #20.0 *SnCl4/GeCl4 The results in Table II demonstrate the higher trans/cis ratios obtained as a result of substituting the internal olefin, 5-decene, for the alpha-olefin l-hexene of Example I. A typical trans/cis ratio of 5:1 or greater is obtained upon reaction of 5-decene with 9-decenyl acetate. Example IV Preparation of 1, 18-Diacetoxy-9-Octadecene The 300 mL autoclave was charged with 9-decenyl acetate (0.22 mol), (phenylmethoxycarbene)pentacarbonyltungsten(o) (0.001 mol), SnC14 (0.01 mol), SiC14 (0.02 mol) and 20 mL chlorobenzene. The autoclave was heated to 860 for 4 hours with continuous venting above 5 psig. The reaction product, following removal of catalyst components, was vacuum distilled at 0.35 mm Hg. Material boiling between 205-2300C was collected and found to be pure 1,18-diacetoxy-9-octadecene. The trans/cis ratio of distilled product was 1.7. The crude reaction product was purified by standard crystallization techniques from ethanol solvent. The crystals so obtained were collected by filtration, analyzed, and found to be essentially pure trans-1,18-diacetoxy-9-octadecene. Example V 9-Tetradecenyl Acetate from l-Hexene and trans-l, 18-Diacetoxy-9-Octadecene A series of runs were carried out for the preparation of 9-tetradecenyl acetate from 1-hexene and the trans-1,18,- diacetoxy-9-octadecene prepared as set forth in the preceding example. The carbene employed for the disproportionation of the acetate was (methoxyphenylcarbene )pentacarbonyltungsten (0) and the metal halide catalyst component consisted of a mixture of SnCl4 and SiC14. The acetate product obtained was essentially all trans. Example VI 9-Tetradecenyl Acetate from 5-Decene and trans-1,18-Diacetoxy-9-Octadecene A series of runs were carried out for the preparation of 9-tetradecenyl acetate from 5-decene having a trans/cis ratio of about 4:1 and trans-l,18-diacetoxy-9 octadecene. Unless otherwise noted, the carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. As in Example V, essentially all trans product was obtained. Exile VII 9-Tetradecenyl Acetate from Mixed Cis/Trans-1,18-Diacetoxy-9-Octadecene A series of runs were carried out for the preparation of 9-tetradecenyl acetate from l-hexene or a trans/cis mixture of 5-decene and 1.7/1 trans/cis mixture of 1,18diacetoxy-9-octadecene. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O), and the metal halide component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities reacted, reaction conditions and reaction results are presented in Table III. Table III Acetate, Catalyst, Mol Time Temp., Press., Run &num; Alkene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/cis 1 1-Hexene, 0.44 0.22 0.001 0.011/0.002 C6H5Cl 120 4 92 30 16.3 4.4 2 5-Decene, 0.44 0.22 0.001 0.011/0.002 C6H5Cl 120 4 96 15 3.1 5.5 3 5-Decene, 0.44 0.19 0.001 0.011/0.002 C6H5Cl 120 4 91 15 10.9 5.8 The results in Table III demonstrate when trans/cis mixture 1,18-diacetoxy-9-octadecene is employed, less trans isomer is obtained than when the octadecene reactant is substantially all trans. The trans level is slightly higher with the internal olefin reactant than the alpha-olefin reactant. Example VIII 9-Tetradecenyl Acetate from l-Hexene and Oleyl Acetate A series of runs were carried out for the preparation of 9-tetradecenyl acetate from l-hexene and oleyl acetate. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiC14. Reagent quantities reacted, reaction conditions and reaction results are presented in Table IV. Table IV Acetate, Catalyst, Mol Time Temp., Press., Run &num; 1-Hexene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/cis 1 0.44 0.11 0.0005 0.011/0.022 C6H5Cl 60 4 109 40 7.1 6.5 2 0.44 0.11 0.0005 0.011/0.022 C6H5Cl 60 4 108 40 8.1 2.1 3 0.44 0.11 0.0005 0.011/0.022 C6H5Cl 60 2 107 200 7.8 1.6 4 0.44 0.22 0.0005 0.011/0.022 C6H5Cl 30 2.25 105 185 3.8 1.5 On the average, a low trans/cis ratio product was obtained. Example XX 9-Tetradecenyl Acetate from 5-Decene and Oleyl Acetate A series of runs were carried out for the preparation of 9-tetradecenyl acetate from a trans/cis mixture of 5-decene and oleyl acetate. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities reacted, reaction conditions and reaction results are presented in Table V. Table V Acetate, Catalyst, Mol Time Temp., Press., Run &num; 5-Decene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/cis 1 0.4 0.11 0.0005 0.011/0.022 C6H5Cl 60 4.5 105 10 6.3 2.1 2 0.4 0.11 0.0005 0.011/0.022 C6H5Cl 60 4.5 92 100 9.8 12.3 The results in Table V demonstrate if 5-decene is employed it is possible to obtain a higher trans/cis ratio than when oleyl acetate was reacted with 1-hexene. Example X 9-DodecenYl Acetate from 1-Butene and 9-Decenyl Acetate A series of runs were carried out for the preparation of 9-dodecenyl acetate from 1-butene and 9-decenyl acetate. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungsten(O). Runs were made using each of the metal halide catalyst components, i.e., WC16, or a mixture of SnCl4 and SiCl4, or a mixture of SnCl4 and GeC14. Trans/ cis ratios of 1.2-5.0 were obtained with a 1.7 average. Example XI 9-Dodecenyl Acetate from 1-Butene and Oleyl Acetate A series of runs were carried out wherein 9-dodecenyl acetate was prepared from l-butene and oleyl acetate. The carbene employed was (methoxyphenylcarbene) pentacarbonyltungsten(O), and the metal halide was WC16 or a mixture of SnCl4 and SiCl4. The trans/cis ratios were in the range of 1.1 to 1.2/1. For the best results in terms of yield excess l-butene was needed. Example XII 9-Dodecenyl Acetate from 3-Hexene and 9-Decenyl Acetate Several runs were carried out for the preparation of 9-dodecenyl acetate from 3-hexene and 9-decenyl acetate. The carbene employed was (methoxyphenylcarbene ) pentacarbonyl - tungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities