Abstract: A process for separating a solvent from a bituminous material by pressure reduction and steam stripping without carry-over of entrained bituminous material. A fluid-like phase comprising bituminous material and solvent is reduced in pressure by passage through a pressure reduction valve to vaporize a portion of the solvent. The reduction in pressure also results in dispersing a mist of fine bituminous material particles in the vaporized solvent. The stream of vaporized solvent, mist and fluid-like bituminous material then is introduced into a static mixer. The static mixer intimately mixes the mist with the fluid-like material and causes the mist to recombine with the fluid-like material from which it was formed. The resulting stream is introduced into a steam stripper to separate the solvent remaining in the bituminous material. The vaporized solvent and steam are withdrawn from the stripper substantially free of entrained bituminous material and condensed.

Abstract: An improvement to a continuous solvent extraction-steam-distillation process for the recovery of aromatic hydrocarbons in the range of C.sub.6 -C.sub.16 from a feed stream containing such aromatics and aliphatic hydrocarbons in the range of C.sub.5 -C.sub.16 which resides in using two extractive distillation zones thermally linked to recover heat and solvent, thereby resulting in a heat savings.

Abstract: A process for solvent extraction of oil from oil bearing diatomite ore and an apparatus for use therewith, wherein the ore is extracted by countercurrent decantation with a hydrocarbon solvent, solvent is recovered from the extract by multiple effect evaporation followed by stripping, and the spent diatomite is contacted with water to displace a major portion of the solvent therefrom, and solvent is recovered from the aqueous slurry of the spent diatomite by stripping with steam at superatmospheric pressure.

Abstract: A solvent recovery portion of a solvent refining plant for producing oil products such as lubricating oils from a crude source of hydrocarbons such as petroleum hydrocarbons wherein there are provided at least three continuous flash stages or zones for which each successive stage or zone operates at pressure and temperature levels higher than the preceding one, the vapor from any successive stage or zone being employed as the heating medium in the preceding one to effect the vaporization in said preceding stage or zone.

Abstract: Improvements in processes for stripping solvent from dewaxed oils and deoiled waxes; the use of an inert gas (such as nitrogen) as a stripping agent for removing solvent from dewaxed oils, deoiled waxes and slack waxes resultant from solvent dewaxing processes.

Abstract: A process for dehydrating an essentially one-phase wet solvent stream obtained in a solvent dewaxing-solvent deoiling process, which solvent stream contains at least 60% toluene with the balance being water and methyl ethyl ketone (hereinafter MEK), is dehydrated by (a) fractionally distilling to produce a bottom fraction of anhydrous MEK-toluene solvent and an overhead fraction containing all the water originally present in the wet solvent stream; (b) condensing and separating said overhead fraction into a toluene-containing, water-lean phase, which is used as reflux in step (a), and a toluene-free, MEK-containing, water-rich phase; (c) extracting into a hydrocarbon stream some MEK from said water-rich phase and from the condensed azeotropic mixture recycled from step (g) hereinafter; (d) recovering from step (c) a second water-rich stream, which water-rich stream contains the MEK not extracted into said hydrocarbon stream; (e) azeotropically distilling said second water-rich stream so as to obtain water as

Abstract: Petroleum fractions may be separated into aromatic rich and paraffinic-rich hydrocarbon streams by the use of methanol/water mixtures having at least 10% water by volume. The paraffinic-rich stream is recovered as raffinate and the aromatic-rich as extract. After the extraction step additional water is added to the extract and raffinate streams where it acts as an anti-solvent to effect separation of the hydrocarbon from the solvent. The water and methanol are then separated for example by flash distillation or by using super critical CO.sub.2 as an extraction solvent.

Abstract: Substantial energy savings are realized in an aromatic extraction process wherein a vapor sidestream is removed from the solvent stripper, compressed and used to provide the heat necesary for distillation in the solvent stripper.

