11937 results about "Boiling point" patented technology

A premium synthetic lubricant having antiwear properties comprises a synthetic isoparaffinic hydrocarbon base stock and an effective amount of at least one antiwear additive. The antiwear additive is preferably at least one of a metal phosphate, a metal dialkyldithiophosphate, a metal dithiophosphate a metal thiocarbamate, a metal dithiocarbamate, an ethoxylated amine dialkyldithiophosphate and an ethoxylated amine dithiobenzoate. Metal dialkyldithiophosphates are preferred, particularly zincdialkyldithiophosphate (ZDDP). The base stock is derived from a waxy, Fischer-Tropsch synthesized hydrocarbon feed fraction comprising hydrocarbons having an initial boiling point in the range of about 650-750 DEG F., by a process which comprises hydroisomerizing the feed and dewaxing the isomerate. The lubricant may also contain hydrocarbonaceous and synthetic base stock material in admxture with the Fischer-Tropsch derived base stock.

A lubricating base stock useful for forming lubricants such as a multigrade automotive oils, automatic transmission oils, greases and the like is prepared by hydroisomerizing a waxy hydrocarbon feed fraction having an initial boiling point in the 650-750 DEG F. range and an end point of at least 1050 DEG F., synthesized by a slurry Fischer-Tropsch hydrocarbon synthesis process. The hydroisomerization forms a hydroisomerate containing the desired base stock which is recovered, without dewaxing the hydroisomerate. The hydroisomerization is conducted at conditions effective to convert at least 67 wt. % of the 650-750 DEG F.+ waxy feed hydrocarbons to lower boiling hydrocarbons. When combined with a standard lubricant additive package, these base stocks have been formed into multigrade automotive crankcase oils, transmission oils and hydraulic oils meeting the specifications for these oils.

A method forms a hydrocarbon-containing polymer film on a semiconductor substrate by a capacitively-coupled plasma CVD apparatus. The method includes the steps of: vaporizing a hydrocarbon-containing liquid monomer (C_αH_βX_γ, wherein α and β are natural numbers of 5 or more; γ is an integer including zero; X is O, N or F) having a boiling point of about 20° C. to about 350° C.; introducing the vaporized gas into a CVD reaction chamber inside which a substrate is placed; and forming a hydrocarbon-containing polymer film on the substrate by plasma polymerization of the gas.

A method of forming a low-carbon silicon-containing film by CVD on a substrate having trenches includes: introducing a silicon-containing compound having three or less hydrocarbon units in its molecule and having a boiling temperature of 35° C. to 220° C.; applying RF power to the gas; and depositing a film on a substrate having trenches wherein the substrate is controlled at a temperature such that components of the silicon-containing compound are at least partially liquidified on the substrate, thereby filling the trenches with the film.

A substrate treatment method is provided, which includes: an organic solvent replacing step of supplying an organic solvent, whereby a liquid film of the organic solvent is formed on the substrate as covering the upper surface of the substrate to replace a rinse liquid with the organic solvent; a substrate temperature increasing step of allowing the temperature of the upper surface of the substrate to reach a first temperature level higher than the boiling point of the organic solvent after the formation of the organic solvent liquid film, whereby a vapor film of the organic solvent is formed below the entire organic solvent liquid film between the organic solvent liquid film and the substrate to levitate the organic solvent liquid film above the organic solvent vapor film; and an organic solvent removing step of removing the levitated organic solvent liquid film from above the upper surface of the substrate.

A method of forming a hydrocarbon-containing polymer film on a semiconductor substrate by a capacitively-coupled plasma CVD apparatus. The method includes the steps of: vaporizing a hydrocarbon-containing liquid monomer (C_αH_βX_γ, wherein α and β are natural numbers of 5 or more; γ is an integer including zero; X is O, N or F) having a boiling point of about 20° C. to about 350° C. which is not substituted by a vinyl group or an acetylene group; introducing the vaporized gas and CO₂ gas or H₂ gas into a CVD reaction chamber inside which a substrate is placed; and forming a hydrocarbon-containing polymer film on the substrate by plasma polymerization of the gas, thereby reducing extinction coefficient (k) at 193 nm and increasing mechanical hardness.