employed, reaction conditions and reaction results are presented in Table VI. Table IV Acetate, Catalyst, Mol Time Temp., Press., Run &num; 3-Hexene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/cis 1 0.5 0.25 0.0005 0.005/0.01 C6H5Cl 60 4 105 50 7.8 5.2 2 1.61 0.25 0.002 0.01/0.02 C6H5Cl 120 6 90 40 69.1 5.4 3 1.61 0.25 0.002 0.01/0.02 C6H5Cl 20 6 87 40 #70.0 5.3 4 3.22 0.50 0.002 0.02/0.02 C6H5Cl 220 5 92 40 - 5.4 5 3.22 0.50 0.002 0.02/0.04 C6H5Cl 220 6 84 35 44.4 5.4 The results in Table VI demonstrate that the trans/cis ratio of 9-dodecenyl acetate typically obtained with the internal olefin, 3-hexene is significantly higher than that normally obtained with the terminal olefin, l-butene. Example XIII 9-Tetradecenyl Acetate and 9-Undecenyl Acetate from 9-Decenyl Acetate and 2-Heptene Several runs were carried out employing cis- or trans-2-heptene with 9-decenyl acetate or 1,18-diacetoxy-9octadecene having a trans to cis ratio of 1.7:1 in the presence of (methopyphenylcarbene)pentacarbonyl-tungsten(O) and SnC14 plus SiC14 as the metal halide catalyst component. The trans/cis ratio of the 9-tetradecenyl acetate was in the range of 2.6-3.4, for the 9-undecenyl acetate it was in the range of 1.6 to 4.9. The 2-heptene produced slightly less trans isomer than an internal symmetrical olefin. The cis isomer of 2-heptene produced even less trans product than the trans isomer of 2-heptene. Example XIV 9-Tetradecenyl Formate from 9-Decenyl Formate Several runs were carried out for the preparation of 9-tetradecenyl formate from 9-decenyl formate and l-hexene or 5-decene. The carbene employed was (methoxyphenylcarbene)- pentacarbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities employed, reaction conditions and reaction results are presented in Table VII. Table VII Formate, Catalyst, Mol Time Temp., Press., Run &num; Alkene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/cis 1 1-Hexene, 0.22 0.11 0.002 0.02/0.04 Hexane 100 5 103 80 7.4 1.8 2 1-Hexene, 0.89 0.44 0.002 0.02/0.04 C6H5Cl 200 4.5 78 5 trace 3 5-Decene, 0.26 0.11 0.001 0.01/0.02 Hexane 80 4 107 55 3.0 #20.0 4 5-Decene, 0.22 0.11 0.001 0.01/0.02 C6H5Cl 125 5 102 50 28.1 5 5-Decene, 0.11 0.22 0.001 0.01/0.02 Hexane 150 4 101 45 trace - The e results in Table VII demonstrate that the ratio of olefin reactants to the carbene catalyst can effect the yield. In the reactions in which the yield was significant, the alpha-olefin (1-hexene) gave 9-tetradecenyl formate with a trans/cis ratio of about 2/1 while the internal olefin (5-decene) gave 9-tetradecenyl formate with a trans/cis ratio of about 20/1. Example XV 9-Tetradecenyl Propionate from 9-Decenyl Propionate Two cross-disproportionation reactions of 9-decenyl propionate were carried out employing l-hexene and 5-decene. The carbene catalyst employed was (lethoxyphenylcarbene )penta- carbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiC14. The solar ratio of the 9-decenyl propionate to the carbene was 220/1. The molar ratio of carbene to SnCl4 was 10/1 and the molar ratio of SiC14 to SnC14 was 2/1. The 5-decene was employed in a 1/1 molar ratio with the propionate. The l-hexene was employed at a 2/1 ratio. The trans/cis ratio obtained with the l-hexene was 1.8/1. The trans/cis ratio obtained with the 5-decene was 4.4/1. Example XVI 9-Tridecenyl Acetate from 9-Decenyl Acetate Two cross-disproportionation reactions of 9-decenyl acetate were carried out with 1-pentene or trans-4-octene. The carbene employed was (methoxyphenylcarbene)pentacarbonyl- tungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. The relative amounts of olefins, carbene, SnCl4 and SiCl4 were as in the preceding example. Here again the alpha-olefin produced a lower trans level than the internal olefin, namely 1.7/1 as compared to 12/1. Example XVII 9-Hexadecenyl Acetate from 9-Decenyl Acetate Several runs were carried out for the preparation of 9-hexadecenyl acetate from 9-tetradecenyl acetate and l-octene or 7-tetradecene. The carbene employed was (methoxyphpenylcarbene)pentacarbonyltungsten(O), and the metal halide component consisted of a mixture of SnCl4 and SiCl4 The end product obtained with the terminal non-functional olefin was relatively low in trans content about 1.8 trans to cis. The trans content of the product obtained with the internal olefin was not determined. Example XVIII 4-Nonenyl Acetate from 5-P entenyl Acetate and l-Bexene or 5-Decene Two cross-disproportionation reactions of 5-pentenyl acetate were carried out with 1-hexene or 5-decene as the second reactant. The carbene employed was (methoxyphenyl carbene )pentacarbonyltungsten(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Again, the internal olefin was found to give a much higher trans- content product than does the terminal olefin reactant, 2.1/1 vs. 6.5/1 for these two reactions. Exawnle XIX Methyl-10-Pentadecenoate from Methyl-10-Undecenoate Two cross-disproportiozation reactions of methyl- 10-undecenvate were carried out with 1-hexene or 5-decene as the second reactant. The carbene employed was (methoxyphenylcarbene)pentacarbonyltungen(O), and the metal halide catalyst component consisted of a mixture of SnCl4 and SiCl4. Reagent quantities employed, reaction conditions and reaction results are presented in Table VIII. Tabele VIII Undecenoate, Catalyst, Mol Time Temp., Press., Run &num; Alkene, Mol Mol Carbene SnCl4/SiCl4 Diluent, mL Hrs. C psig Yield Trans/Cis 1 1-Hexene, 0.44 0.26 0.002 0.02/0.04 C6H5Cl 100 4.5 83 5 42.7 2.9 2 5-Decene, 0.26 0.26 0.002 0.02/0.04 C6H5Cl 100 5 82 60 66.9 4.0 The results again demonstrate that the internal olefin gives a product having a higher trans content than the alpha-olefin Example XX Field Tests 9-Dodecenyl Acetate Three adjacent test plots 2000 ft wide and 4000 ft long in a ponderosa pine plantation in Oregon were