Abstract: A fractionation process wherein a fractionation column is maintained at a subatmospheric pressure through the use of a steam-jet ejector. Water drawn off the overhead receiver of the fractionation column is vaporized by indirect heat exchange to form the moderate pressure steam charged to the ejector. The effluent of the ejector is passed through a condenser, and the resultant condensate is recycled to the overhead receiver by admixture with the overhead vapor stream of the fractionation column. The disposal of hydrocarbon-contaminated aqueous overhead liquid is thereby minimized.

Abstract: The thermal decomposition of N-methyl-2-pyrrolidone is minimized by the addition of minor amounts of water thereto prior to its being heated to temperatures in excess of 500.degree. F. This is of particular importance in processes using N-methyl-2-pyrrolidone as an extraction solvent to remove aromatics from mixtures of aromatic and non-aromatic hydrocarbons and wherein the N-methyl-2-pyrrolidone is recovered from the extracted fractions by thermal means such as flash evaporation and distillation.

Abstract: An asphalt containing mineral oil is simultaneously deasphalted and extracted in a combination zone by contacting the oil with a solvent comprising N-methyl-2-pyrrolidone (NMP) containing from 0-5 LV% water and a light hydrocarbon to produce a raffinate and extract phase, with the raffinate phase containing the desired oil, most of the hydrocarbon solvent and some NMP. The raffinate is then passed to a reduced pressure zone to remove most of the hydrocarbon solvent therefrom. The remaining raffinate oil and NMP solution is then chilled to produce bulk liquid-liquid immiscibility between the oil and NMP. The chilled oil and NMP are then passed to a settling zone wherein the NMP is separated from the oil and recycled back into the combination zone.

Abstract: Coal can be extracted with high boiling aromatic oils produced by extracting the aromatic constituents of a heavy petroleum material, e.g. a bitumen residue, using a selective solvent, mixing the extract with a low-boiling aromatic solvent, adding water and separating the aromatic-containing phase and recovering said aromatic constituents. The resulting coal extract is particularly suitable for the production of electrode coke.

Abstract: A solvent extraction process for separating polar hydrocarbons from non-polar hydrocarbons. The solvent-rich extract phase is introduced into a stripping column through two separated loci; the bottoms from the stripping column, a polar hydrocarbon-containing, solvent-rich stream, is introduced into an upper portion of the solvent recovery column. Polar hydrocarbons in concentrated form are recovered as an overhead stream, a lean solvent stream, virtually free from hydrocarbons, is withdrawn as a bottoms product and recycled in part to the extraction zone, and admixed in part with that portion of the extract phase introduced into the upper of the two separated loci. An internally prepared vaporous stripping medium is introduced into the lower portion of the solvent recovery column.

Abstract: Process for recovering highly pure aromatic substances from mixtures of hydrocarbons which contain in addition to the aromatic substances, large amounts of non-aromatic substances by liquid-liquid extraction in combination with an after arranged extractive distillation whereby the liquid-liquid extraction of the starting hydrocarbon mixture is carried out under such conditions that the resulting extract contains substantially the total amount of the aromatic substances and a portion of the non-aromatic substances, introducing this extract into an after arranged extractive distillation for further separating said extract whereby the sump product (extract phase) formed is drawn off and introduced into an after arranged distillation column where it is separated into an aromatic and a solvent fraction, while the head product of the extractive distillation (raffinate phase) is reintroduced into the bottom of the extractor for liquid-liquid extraction thereof, wherein there is used in both of the extracting stages,

Abstract: A solvent extraction process for separating polar hydrocarbons from non-polar hydrocarbons. The solvent-rich extract phase from the extraction zone is introduced into a stripping column. The stripper bottoms, being a polar hydrocarbon-containing, first solvent-rich stream, is introduced into an upper portion of a solvent recovery column. A vaporous stripping medium is introduced into a lower portion of the solvent recovery column. A second solvent-rich stream, virtually free from hydrocarbons, is withdrawn as a bottoms product and recycled to the extraction zone, while a hydrocarbon-containing, side-cut third solvent-rich phase is withdrawn, and a portion introduced into the stripping column in admixture with the extract phase. Of the total recovery column solvent-rich streams, the amount commingled with the fresh hydrocarbon feed and introduced therewith into the extraction zone, is from about 5.0% to about 25.0% of the total solvent introduced thereto.

