Showing papers on "Raffinate published in 1974"

Recovery of fluorine, uranium and rare earth metal values from phosphoric acid by-product brine raffinate

Abstract: A method for recovering substantially all of the fluorine and uranium values and at least 90 percent of the rare earth metal values from brine raffinate obtained as by-product in the production of phosphoric acid by the hydrochloric acid decomposition of tricalcium phosphate minerals. A basically reacting compound is added to the brine raffinate to effect a pH of at least about 9, whereby fluorine, uranium and rare earth metal values are simultaneously precipitated therefrom. These values may then be separately recovered from the precipitate by known processes.

Recovery of copper and zinc from low-grade non-ferrous materials

Abstract: Copper and zinc are separately recovered in the form of substantially pure marketable products from low grade materials, such as metallic copper and brass scrap (e.g., junked automobile radiators) and oxidized residues (e.g., smelter flue dusts) which contain relatively large proportions of copper and zinc and relatively small proportions of other non-ferrous elements, by an improved ammoniacal leaching procedure. The low grade material is leached with an aqueous ammoniacal solution (ammonium sulfate or ammonium carbonate solution), dissolving the copper and zinc and leaving an insoluble residue. The copper-zinc solution is treated with a liquid ion exchanger to produce a raffinate containing a zinc ammonium complex in solution which is substantially completely free of copper. The liquid ion exchanger then is treated with an aqueous acid solution to form an eluant solution containing copper and substantially completely free of zinc and other metals. Substantially pure copper is recovered from the eluant solution; and the raffinate solution is treated to form a substantially pure zinc product. The copper and zinc depleted residual ammoniacal solution is recycled for re-use in the leaching operation.

Process for separating acrylic acid from aqueous solutions

Abstract: Acrylic acid is separated from aqueous solution by extraction of the solutions with organic solvents and separating the organic phase from the aqueous raffinate. Extraction is effected with a mixture of from 1 to 50 parts by weight of butanol and from 1 to 10 parts by weight of butyl acrylate.

Combination process for solvent deasphalting and catalytic upgrading of heavy petroleum stocks

Abstract: A raffinate product of residual oil solvent extraction is upgraded in a fluid zeolite catalyst cracking operation in the presence of one or more low molecular weight carbon-hydrogen fragment contributors. Gas oil products of atmospheric and vacuum distillation may be simultaneously converted by admixture with the raffinate charge. In addition the process is enhanced by the addition of straight run naphtha product of distillation with the raffinate charge.

Hydrocracking extraction process for lubes

Abstract: High quality UV stable lubricating oil stocks are prepared by hydrocracking a hydrocarbon feedstock under mild hydrocracking conditions to increase the viscosity index of the feedstock. The hydrocrackate product is subsequently solvent-extracted with a solvent having preferential solubility for aromatics, thereby forming extract and raffinate phases. The extract phase is stripped of solvent, and at least a portion of the substantially solvent-free extract phase is recycled to the hydrocracking step.

Lube extraction with NMP/phenol/water mixtures

Abstract: Lubricating oil stocks are upgraded by contacting same with a solvent comprising a mixture of n-methyl-2-pyrrolidone (NMP) and phenol. The solvent may also contain a minor amount of water. The phenol concentration in the solvent ranges between about 20 and 80 LV% based on the total amount of NMP, phenol and water in the solvent, while the water concentration in the solvent ranges between 0 and about 10 LV% based on the total amount of NMP, phenol and water in the solvent and preferably between about 1 and 4 LV%. At least a portion of the solvent is recovered from the thus-formed extract and raffinate phases by heating same to temperatures in the range of about 500° to 700° F., thereby flashing off the bulk of the solvent; remaining solvent may be stripped out from the extract and raffinate phases with an inert gas such as nitrogen, light hydrocarbons or hydrogen at superatmospheric pressures. The hot, stripped raffinate may be sent directly to a hydrofiner reactor, if desired, for further improvement of color, carbon residue, viscosity characteristics, sulfur removal, etc.