used to evaluate a high trans-9-dodecenyl acetate product for its utility in controlling the Western Pine Shoot Borer, viz. Encosoma sonomana. The first plot was treated with commercially available pheromone for the Western Pine Shoot Borer, i.e., a 4/1 cis/trans 9-dodecenyl acetate at a rate of 4 grams/acre using commercially available dispensing Beans such as those disclosed in U. S. 4,160,335 and U. S. 4,198,782. The middle plot was treated in the same manner and at the same rate with 9-dodecenyl acetate prepared according to the present invention. The 9-dodecenyl acetate had a cis/trans ratio of 1/2. The third plot was not treated with any 9-dodecenyl acetate- - in order to serve as a control. The applications were carried out during the week of 3/30/81 and trap catches 4/27 4/30 and 4/30 - 6/2/81. Tree damage was observed at the end of the growing season in the fall of 1981. Trap catch data and tree damage results are presented in Table IX. Table IX Total Trap Catches Commercial (4/1) Inventive (1/2) Control 4/3 - 4/27 0 4 45 4/27 - 4/30 0 1 39 4/30 - 6/2 0 3 65 x Tree Damage 21.5 24.0 39.8 The results presented in Table IX demonstrate the effectiveness of a 1/2 cis/trans ratio of 9-dodecenyl acetate for the disruption of mating of Western Pine Shoot Borer. In addition, the reduction of tree damage is comparable to the reduction obtained with the commercially available 4/1 cis/ trans 9-dodecenyl acetate. This inventive composition gave a 40% reduction in tree damage and the commercial composition a 46% reduction. It should be noted that X reduction in tree damage obtained in these tests is significant but even for the commercial product the results were not as good as results previously obtained with the product. The difference in the effectiveness of the commercial material is attributed to a problem observed in the application of the flake dispensing means. The same problem existed for the inventive composition. The problem involved the fact that a large portion of the flakes fell to the ground rather than becoming stuck in the trees. Another evaluation was conducted of the 1/2 cm trans product in 1982 employing improved application technology. In one plot 6,000 Hercon flake dispensing means were applied per acre to provide 4 gm per acre of the 1/2 isomer mixture. In another plot, 12,000 flake dispensing means were applied to provide 8 gm per acre of the 1/2 isomer mixture. The effects as compared to a control plot where no pheromone was applied are summarized in Table IXA. Table IXA 4 gm/acre 8 gm/acre Control % Tree Damage 7.75 5.75 39.75 Total Trap Catches 0 0 239 The 4 gm/acre application gave an 81% reduction in tree damage and the 8 gm/acre application an 86% reduction. This is further evidence that the 1/2 isomer fixture is effects tive in disrupting the mating of Eucosma sonomana. In addition, these results are within the acceptable range for economical commercial application. Example XXI Field Tests - Tetradecenyl Formate Fields of cotton in a late fruiting stage were used to evaluate the effectiveness of tetradecenyl formate in controlling Heliothis species. In this case, the 9-tetradecenyl formate was prepared from 9-tetradecenyl acetate (5/1 or 2/1 trans/cis content) rather than directly from 9-decenyl formate. In a typical process 21.1 g (o.Q8 mol) of tetradecenyl acetate, 22.2 g (0.16 mol) K2CO3, 200 mL methanol, and 2 iii water were added to a 500 mL one neck round bottom flask. The mixture was stirred for two hours at room temperature. Then 200 mL of diethyl ether was added, and the mixture was filtered. The ether layer was washed with water, then saturated NaCl solution, then dried over MgS04. The dried solution was filtered and concentrated on a rotary evaporator. The product consisting of 9-tetradecenyl alcohol was then reacted with formic acid in benzene at gentle reflux (-BO0C) for 24 hours. Then additional formic acid was added and the gentle reflux continued for another 24 hours. The 9-tetradecenyl formate was recovered by extraction. Test plots measured 200 ft long and 100 ft wide and contained 60 rows. Plots were separated from each other by at least 200 ft down row and by 100 ft across rows. The test compound was laminated between ·" x ·" plastic flaks. Plots were treated with formats at the rate of 10 grams/acre. In another plot flakes were used containing Z-ll-hexadecenal, which has been reported as one of the components in the natural pheromone of H. Zea and virescens. The chemicals were applied on 8/12/81 and 9/1/81 and insects were monitored on the nights of 8/12-14 and 9/1-9, respectively. Separate traps were put out for Heliothis zea and Heliothis virescens. Trap catch data are presented in Table X. Table X Total Trap Catches 5/1- g/1 Z-11-HDA Control 8/12-14 H. zea 5 2 0 87 H. virescens 30 . 34 45 213 9/1-9 H. zea 18 1 1 20 H. virescens 18 6 4 21 The results presented in Table X demonstrate the effectiveness, a 2/1 trans/cis ratio of 9-tetradecenyl formate for the disruption of mating of both Heliothis species. The 5/1 trans/cis ratio 9-tetradecenyl formate was also effective for disruption of mating Reliothis species. Example XXII Field Tests - 9-Tetradecenal A 2/1 trans to cis ratio of 9-tetradecenal was evaluated in the same manner as was used in the preceding example. Z-9-tetradecenal which has been reported as a component in the natural pheromone of H. Zea was used for comparison. The e 9-tetradecenal was prepared from 9-tetra- decenyl alcohol prepared in the same manner as described in the preceding example. About 21 grams of the alcohol in a 50/50 weight ratio selection of dichloromethane was added dropwise to a flask charged with 43 g (0.2 mol) pyridinium chlorochromate, 20 g celite and 200 mL dichloromethane. The mixture was stirred at room temperature for about 2 hours after addition of the alcohol solution was complete. Then 200 mL of hexane was added and the mixture was filtered. The solvent was evaporated and the product vacuum distilled through a 2 ft. x 3/4 in. packed column (Penn State stainless steel packing). A 36% yield of pure 9-tetradecenyl acetate was obtained. The trap catch results are set forth in Table XI. Table XI Total Trap Catches Test Plot Z-9-TDA Control Plot 8/12-14 H. sea 1 9 87 H. virescens 44 24 213 9/1-9 H. sea 13 1 20 H. 