A multi-stage catalytic hydrogenation and hydroconversion process for heavy hydrocarbon feed materials such as coal, heavy petroleum fractions, and plastic waste materials. In the process, the feedstock is reacted in a first-stage, back-mixed catalytic reactor with a highly dispersed iron-based catalyst having a powder, gel or liquid form. The reactor effluent is pressure-reduced, vapors and light distillate fractions are removed overhead, and the heavier liquid fraction is fed to a second stage back-mixed catalytic reactor. The first and second stage catalytic reactors are operated at 700-850.degree. F. temperature, 1000-3500 psig hydrogen partial pressure and 20-80 lb./hr per ft.sup.3 reactor space velocity. The vapor and light distillates liquid fractions removed from both the first and second stage reactor effluent streams are combined and passed to an in-line, fixed-bed catalytic hydrotreater for heteroatom removal and for producing high quality naphtha and mid-distillate or a full-range distillate product. The remaining separator bottoms liquid fractions are distilled at successive atmospheric and vacuum pressures, low and intermediate-boiling hydrocarbon liquid products are withdrawn, and heavier distillate fractions are recycled and further upgraded to provide additional low-boiling hydrocarbon liquid products. This catalytic multistage hydrogenation process provides improved flexibility for hydroprocessing the various carbonaceous feedstocks and adjusting to desired product structures and for improved economy of operations.

A liquid raw material is heated to its boiling point or higher at a vaporizer to mix the vaporized ingredient gas and a carrier gas at a mixer at predetermined concentrations. The flow of the mixed gas is adjusted while the mixed gas is heated to over its condensing point and the temperature thereof is kept. Subsequently, the mixed gas is fed to a reactor for epitaxial growth while the mixed gas is heated to over its condensing point and the temperature thereof is kept. When the temperature of a heating medium is kept constant at the vaporizer to vaporize the liquid raw material and the feeding amount of the liquid into the vaporizer is adjusted by the pressure of the gas inside the vaporizer, the liquid surface level can be controlled to be constant.

A process for producing a blended fuel from a paraffin rich component and a cyclic rich component, where each of the components are generated from a renewable feedstock, is presented. The paraffin rich component is generated from a first renewable feedstock comprising at least one component selected from the group consisting of glycerides, free fatty acids, biomass, lignocellulose, free sugars, and combinations thereof. The cyclic rich component is generated from a second renewable feedstock comprising at least one component selected from the group consisting of glycerides, free fatty acids, free fatty alkyl esters, biomass, lignocellulose, free sugars, and combinations thereof. The blended fuel may a gasoline boiling point range blended fuel, a diesel boiling point range blended fuel, an aviation boiling point range blended fuel, any combination thereof, or any mixture thereof.

One or more materials selected from 1,1,1,3,3-pentachloropropane, 1,1,3,3-tetrachloropropene and 1,3,3,3-tetrachloropropene are used as the specific materials described above. Before submitting the materials and HF to a fluorination reaction, almost all water is removed from them.To continuously manufacture useful intended products efficiently as well as to prevent deactivation of the catalyst and the accumulation of organic substances with high boiling points when manufacturing said useful 1,1,1,3,3-pentafluoropropane and/or 1-chloro-3,3,3-trifluoropropene, by fluorinating the specific materials with HF in the presence of a catalyst.

Premium synthetic lubricants comprise a synthetic isoparaffinic hydrocarbon base stock and an effective amount of at least one, and typically a plurality of lubricant additives such as a detergent, dispersant, antioxidant, antiwear additive, pout point depresant, VI improver and the like. The base stock is derived from a waxy, paraffinic, Fischer-Tropsch synthesized hydrocarbon feed fraction having an initial boiling point in the range of about 650-750° F. and continuously boiling up to at least 1050° F., by a process which comprises hydroisomerizing the feed and dewaxing the isomerate. The waxy feed has a T90-T10 temperature difference of at least 350° F. and is preferably hydroisomerized without any pretreatment, other than optional fractionation. The lubricant may also contain hydrocarbonaceous and synthetic base stock material. Lubricants, such as fully formulated multigrade automotive crankcase and transmission oils formed by adding a suitable additive package to the isoparaffinic base stock have exhibited performance superior to similar fully formulated oils based on both PAO and conventional, petroleum derived base stocks.

