Abstract: Barbed wire repair apparatuses including (a) two members, each of the two members includes a barbed wire attachment or receiving apertures and an engaging surface having connection slot and (b) a connection device so that as connection devices insert into and through the connection slots and tightened to bring the engaging surfaces into contact and simultaneously tensioning the barbed wire at a break therein and methods for making and using same.

Abstract: An umbrella clamping system for clamping an umbrella to a chair includes an umbrella having a canopy, selectively movable between an extended configuration and a collapsed configuration, and a vertical shaft supports the canopy and has a base attachment member at a bottom end thereof. A clamp assembly securely receives the umbrella base attachment member and is configured for attachment to an external horizontal structural element. The clamp assembly includes a body, an upper clamp affixed to an upper end of the body for receiving the umbrella base attachment member and is selectively adjustable between an opened release position and a closed gripping position. A lower clamp is affixed to a bottom end of the body and has opposed first and second jaws defining a horizontally oriented gripping opening therebetween and adjustable one with respect to the other for attachment to the external horizontal structural element.

Abstract: A wedge-shaped member to restrain coil windings of a generator rotor from moving under centrifugal force. The wedge-shaped, substantially hollow member including a first plate, a second plate positioned opposite the first plate and positioned at an angle relative to the first plate, and one or more reinforcing members coupled between the first plate and the second plate. The wedge-shaped member is configured to fit between the core poles of a generator. A plurality of holes in the first and/or second plates permit a bonding material to adhere to adjacent coil windings and spread through the holes.

Abstract: A rotor for a high speed generator is constructed of a plurality of laminations and interlamination disks, which are disposed between each of the laminations. A coil support assembly is disposed within each of the rotor interpole regions and is secured to the interlamination disks.

Abstract: A process for the recovery of substantially pure alkyl alkanoate, such as ethyl acetate, from an impure feedstock. The impure feedstock is contacted with a selective hydrogenation catalyst in the presence of hydrogen in a selective hydrogenation zone maintained under selective hydrogenation conditions effective for selective hydrogenation of impurities containing reactive carbonyl groups thereby to hydrogenate the impurities to the corresponding alcohols. After recovery from the selective hydrogenation zone of a selectively hydrogenated reaction product mixture including the alkyl alkanoate and the corresponding alcohols, this is distilled in one or more distillation zones so as to produce substantially pure alkyl alkanoate therefrom which is recovered.

Abstract: Aliphatic aldehydes are hydrogenated to alcohols containing by product ester which ester is removed and separately hydrogenated to provide additional product.

Abstract: A process is described for the production of substantially pure gamma-butyrolactone from a feed mixture containing a major amount of gamma-butyrolactone and a minor amount of diethyl succinate which comprises fractionally distilling the mixture in a fractionation zone in the presence of added diethyl maleate and recovering from the fractionation zone an overhead vaporous product comprising gamma-butyrolactone which is substantially free from diethyl succinate and a liquid bottom product comprising diethyl maleate and diethyl succinate in admixture one with another. This procedure can be used to separate a gamma-butyrolactone rich fraction obtained by distillation in one or more stages of a crude reaction product obtained by hydrogenation of a C.sub.

Abstract: A continuous process is described for the production of a substantially acid free dialkyl maleate, for example diethyl maleate, from a feed stream containing a major amount of dialkyl maleate and a minor amount of the corresponding monoalkyl maleate. This comprises continuously distilling the feed stream in a primary distillation zone, which can comprise a single distillation column or a series of distillation columns connected in series, so as to give (i) a bottom fraction containing monoalkyl maleate and dialkyl maleate in admixture, (ii) a vaporous fraction comprising alkanol, and (iii) an intermediate fraction that is substantially free from alkanol and comprises a major proportion of diethyl maleate and a minor proportion of maleic anhydride. The intermediate fraction (iii) is redistilled in a secondary distillation zone to yield (i) an overhead fraction containing maleic anhydride and (ii) a bottom fraction containing substantially acid free dialkyl maleate.