'Nirescens 2 3 21 The results presented in Table XI demonstrate the effectiveness of a 2/1 trans/cis ratio of 9-tetradecenal for the disruption of mating of the Heliothis species. Example - XXIII Field Test - 9-Hexadecenyl Alcohol The effect of a 2/1 trans/cis mixture of 9-hexadecenyl alcohol on Heliothis species was tested in the same manner as described in Example XXI. Z-ll-hexadecenyl alcohol was used in a comparison test. The alcohol was prepared by the hydrolysis of 9-hexadecenyl acetate. The results are shown in Table XII. Table XII Total Trap Catches Test Plot Z-ll-HDOH Control Plot 8/12-14 H. zea 30 6 87 H. virescens 58 37 213 9/1-9 H. zea 10 19 20 H. virescens 56 28 21 The results presented in Table XII demonstrate the effectiveness of a 2/1 trans/cis ratio of 9-hexadecenyl alcohol for the description of mating of Heliothis zea. Results for the description of Heliothis virescens are mixed, the 9-hexadecenyl alcohol showing disruptive activity in one test, but not in the other. Example XXIV Six hundred mL of a hexane solution of 1,7-octadiene (110 g, 1 mol) was added to a 2 L three-neck flask equipped with a bubble tube, a magnetic stir base, and a condenser and about 10 mg of metachloroperbenzoic acid was added. The flask and contents were cooled to about 0 C and HBr (80 g, 1 mol) was bubbled into the liquid in the flask over about 2 hours after being passed through a CCl4 solution of phenol which removed any free bromine that might have been present in the HBr. By keeping the extent of diene conversion to less than about 50%, it was possible to obtain a 60% selectivity to 8-bromo-1-octene. The reaction product was washed with equal volume 10% aqueous Na2CO3 and then with an equal volume saturated aqueous NaCl solution. The recovered organic layer was dried over anhydrous MgSO4 and then filtered. Distillation at reduced pressure was used to separate the 8-bromo-1-octene (bp 81 to 820C at 11 mm Hg) from the dibromo- octene. Recovered 8-bro o-1-octene was then reacted with l-hexene in an autoclave according to the general procedure set forth above in the presence of the homogeneous catalyst system of (methoxyphenylcarbene) pentacarbonyl tungsten(0) (10 mL of 1M catalyst in hexane) and a mixture of SnCl4 (1 mL, 0.01 mol) and SiCl4 (2.3 mL, 0.02 mol). The reaction was carried out for two hours at 80 C and about 40 psig. The reaction product included 7-dodecenyl bromide. From G. C. analysis it appeared that the trans/cis ratio of the bromide isomers was about 3/1. In an oven dried one liter three-neck flank equipped with a magnetic stirrer and a reflux condenser, 46.5 g 7-dodecenyl bromide (0.19 mol) prepared as described above was combined with 20 g sodium formate (0.29 mol), and 300 mL dimethylformamide under a N2 atmosphere. The mixture was heated to reflux and stirred for 4-5 hours. GC analysis showed that the reaction was complete. The reaction mixture was cooled and diluted with about 300 kL of ice water and extracted three tines with equal volumes of ether. The ether layer was then washed with an equal volume H2o, then two times with equal volumes of NaCl saturated H2O, and finally the organic portion was dried over anhydrous )(gSO4. The resulting material was then distilled to obtain a product comprising 7-dodecenyl formate having a trans to cis isomer ratio of about 3/1 (bp 86 to 870C at 0.5 mm Hg). Example XXV A hexane solution of 1,9-decadiene was reacted with HBr in the presence of metachloroperbenzoic acid in the same manner as the 1,7-octadiene was reacted in the preceding example. The reaction product was also worked up as described above. The product boiling between 106 and 1120C at 7 to 8 mm Hg was essentially pure 9-decenyl bromide. About 90 mL (0.5 mol) of 9-decenyl bromide, 100 mL (0.8 mol) of 1-hexene, 2Q mL of a 0.1 N chlorobenzene solution of (methyloxyphenylcarbene) pentacarbonyl tungsten(0) (0.002 mol) 2.8 mL (0.020 mol) SnCl4, 5.2 mL (0.040 mol) SiCl4 were combined and heated at about 800C and about 120 psig for about 2 hours in 100 mL of chlorobenzene. The trans/cis isomer ratio in the 9-tetradecenyl bromide product was about 4/1 as shown by gas chromatography. An analogous disproportionation reaction was carried out using 50 mL (0.23 mol) of 9-decenyl bromide, 87 mL (0.46 mol) of 5-decene, 10 mL of 0.1 M chlorobenzene solution of the carbene catalyst (0.001 mol), 1.4 mL (0.01 101) of SnCl4, and 2.6 mL (0.02 mol) of SiCl4 in 100 mL of chlorobenzene. The trans/cis isomer ratio in the 9-tetradecenyl bromide wu about 5/1 as shown by gas chromatography. The 9-tetradecenyl bromide can be readily converted to 9-tetradecenyl acetate by reaction with sodium acetate in DMF as described in the preceding example. The above results indicate that the selection of an internal or alpha-olefin reactant in the cross-disproportiona tion of the unsaturated bromide compounds does not have the same notable effect on the trans/cis ratio a8 it has on those olefins containing ester groups. That is to say whereas internal and alpha-olefins produce quite different isomer ratios when reacted with unsaturated esters there is much less difference when an unsaturated bromide compound is substituted for the unsaturated ester. As will be evident to those skilled in the art, many variations and modificatione of the present invention can be practiced in view of the foregoing disclosure without departing from the spirit and scope thereof. The following part of the description are preferred embodiments 1 to 33 presented in the format of claims. 