A grease composition may contain a base oil (A) and a urea-based thickener (B). Particles containing the urea-based thickener (B) in the grease composition may satisfy requirement (I). The base oil (A) may be a mixed base oil containing a high-viscosity base oil (A1) having a kinematic viscosity at 40° C. of 250 mm.sup.2/s to 550 mm.sup.2/s, a low-viscosity base oil (A2) having a kinematic viscosity at 40° C. of 5.0 mm.sup.2/s to 110 mm.sup.2/s, and an ultra-high viscosity hydrocarbon-based synthetic oil (A3) having a number average molecular weight (Mn) of 2,500 to 4,500 and a kinematic viscosity at 40° C. of 25,000 mm.sup.2/s to 50,000 mm.sup.2/s. The base oil (A) may have a kinematic viscosity at 40° C. of 25 mm.sup.2/s to 105 mm.sup.2/s and a viscosity index of 120 or more. Both low-temperature characteristics and a lubricating life can be achieved.

Aspects of the present disclosure relate to a process for producing synthetic hydrocarbon base oils having advantageous properties for formulation of engine oils, and the base oils obtained by such processes, involving the production of branched alkenes from the oligomerization of C14-C18 olefins. According to one embodiment, the base oils are obtained by first forming a mixture of two or more olefins ranging from C14-C18, where one of the olefins is an alpha olefin and the other has an average double bond position between 1.5-5.0, and oligomerizing this mixture in the presence of a catalyst to form one or more branched alkenes, hydrogenating the branched alkenes, and fractionating to form base oils. According to one aspect, advantageous properties can be obtained by controlling one or more of the degree of branching, branch length, branching positions, selection of the C14-C18 olefins, and catalytic isomerization, during or after the oligomerization process.

Aspects of the present disclosure relate to a process for producing synthetic hydrocarbon base oils having advantageous properties for formulation of engine oils, and the base oils obtained by such processes, involving the production of branched alkenes from the oligomerization of C14-C18 olefins. According to one embodiment, the base oils are obtained by first forming a mixture of two or more olefins ranging from C14-C18, where one of the olefins is an alpha olefin and the other has an average double bond position between 1.5-5.0, and oligomerizing this mixture in the presence of a catalyst to form one or more branched alkenes, hydrogenating the branched alkenes, and fractionating to form base oils. According to one aspect, advantageous properties can be obtained by controlling one or more of the degree of branching, branch length, branching positions, selection of the C14-C18 olefins, and catalytic isomerization, during or after the oligomerization process.

Provided is a continuous process for converting waste plastic into recycle for polyethylene polymerization. In one embodiment, the process comprises selecting waste plastics containing polyethylene and/or polypropylene and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a crude unit distillation column in a refinery where a straight run naphtha (C.sub.5-C.sub.8) fraction or a propane/butane (C.sub.3-C.sub.4) fraction is recovered. The straight run naphtha fraction (C.sub.5-C.sub.8) or the propane/butane (C.sub.3-C.sub.4) fraction is passed to a steam cracker for ethylene production. The heavy fraction from the pyrolysis unit can also be passed to an isomerization dewaxing unit to produce a base oil.

Provided is a continuous process for converting waste plastic into recycle for polyethylene polymerization. In one embodiment, the process comprises selecting waste plastics containing polyethylene and/or polypropylene and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a crude unit distillation column in a refinery where a straight run naphtha (C.sub.5-C.sub.8) fraction or a propane/butane (C.sub.3-C.sub.4) fraction is recovered. The straight run naphtha fraction (C.sub.5-C.sub.8) or the propane/butane (C.sub.3-C.sub.4) fraction is passed to a steam cracker for ethylene production. The heavy fraction from the pyrolysis unit can also be passed to an isomerization dewaxing unit to produce a base oil.

An electrotechnical fluid composition, comprising more than 90 wt-% paraffins in the C17-C18 range, based on the total weight of the composition, is described. The ratio of the amount of C18 i-paraffins to the amount of C18 n-paraffins is more than 40, based on the weight of the C18 i-paraffins and the weight of the C18 n-paraffins in the composition.

A composition of a lubricant including a GTL hydrocarbon, fatty acid amine, and styrene block polymer.

A composition of a lubricant including a GTL hydrocarbon, fatty acid amine, and styrene block polymer.

A process for converting plastic feedstock into a lubricant on an industrial scale can include a reactor having a filter integrated therein to allow for separation and recovery of catalyst so it can be washed and reused in subsequent conversion processes. Such recycling of the catalyst can allow for an industrial scale conversion process.

The present disclosure relates to methods for producing renewable base oil and other valuable renewable fuel components from a feedstock of biological origin comprising free fatty acids and glycerides. The feedstock is first separated to two or more effluent streams containing a fatty acid fraction and glyceride fraction. The glycerides are hydrolyzed to free fatty acids and glycerol, and the fatty acids thus obtained are recycled to the separating. The fatty acids are then converted to the base oil by ketonisation, hydrodeoxygenation and hydroisomerisation. The glycerol is converted to propanols by selective hydrogenolysis.