A cryoablation system including a cannula having a proximal end, a distal end, and a longitudinal axis, an expandable balloon extending from the distal end of the cannula and fluidly connected to a source of heat transfer fluid by at least one fluid path, a pump for circulating the heat transfer fluid into and out of the balloon, a probe handle coupled to the proximal end of the cannula and in fluidic communication with the balloon through the cannula, and a heat exchanger for varying the temperature of the heat transfer fluid, wherein the heat exchanger is fluidly connected to a secondary refrigerant source. The heat exchanger may be positioned within the probe handle, within the cannula, or at least partially within the balloon. The heat transfer fluid of this cryoablation system preferably has a freezing point lower than about −110° C. and a boiling point greater than about 50° C.

A method is provided for manufacturing cleaner fuels, in which NPC (Natural Polar Compounds), naturally existing in small quantities within various petrolic hydrocarbon fractions, are removed from the petrolic hydrocarbon fractions ranging, in boiling point, from 110 to 560° C. and preferably from 200 to 400° C., in advance of catalytic hydroprocessing. The removal of NPC improves the efficiency of the catalytic process and produces environment-friendly products, such as diesel fuel with a sulfur content of 50 ppm (wt) or lower. Also, the NPC can be used to improve fuel lubricity.

A high VI and low pour point lubricant base stock is made by hydroisomerizing a high purity, waxy, paraffinic Fischer-Tropsch synthesized hydrocarbon fraction having an initial boiling point in the range of 650-750° F., followed by catalytically dewaxing the hydroisomerate using a dewaxing catalyst comprising a catalytic platinum component and an H-mordenite component. The hydrocarbon fraction is preferably synthesized by a slurry Fischer-Tropsch using a catalyst containing a catalytic cobalt component. This combination of the process, high purity, waxy paraffinic feed and the Pt/H-mordenite dewaxing catalyst, produce a relatively high yield of premium lubricant base stock.

Processes for the conversion of hydrocarbons boiling in the temperature range of from about 80° F. to about 1000° F. to diesel boiling range hydrocarbons, and processes for increasing the cetane number and amount of n-C₁₇ hydrocarbon products in such processes. Diesel boiling range hydrocarbons may be produced by contacting a hydrocarbon boiling in the above-mentioned boiling range with a triglyceride-containing compound to form a mixture, and then contacting the mixture with a hydrotreating catalyst under suitable reaction conditions.

A recording ink containing at least a solid component which contains a colorant and a resin and is a solid at 25° C., a liquid component which has a higher boiling point than that of water and is a liquid at 25° C. and water, wherein the total content of the liquid component in the recording ink is 20% by mass or less, the total content of the solid component in the recording ink is 20% by mass or more, and the total content of a resin component in the solid component is 40% by mass to 95% by mass relative to a total amount of the solid component is provided.

A reactive-separation process converts glycerin into lower alcohols, having boiling points less than 200° C., at high yields. Conversion of natural glycerin to propylene glycol through an acetol intermediate is achieved at temperatures from 150° to 250° C. at a pressure ranging from 1 and 25 bar. The preferred applications of the propylene glycol are as an antifreeze, deicing compound, or anti-icing compound. The preferred catalyst for this process in a copper-chromium powder.

A wide-cut lubricant base stock is made by hydroisomerizing and then catalytically dewaxing a waxy Fischer-Tropsch synthesized hydrocarbon fraction feed and comprises the entire dewaxate having an initial boiling point in the 650-75O° F.+ range. Formulated lubricating oils made by admixing the base stock with a commercial automotive additive package meet all specifications, including low temperature properties, for multigrade internal combustion engine crankcase oils. The waxy feed has an initial boiling point in the 650-750° F. range and continuously boils to an end point of at least 1050° F.+. Lower boiling hydrocarbons produced by the process are separated from the base stock by simple flash distillation. The base stock comprises the entire dewaxate having an initial boiling point in the 650-750° F. range.

A dynamic heat sink engine including a storage vessel having a working fluid outlet and a working fluid inlet. The lower portion of the storage vessel contains a cryogenic working fluid, such as liquid hydrogen, at a temperature at near its boiling point. The engine further includes a working fluid circuit extending between the working fluid outlet and the working fluid inlet of the storage vessel. The working fluid circuit includes the serial connection of the following components from the working fluid outlet to the working fluid inlet: a fluid pump; a vaporizer having a liquid line passing therethrough; a heater; an expansion engine having a rotary output shaft; an electrical generator connected to the rotary output shaft of the expansion engine; a vapor line passing through the vaporizer, the vaporizer including a heat exchanger providing thermal communication between the liquid line and the vapor line.