1. A composition consisting essentially of 9-dodecenyl acetate having a trans/cis ratio greater than 0.25/1. 2. A composition according to claim 1 wherein the trans/cis molar ratio is in the range of about 1/1 to about 3/1. 3. A composition according to claim 2 wherein the trans to cis molar ratio is about 2/1. 4. A process for disrupting the mating of the Western Pine Shoot Borer comprising applying to the infested area an effective amount of the composition of claim 1. 5. A process according to claim 4 wherein the trans to cis molar ratio is in the range of about 1/1 to about 3/1. 6. A composition consisting essentially of an admixture of the cis and trans isomers of 9-tetradecenyl formate. 7. A composition according to claim 6 wherein the molar ratio of trans to cis is in the range of about 6/1 to 1/1. 8. A composition according to claim 8 wherein the molar ratio of trans to cis is about 2/1. 9. A process for disrupting the mating of pests selected from the group consisting of Heliothis spp. comprising applying to the infested area an effective amount of the composition of claim 6. 10. A process according to claim 9 wherein the molar ratio of trans to cis is in the range of about 5/1 to 2/1. 11. A process according to claim 10 wherein the composition is applied in an amount sufficient to disrupt the mating of Heliothis zea. 12. A process according to claim 11 wherein the molar ratio of trans to cis is about 2/1. 13. A process according to claim 9 wherein the molar ratio of trans to cis is about 2/1 and the composition is applied in an amount sufficient to disrupt the mating of Heliothis virescens. 14. A composition consisting essentially of an admixture of the cis and trans isomers of 9-tetradecenal. 15. A composition according to claim 14 wherein the trans to cis ratio is about 2/1. 16. A process for disrupting the mating of pests selected from the group consisting of Heliothis spp. comprising applying to the infested area an effective amount of the composition of claim 14. 17. A process according to claim 16 wherein the trans to cis ratio is about 2/1. 18. A process according to claim 16 for disrupting the mating of Heliothis zea. 19. A composition consisting essentially of an admixture of the cis and trans isomers of 9-hexadecenyl alcohol. 20. A composition according to claim 19 wherein the trans to cis ratio is about 2/1. 21. A process for disrupting the mating of pests selected from the group consisting of Heliothis spp. comprising applying to the infested area an effective amount of the composition of claim 19. 22. A process according to claim 21 wherein the trans to cis ratio is about 2/1. 23. A process according to claim 22 for disrupting the mating of Heliothis zea. 24. A method for producing an internally unsaturated alpha ester comprising hydrohalogenating an alpha, omega diene under conditions suitable for producing an omega-halo-alpha olefin, and then reacting the omega-halo-alpha olefin with a hydrocarbyl monoolefin in the presence of a suitable disproportionation catalyst to obtain an internally unsaturated compound having a terminal halide radical, and then converting the terminal halide radical to an ester radical. 25. A method according to claim 24 wherein said disproportionation is conducted in the presence of a catalytic amount of a catalyst composition comprising effective amounts of (methoxyphenylcarbene) pentacarbonyl tungsten(0), SnCl4 and Sic14 and wherein HBr is used in the hydrohalogenation. 26. A process according to claim 25 wherein 7-dodecenyl formate is produced from 1,7-octadiene. 27. A process according to claim 25 wherein 9-tetradecenyl acetate is produced from 1,9-decadiene. 28. A process for producing an internally unsaturated alpha ester comprising hydrohalogenating an alpha, omega diene under conditions suitable for producing an omega-halo-alpha olefin, and then converting the terminal halide of said omega-halo-alpha olefin to an ester radical, and then reacting the resulting omega-ester-alpha-olefin with a hydrocarbyl monoolefin in the presence of a suitable disproportionation catalyst to obtain a said internally unsaturated alpha ester. 29. A method according to claim 28 wherein said disproportionation is conducted in the presence of a catalytic amount of a catalyst composition comprising effective amounts of (methoxyphenylcarbene) pentacarbonyl tungsten(O), SnCl4 and SiCl4 and HBr is used in the hydrohalogenation. 30. A composition consisting essentially of an admixture of the cis and trans isomers of 9-tetradecenyl acetate. 31. A composition according to claim 30 wherein the molar ratio of trans to cis is in the range of about 6/1 to 1/1. 32. A composition according to claim 31 wherein the molar ratio of trans to cis is about 2/1. 33. A composition according to claim 31 wherein the molar ratio of trans to cis is about 5/1. The following part of the description are preferred embodiments 1 to 40 presented in the format of claims. 