Process for the recovery of amides

Abstract: A solvent extraction-distillation process for the recovery of a water-soluble aliphatic amide having 1 to 8 carbon atoms or mixtures thereof from an aqueous solution wherein the concentration of the amide is in the range of about 0.25 percent by weight to about 25 percent by weight, based on the weight of the solution, and the solvent is a compound having the following structural formula: ##STR1## wherein M is OH or CH 2 OH, R is hydrogen or an alkyl radical, there being at least one alkyl radical, and the total number of carbon atoms in all of said alkyl radicals taken together is 3 to 12, or a mixture of isomers thereof, Said compound or mixture of isomers having a boiling point higher than the amide and less than about 350° C. and being non-azeotropic with the amide, Comprising the following steps: (a) contacting the solution in an extraction zone with the solvent to provide an extract comprising solvent, amide, and no more than about 5 percent by weight of water based on the weight of the solution and a raffinate comprising at least about 95 percent by weight of water based on the weight of the solution and less than about 5 percent by weight of solvent based on the weight of the solvent; (b) introducing the extract from step (a) into a distillation zone wherein the pressure is less than about 500 millimeters of mercury and the temperature is less than the decomposition temperatures of the amide and the solvent at said pressure, to separate the solvent from a mixture of amide and water; and (c) recovering the mixture of amide and water.

Process for the separation of ethylbenzene

Abstract: An adsorptive separation process for separating ethylbenzene from a feed mixture comprising ethylbenzene and at least one xylene isomer, which process comprises contacting the feed mixture with a crystalline aluminosilicate adsorbent containing calcium cations at the exchangeable cationic sites whereby there is obtained a fluid raffinate stream comprising ethylbenzene and a rich adsorbent containing said xylene isomer of the feed. A desorption step may then be used to desorb the adsorbed feed component. The process can be either in the liquid or vapor phase.

Method for making separations from aqueous solutions

Abstract: Method and apparatus for making separations from aqueous solutions, particularly for removing water from aqueous solutions of electrolytes or other substantially non-volatile solutes, such as saline water. According to the invention, a solvent extraction process is employed which produces streams of lower and higher solute concentration in composition from an aqueous solution by contacting the aqueous solution with a solvent to produce an extract stream and a residual raffinate stream, the solvent having the property of dissolving water at a first lower temperature and substantially releasing it at a second higher temperature without substantially extracting the solute from the aqueous solution. The extract stream is contacted with a hotter aqueous reflux and thereby simultaneously heated and caused to have its content of undesired solute diminished. In addition to the heat supplied by the reflux, heat is also added to the extract stream in a plurality of stages by condensing in the extract in each stage vapors obtained by flashing previously heated streams comprising mixtures of water and the solvent.

Edible oil solvent production

Abstract: An improved process for the solvent extraction of aromatics from a mixture thereof with non-aromatics. Increased aromatic recovery and solvent purity in the lean solvent recycle to the extraction zone is afforded. The resulting non-aromatic raffinate stream is reduced in the concentration of aromatic hydrocarbons, particularly those having more than eight carbon atoms per molecule, and is suitable for use as an edible oil solvent.

Process for producing uninhibited transformer oil

Abstract: A method for producing uninhibited transformer oil is disclosed which includes isolating a petroleum distillate that is primarily naphthenic and aromatic in character, boiling above 400°F, having a viscosity between 50 and 100 SSU at 100°F, and containing sulfur compounds; contacting the distillate with a solvent selective for aromatic hydrocarbons under conditions to produce a raffinate phase containing 15-30%v aromatic hydrocarbons; hydrotreating the raffinate phase to reduce the nitrogen content to at most 25 PPM, to maintain the sulfur content greater than 0.08%w, and to maintain the aromatic hydrocarbon content greater than 15%v. The product is an uninhibited transformer oil, and it can be further improved by regenerative clay treatment and by the addition of certain aromatic hydrocarbon compounds containing two or more six carbon membered fused or unfused rings, at least one of which is a benzene ring.

Removal of solvent

Abstract: Sulfolane is recovered from the extract and raffinate product streams of an extraction process employing sulfolane as the solvent by contacting the extract and raffinate product streams with a solid adsorbent and regenerating the adsorbent by displacing the adsorbed solvent with extraction process feed.

Solvent de-asphalting of heavy petroleum residues - at elevated temps in presence of water, giving improved sepn and easier processing

Abstract: Atmospheric or vacuum distn residues are treated with 4-8C paraffins in presence of >=2% water (based on vol of oil) at >=100 degrees C, and below the criticl bpt of the solvent, the water passing into the raffinate phase Extn is pref at 140-190 degrees C, wit a ratio of solvent to oil of 2-5:1 The water, with density between that of the extract and the asphaltene concentrate, displaces the solvent from the latter and increases the efficiency of the extn process Water-soluble salts are removed from the extract, and the viscosity of the asphaltene concentrate is reduced, together with its tendency to stick to the walls of the extn equipment