Abstract: Butane-1,4-diol is produced by vapor phase hydrogenolysis of an alkyl ester of a C.sub.4 dicarboxylic acid, e.g. diethyl maleate, over a reduced Cu-Cr or Cu-Zn mixed oxide catalyst. Two adiabatic hydrogenolysis zones are used. The mixture exiting the first of these zones is cooled (by, for example, 5.degree. C.) and the resulting cooled mixture is fed to the second zone in which is reequilibriates at a lower temperature to increase the butane-1,4-diol yield at the expense of gamma-butyrolactone. Typical reaction conditions include use of temperatures of 150.degree. C. to 200.degree. C., pressures of 25 to 70 bar, and a H.sub.2 :ester molar ratio of 100:1 to 800:1. When using a maleate ester it is often advantageous to hydrogenate this to the corresponding succinate ester in an upstream hydrogenation zone prior to entry to the first hyrogenolysis zone.

Abstract: Butane-1,4-diol is produced by converting allyl alcohol to an allyl t-alkyl or -cycloalkyl ether of the general formula: ##STR1## wherein R.sub.1 and R.sub.2 each, independently of the other, represent a C.sub.1 to C.sub.4 alkyl radical, and R.sub.3 and R.sub.4 each, independently of the other, represent a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, or wherein R.sub.1 represents a C.sub.1 to C.sub.4 alkyl radical, R.sub.2 and R.sub.3 together with the carbon atoms to which they are attached form a 5-membered or 6-membered cycloaliphatic ring, and R.sub.4 represents a hydrogen atom or a C.sub.1 to C.sub.

Abstract: Aldehyde ethers of the general formula ##STR1## wherein R.sub.1 and R.sub.2 each, independently of the other, represent a C.sub.1 to C.sub.4 alkyl radical, and R.sub.3 and R.sub.4 each, independently of the other, represent a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, or wherein R.sub.1 represents a C.sub.1 to C.sub.4 alkyl radical, R.sub.2 and R.sub.3 together with the carbon atoms to which they are attached form a 5-membered or 6-membered cycloaliphatic ring, and R.sub.4 represents a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, and wherein Y represents --CH.sub.2 --CH.sub.2 --CH.sub.2 or --CH.sub.2 --CH (CH.sub.3)--, are prepared by hydroformylation of a corresponding compound of formula. ##STR2## by reaction with hydrogen and carbon monoxide in the presence of a hydroformylation catalyst, e.g. a rhodium complex catalyst. Preferred compounds include 4-t-butoxybutyraldehyde and 3-t-butoxy-2-methylpropionaldehyde.

Abstract: A process is disclosed for producing a substantially sulphur-free, butene-1 rich stream from a butene-containing C.sub.4 hydrocarbon feed stream by passage through a desulphurization zone, e.g. successive beds of active alumina and zinc oxide, and then distilling it. The desulphurization zone adsorbs, absorbs or converts to higher boiling sulphurous compounds low boiling sulphurous impurities such as H.sub.2 S, COS and CH.sub.3 SH. A sulphur-free butene-1 rich stream is recovered overhead from the distillation zone, while a butene-2 rich stream containing higher boiling sulphurous impurities originally present or produced in the desulphurization zone is recovered as a bottom product. A dechlorination zone (containing, for example, a charge of copper impregnated active carbon) can be provided upstream or downstream from the desulphurization zone but upstream from the distillation zone or can be provided in the path of the butene-1 rich stream from the distillation zone.

Abstract: Aldehyde ethers of the general formula ##STR1## wherein R.sub.1 and R.sub.2 each, independently of the other, represent a C.sub.1 to C.sub.4 alkyl radical, and R.sub.3 and R.sub.4 each, independently of the other, represent a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, or wherein R.sub.1 represents a C.sub.1 to C.sub.4 alkyl radical, R.sub.2 and R.sub.3 together with the carbon atoms to which they are attached form a 5-membered or 6-membered cycloaliphatic ring, and R.sub.4 represents a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, and wherein Y represents --CH.sub.2 --CH.sub.2 --C.sub.2 or --CH.sub.2 --CH (CH.sub.3)--, are prepared by hydroformylation of a corresponding compound of formula: ##STR2## by reaction with hydrogen and carbon monoxide in the presence of a hydroformylation catalyst, e.g. a rhodium complex catalyst. Preferred compounds include 4-t-butoxybutyraldehyde and 3-t-butoxy-2-methylpropionaldehyde.