1. A method of preparing an internally unsaturated olefin having an oxygen containing functional group comprising reacting (1) a functional monoolefin having at least one terminal functional group selected from groups having the formulas EMI43.1 wherein R is a hydrocarbyl group having 1 to 20 carbon atoms or in the case of the first formula hydrogen with (2) a hydrocarbyl monoolefin consisting essentially of either an internal olefin or an alpha-olefin having at least three carbon atoms per molecule under suitable reaction conditions in the presence of a catalytic amount of a catalyst composition comprising effective amounts of (1) at least one neutral carbene complex having the formula EMI43.2 wherein R' is selected from the group consisting of alkyl or cycloalkyl radicals containing 1 to 10 carbons per radical and aryl or substituted aryl radicals containing 6 to 30 carbon atoms per radical wherein the substituted radicals can have one or more substituents, each of which can be the same or different and selected from the group consisting of halides, alkoxides, and alkyl radicals containing 1 to 20 carbon atoms per radical; wherein Y is S or 0; R" is selected from the group consisting of alkyl, cycloalkyl, aryl, and substituted aryl radicals containing 1 to 30 carbon atoms per molecule and wherein the aryl substituents are as described for R' and wherein if Y is S only one of R' and R" can be aryl or substituted aryl; each L is a neutral ligand individually selected from CO, NO, PR'3, PCl3, PF3, and pyridine, where R' is as defined above, and L' is cyclopentadienyl; p is 0 or 1; and n is 5 when p is 0 or 2 when p is 1; and (2) a metal component selected from the group consisting of the chlorides and bromides of the metals of Groups IVa, IVb, Vb, VIb, VIIb, VIII, and Ib and the oxychlorides and oxybro-ides of iolybdenum, tungsten, vanadium, and chromium, wherein if the metal is vanadium it is in an oxidation state of either 4 or its highest, stable, common, ionic oxidation state; if the metal is molybdenum, tungsten, or rhenium it is in an oxidation state of either 5 or its highest, stable, common, ionic oxidation state; and if the metal is not vanadium, molybdenum, tungsten or rhenium the metal is in its highest, stable, common, ionic, oxidation state. 2. A process according to claim 1 wherein said neutral carbene complex is selected from those wherein R' is selected from phenyl or an alkyl group having 1 to 10 carbon atoms; R" is an alkyl radical having 1 to 10 carbon atoms; Y is O, L is CO, n is 5, and p is 0. 3. A process according to claim 2 wherein said metal component of said catalyst comprises a mixture of SnCl4 and either SiCl4 or Get14. 4. A process according to claim 3 wherein the olefinic hydrocarbyl portion of said functional monoolefin has the formula R"' -CH'CH(CH2),- wherein n is in the range of 2 to 10, R"' is hydrogen or an alkyl radical having 1 to 20 carbon atoms. 5. A process according to claim 4 wherein said hydrocarbyl monoolefin is an alpha-olefin having no more than 20 carbon atoms per molecule. 6. A process according to claim 3 wherein said functional monoolefin is selected from the group consisting of 9-decenyl acetate, oleyl acetate, 1,18-diacetoxy-9-octadecene, 9-decenyl formate, 9-decenyl propionate, 5-pentenyl acetate, and methyl-lO-undecenoate. 7. A process according to claim 6 wherein 9-tetradecenyl acetate is produced by reacting 1-hexene and 9-decenyl acetate. 8. A process according to claim 6 wherein 9-tetradecenyl acetate is produced by reacting a functional olefin consisting essentially of trans-1,18-diacetoxy-9-octadecene with 1-hexene. 9. A process according to claim 6 wherein 9-dodecenyl acetate is produced by reacting 1-butene and 9-decenyl acetate. 10. A process according to claim 6 wherein 9-dodecenyl acetate is produced by reacting 1-butene and oleyl acetate. 11. A process according to claim 6 wherein 9-tetradecenyl formate is produced by reacting 1-hexene and 9-decenyl formate. 12. A process according to claim 6 wherein 9-tetradencyl propionate is produced by reacting 9-dodecenyipropionate and 1-hexene. 13. A process according to claim 6 wherein 9-tridecenyl acetate is produced by reacting 9-decenyl acetate with 1-pentene. 14. A process according to claim 6 wherein 9-hexadecenyl acetate is produced by reacting 9-decenyl acetate with 1-octene. 15. A process according to claim 6 wherein 4-nonenyl acetate is produced by reacting 5-pentenyl acetate with 1-hexene. 16. A process according to claim 6 wherein methyl-lO-penta- decenoate is produced by reacting methyl-lO-undecenoate with 1-hexene. 17. A process according to claim 6 wherein said hydrocarbyl monoolefin is an internal olefin. 18. A process according to claim 17 wherein said internal olefin comprises a symmetrical olefin. 19. A process according to claim 18 wherein said functional monoolefin is selected from the group consisting of 9-decenyl acetate, oleyl acetate, 1,18-diacetoxy-9-octadecene, 9-decenyl formate, 9-decenyl propionate, 5-pentenyl acetate, and methyl-lO-undecenoate. 20. A process according to claim 17 wherein said internal olefin is selected from the group consisting of 5-decene, 2-butene, 3-hexene, 4-octene, and 7-tetradecene. 21. A process according to claim 20 wherein said internal olefin is 5-decene produced by the self-disproportionation of 1-hexene in the presence of the same catalyst specified for the reaction of the functional olefin. 22. A process according to claim 21 wherein said functional olefin reactant consists essentially of the trans isomer of 1,18diacetoxy-9-octadecene. 23. A process according to claim 17 wherein said functional olefin is a symmetrical difunctional olefin consisting essentially of the trans isomer. 24. A process according to claim 17 wherein 9-dodecenyl acetate is produced by reacting 9-decenyl acetate and 3-hexene. 25. A process according to claim 17 wherein 9-tridecenyl acetate is produced by reacting 9-decenylacetate and trans-4-octene. 26. A process according to claim 17 wherein 9-hexadecenyl acetate is produced by reacting 9-decenyl acetate and 7-tetradecene. 27. A composition capable of disrupting the mating of the Western Pine Shoot Borer consisting essentially of 9-dodecenyl acetate having a cis to trans molar ratio of about 1/2. 28. A process for disrupting the Bating of the Western Pine Shoot Borer comprising applying to the infested area an effective amount of the composition of claim 27. 29. A composition capable of disrupting the mating of Heliothis, spp. consisting essentially of 9-tetradecenyl formate having a cis to trans molar ratio of about 1/2. 30. A process for disrupting the mating of pests selected from the group consisting of Heliothis, spp. comprising applying to the infested area an effective amount of the composition of claim 29. 31. A composition capable of disrupting the mating of Heliothis, spp. consisting essentially of 9-tetradecenyl formate having a cis to trans ratio of about 1/5. 32. A process for disrupting the mating of pests selected from the group consisting of Heliothis, spp. comprising applying to the infested area an effective amount of the composition of claim 31. 33. A composition capable of disrupting the mating of Heliothis, spp. consisting essentially of 9-tetradecenal having a cis to trans molar ratio of about 1/2. 34. A process for disrupting the mating of pests selected from the group consisting of Heliothis, spp. comprising applying to the infested area an effective amount of the composition of claim 33. 35. A composition capable of disrupting the mating of Heliothis, spp. consisting essentially of 9-hexadecenyl alcohol having a cis to trans molar ratio of about 1/2. 36. A process for disrupting the mating of pests selected from the group consisting of Heliothis, spp. comprising applying to the infested area an effective amount of the composition of claim 35. 37. A process for preparing 9-tetradecenyl formate by reacting 1-hexene or 5-decene with 9-decenyl acetate in accordance with the method of claim 1 to obtain 9-tetradecenyl acetate, then reacting the acetate with water to obtain the corresponding alcohol and then reacting the alcohol with formic acid to obtain the formate. 38. A process for preparing 9-hexadecenyl alcohol by reacting 1-octene or 7-tetradecene with 9-decenyl acetate in accordance with the method of claim 1 to obtain 9-hexadecenyl acetate and then reacting the acetate with water to obtain the corresponding alcohol. 39. A process for preparing 9-tetradecenyl alcohol by reacting 1-hexene or 5-decene with 9-decenyl acetate in accordance with the method of claim 1 to obtain tetradecenyl acetate and then reacting the acetate with water to obtain said alcohol. 40. A process for preparing 9-tetradecenal comprising preparing 9-tetradecenyl alcohol in accordance with claim 39 and oxidizing the alcohol to the aldehyde.

Claims: Claims 1. A process of preparing an internally unsaturated olefin having an oxygen containing functional group c h a r a c t e r i z e d b y reacting (1) a functional monoolefin having at least one terminal functional group selected from the formulas EMI48.1 wherein R is a hydrocarbyl group having 1 to 20 carbon atoms or in the case of the first formula hydrogen with (2) a hydrocarbyl monoolefin having at least three carbon atoms in the presence of a catalyst composition comprising (1) at least one neutral carbene complex having the formula EMI48.2 wherein R' is selected from alkyl or cycloalkyl radicals containing 1 to 10 carbons per radical and aryl or sub stituted aryl radicals containing 6 to 30 carbon atoms per radical wherein the substituted radicals can have one or more substituents, each of which can be the same or different and are selected from halides, alkoxides, and alkyl radicals containing 1 to 20 carbon atoms per radi cal; Y is S or O; R" is selected from alkyl, cycloalkyl, aryl, and substituted aryl radicals containing 1 to 30 carbon atoms per molecule, wherein the aryl substituents are as described for R' and wherein Y is S only one of R' and R" can be aryl or substituted aryl; each L is a neutral ligand individually selected from CO, NO, PR'3, PC131 PF3, and pyridine, where R' is as defined above, and L' is cyclopentadienyl; p is O or 1; and n is 5 when p is O or 2 when p is 1; and (2) a metal component selected from the chlorides and bromides of the metals of Groups IVa, IVb, Vb, VI6, VIIb, VIII, and Ib and the oxychlorides and oxybromides of molybdenum, tungsten, vanadium, and chromium, wherein if the metal is vanadium it is in an oxidation state of either 4 or its highest, stable, common, ionic oxidation state; if the metal is molybdenum, tungsten, or rhenium it is in an oxidation state of either 5 or its highest, stable, common, ionic oxidation state; and if the metal is not vanadium, molybdenum, tungsten or rhenium the metal is in its highest, stable, common, ionic, oxida tion state. 2. The process of claim 1 characterized in that said neutral carbene complex is selected from those wherein R' is selected from phenyl or an alkyl group having 1 to 10 carbon atoms; R" is an alkyl radical having 1 to 10 car bon atoms; Y is 0, L is CO, n is 5, and p is 0; in parti cular wherein said metal component of said catalyst com prises a mixture of SnCl4 and either SiC14 or Gel4; in particular wherein the olefinic hydrocarbyl portion of said functional monoolefin has the formula R"'-CH=CH(CH2)n wherein n is in the range of 2 to 10, and R"' is hyrdogen or an alkyl radical having 1 to 20 carbon atoms. 3. The process of claim 1 or 2 characterized in that said functional monoolefin is selected from 9-decenyl acetate, oleyl acetate, 1,18-diacetoxy-9-octadecene, 9-decenyl formate, 9-decenyl propionate, 5-pentenyl acetate, and methyl-I 0-undecenoate. 