Abstract: A rhodium-catalyzed hydroformylation process in disclosed in which an overhead vapor stream is recovered from the hydroformylation zone containing reactant alkene, hydrogen, carbon monoxide, alkene hydrogenation product(s), aldehyde product and aldehyde condensation products. This vapor stream is subjected to condensation conditions in one or two stages to condense therefrom condensible components comprising unreacted alkene, aldehyde product, and aldehyde condensation products. Non-condensed components of the vapor stream (e.g. H.sub.2 and CO) are recycled to the hydroformylation zone. Unreacted alkene is also recycled in liquid form to the hydroformylation zone.

Abstract: n-Valeraldehyde is produced by hydroformylation of butene-1 in the presence of one or more of cis- and trans-butene-2 and iso-butylene using a rhodium complex catalyst such as HRh(CO)PPh.sub.3).sub.3. Reaction conditions include use of at least about 100 moles of free triorganophosphine per gram atom of rhodium, a temperature of about 80.degree. C. to about 130.degree. C., a total pressure of not more than about 50 kg/cm.sup.2 absolute, a partial pressure of carbon monoxide of not more than about 1.5 kg/cm.sup.2 absolute, and a partial pressure of hydrogen of from about 1.0 to about 7.5 kg/cm.sup.2 absolute. An n-/iso-ratio of 20:1 and a conversion efficiency of butene-1 to n-valeraldehyde of over 85% are possible under these conditions with essentially no resin formation despite the presence of iso-butylene. The n-/iso-valeraldehyde mixture can be aldolized and reduced without intermediate purification to give a commercially acceptable C.sub.10 -plasticizer alcohol.

Abstract: Tetrahydrofuran is produced by converting allyl alcohol to an allyl t-alkyl or -cycloalkyl ether of the general formula: ##STR1## wherein R.sub.1 and R.sub.2 each, independently of the other, represent a C.sub.1 to C.sub.4 alkyl radical, and R.sub.3 and R.sub.4 each, independently of the other, represent a hydrogen atom or a C.sub.1 to C.sub.3 alkyl radical, or wherein R.sub.1 represents a C.sub.1 to C.sub.4 alkyl radical, R.sub.2 and R.sub.3 together with the carbon atoms to which they are attached form a 5-membered or 6-membered cycloaliphatic ring, and R.sub.4 represents a hydrogen atom or a C.sub.1 to C.sub.

Abstract: A hydroformylation process is disclosed utilizing a rhodium complex catalyst and an excess of a triorganophosphine wherein active rhodium catalyst and triorganophosphine can be separated from inactive rhodium, "heavies" and triorganophosphine oxide in partially deactivated reaction medium by extraction into concentrated phosphoric acid or aqueous solutions containing at least 40% by weight phosphoric acid. By neutralization of the phosphoric acid extract in the presence of organic solvent, e.g. aldehyde trimers, a solution of active rhodium catalyst and triorganophosphine can be produced that is suitable for re-use in the hydroformylation reaction.

Abstract: Alkanes are catalytically oxidized in the absence of ammonia by passing a feed gas including the alkane and oxygen at an elevated temperature over a solid catalyst. The partial pressure of the alkane in the feed gas exceeds 0.70 atmospheres absolute. Examples of the catalytic oxidation are the production of acrolein and methacrolein and acrylic acid and methacrylic acid from propane and iso-butane.

Abstract: A process is described for the production of methane from methanol by catalytic dehydration and dehydrogenation providing a high initial methane yield and a final substitute natural gas product of high calorific value. The catalytic dehydration and dehydrogenation steps may be effected simultaneously or in sequence. High efficiency in usage of raw materials and thermal requirements of the process are secured. A preferred catalyst containing both dehydration and dehydrogenation functions consists essentially of a major amount of iron oxide and minor amounts of chromium oxide and phosphate or tungstate ions.

Abstract: A process is provided for the catalytic production of methane from carbon oxides and hydrogen wherein water is introduced into the reaction vessel for the removal of the heat of reaction by the production of steam with the use of a catalyst effective at a temperature below 500.degree.F. The catalyst is a Group 8 metal, preferably mixtures of nickel and metals of the platinum group. Feedstock gas is normally obtained by gasification of fossil fuels or aliphatic alcohols with steam and/or oxygen.