4. The process of claim 1 or 2, characterized in that said hydrocarbyl monoolefin is an alpha-olefin having no more than 20 carbon atoms; in particular wherein 9-tetrade cenyl acetate is produced by reacting 1-hexene and 9 decenyl acetate; in particular wherein 9-tetradecenyl acetate is produced by reacting a functional olefin con sisting essentially of trans-1,18-diacetoxy-9-octadecene with 1-hexene; in particular wherein 9-dodecenyl acetate is produced by reacting 1-butene and 9-decenyl acetate; in particular wherein 9-dodecenyl acetate is produced by reacting 1-butene and oleyl acetate; in particular wherein 9-tetradecenyl formate is produced by reacting 1-hexene and 9-decenyl formate; in particular wherein 9-tetradece nyl propionate is produced by reacting 9-dodecenylprop ionate and 1-hexene; in particular wherein 9-tridecenyl acetate is produced by reacting 9-decenyl acetate with 1-pentene; in particular wherein 9-hexadecenyl acetate is produced by reacting 9-decenyl acetate with 1-octene; in particular wherein 4-nonenyl acetate is produced by reacting 5-pentenyl acetate with 1-hexene; in particular wherein methyl-10-pentadecenoate is produced by reac ting methyl-10-undecenoate with 1-hexene. 5. The process according to any of claims 1 to 3 characterized in that said hydrocarbyl monoolefin is an internal olefin; in particular wherein said internal olefin comprises a symmetrical olefin; in particular wherein said functional monoolefin is selected from the group consisting of 9 decenyl acetate, oleyl acetate, 1,18-diacetoxy-9-octa decene, 9-decenyl formate, 9-decenyl propionate, 5-pen tenyl acetate, and methyl-lO-undecenoate; in particular wherein said internal olefin is selected from the group consisting of 5-aecene, 2-butene, 3-hexene, 4-octene, and 7-tetradecene; in particular wherein said internal olefin is 5-decene produced by the self-disproportiona tion of 1-hexene in the presence of the same catalyst specified for the reaction of the functional olefin; in particular wherein said functional olefin reactant con sists essentially of the trans isomer of 1,18-diacetoxy 9-octadecene; in particular wherein said functional ole fin is a symmetrical difunctional olefin consisting essentially of the trans isomer; in particular wherein 9-dodecenyl acetate is produced by reacting 9-decenyl acetate and 3-hexene; in particular wherein 9-tridecenyl acetate is produced by reacting 9-decenylacetate and trans-4-octene; in particular wherein 9-hexadecenyl ace tate is produced by reacting 9-decenyl acetate and 7 tetradecene. 6. The process of claim 1 or 2 for preparing 9-tetradecenyl formate characterized by reacting 1-hexene or 5-decene with 9-decenyl acetate to obtain 9-tetradecenyl acetate, then additionally reacting the acetate with water to ob tain the corresponding alcohol and then reacting the al cohol with formic acid to obtain the formate; in parti cular for preparing 9-hexadecenyl alcohol characterized by reacting 1-octene or 7-tetradecene with 9-decenyl acetate to obtain 9-hexadecenyl acetate and then addi tionally reacting the acetate with water to obtain the corresponding alcohol; in particular for preparing 9-tetradecenyl alcohol characterized by reacting 1-hexene or 5-decene with 9-decenyl acetate to obtain tetradecenyl acetate and then additionally reacting the acetate with water to obtain said alcohol; in particular for preparing 9-tetradecenal characterized by oxidizing said 9-tetra-. decenyl alcohol to the aldehyde. 7. A method for producing an internally unsaturated alpha ester characterized by hydrohalogenating an alpha, omega diene to obtain an omega-halo-alpha olefin, and then reacting the omega-halo-alpha olefin with a hydrocarbyl monoolefin in the presence of a disproportionation cata lyst to obtain an internally unsaturated compound having a terminal halide radical, and then converting the terminal halide radical to an ester radical; or first con verting the terminal halide of said omega-halo-alpha ole fin to an ester radical, and then reacting the resulting omega-ester-alpha-olefin with said hydrocarbyl monoolef in in the presence of said disproportionation catalyst to obtain said internally unsaturated alpha ester; in parti cular wherein said disproportionation is conducted in the presence of a catalyst composition comprising (methoxy phenylcarbene) pentacarbonyl tungsten (0), SnCl4 and SiCl4 and wherein HBr is used in the hydrohalogenation; in particular wherein 7-dodecenyl formate is produced from 1,7-octadiene; in particular wherein 9-tetradecenyl acetate is produced from 1,9-decadiene. 8. A composition suitable as insecticide characterized by con taining as active ingredient 9-dodecenyl acetate having a trans/cis ratio greater than 0.25/l; in particular wherein the trans/cis molar ratio is in the range of 1/1 to 3/1; in particular wherein the trans to cis molar ratio is about 2/1. 9. A composition suitable as insecticide characterized by containing as active ingredient an admixture of the cis and trans isomers of 9-tetradecenyl formate; in particular wherein the molar ratio of trans to cis is in the range of 6/1 to 1/1; in particular wherein the molar ratio of trans to cis is in the range of 5/1 to 2/1; in particular wherein the molar ratio of trans to cis is about 2/1. 10. A composition suitable as insecticide characterized by containing as. active ingredient an admixture of the cis and trans isomers of 9-tetra decenal or an admixture of the cis and trans isomers of 9-hexydecenyl alcohol; in particular wherein the trans to cis ratio is about 2/1. 11. A composition sgitable.as insecticide characterAzed by containing as active ingredient an admixture of the cis and transisomers of 9-tetra decenyl acetate; in particular wherein the molar ratio of trans to cis is in the range of 6/1 to 1/1; in particular wherein the molar ratio of trans to cis is about 5/1; in particular wherein the molar ratio of trans to cis is about 2/1. 12. The use of the composition of claim 8 for controlling the Western Pine Shoot Borer by disrupting the mating thereof. 13. The use of the composition of claim 9, 10 or 11 for con trolling Heliothis spp.by disrupting the mating thereof; in particular wherein said Heliothis species is Helio this zea or Heliothis virescens.

Inventors: BANASIAK, DENNIS STEPHEN
Applicants: PHILLIPS PETROLEUM COMPANY
Application year: 1983
Main classification: C07C69
IPC codes: C07C17, A01N35, A01N31, A01N37, C07C69