Abstract: N-methyl-2-pyrrolidone is recovered from the raffinate and extract phases produced by its use in hydrocarbon extraction processes, particularly lube oil extraction, through the use of flash evaporation and/or distillation followed by gas stripping. Water buildup in the recovered solvent is prevented by employing solvent dehydration means in the solvent recovery line after gas stripping. Proper control of process parameters enables the dehydration means to remove excess water without requiring additional heat input to the process.

Abstract: A solvent extraction process for separating polar hydrocarbons from non-polar hydrocarbons. The solvent-rich extract phase is introduced into a stripping column, the bottoms from which, being a polar hydrocarbon-containing, solvent-rich stream, is introduced into an upper portion of a solvent recovery column. A first vaporous stripping medium is introduced into a lower portion of the solvent recovery column. A portion of the solvent-rich stream, virtually free from hydrocarbons, withdrawn as a bottoms product, is introduced into a solvent regeneration zone, the remainder being recycled to the extraction zone. A second vaporous stripping medium is introduced into the solvent regeneration zone, recovered with regenerated solvent and introduced into the solvent recovery column as at least a portion of the first vaporous stripping medium.

Abstract: A solvent extraction process for separating polar hydrocarbons from non-polar hydrocarbons. The solvent-rich extract phase from the extraction zone is introduced into a stripping column. The stripper bottoms, being a polar hydrocarbon-containing, solvent-rich stream, is introduced into an upper portion of a solvent recovery column. A first vaporous stripping medium is introduced into a lower portion of the solvent recovery column. A first solvent-rich stream, virtually free from hydrocarbons, is withdrawn as a bottoms product and recycled to the extraction zone, while a hydrocarbon-containing, side-cut second solvent-rich phase is withdrawn and introduced into the stripping column in admixture with the extract phase. At least a portion of one of the first and second solvent-rich streams is commingled with the fresh feed for introduction therewith into said extraction zone.

Abstract: A solvent extraction process for separating polar hydrocarbons from non-polar hydrocarbons. The solvent-rich extract phase is introduced into a stripping column, the bottoms from which, a polar hydrocarbon-containing, solvent-rich stream, is introduced into an upper portion of a solvent recovery column. A vaporous stripping medium is introduced into a lower portion of the solvent recovery column. Polar hydrocarbons in concentrated form are recovered as an overhead stream, a solvent-rich stream, virtually free from hydrocarbons, is withdrawn as a bottoms product and recycled to the extraction zone, while a hydrocarbon-containing side-cut solvent-rich phase is withdrawn and introduced into the stripping column with the extract phase.

Abstract: The energy requirements of a process for the solvent extraction of hydrocarbons from residua are reduced by nearly 50%, and capital requirements reduced substantially by evaporating solvent from extracted hydrocarbons in two or more pressure stages, the first stage evaporation occurring at a pressure sufficiently high to permit condensation of the solvent at a temperature sufficient to be combined with the solvent feed to the extractor at the required extraction temperature.

Abstract: A more economical method of removing materials adsorbed on solid adsorbents used to treat hydrocarbon streams is presented. The method comprises removing a liquid hydrocarbon stream from a distillation column, vaporizing the liquid stream and superheating the vapors which are formed, passing the superheated vapor through the adsorbent and effecting the removal of the adsorbed material, and then returning the vapor to the fractionation column and utilizing the vapor as stripping media within the column. In the preferred embodiment, water is removed from alumina.

Abstract: Petroleum fractions may be separated into aromatic-rich and paraffinic-rich hydrocarbon streams by the use of methanol/water mixtures having more than 20% water. The paraffinic-rich stream is recovered as raffinate. The aromatic-rich stream passes out of the extraction zone and is recovered by lowering the temperature to induce a phase separation.

Abstract: A continuous solvent extraction-steam distillation process for the recovery of aromatic hydrocarbons having boiling points in the range of about 80.degree.C. to about 175.degree.C. from a feedstock containing aliphatic hydrocarbons and said aromatic hydrocarbons comprising the following steps:A. introducing the feedstock into an extraction zone at about the midpoint thereof;B. introducing a mixture of water and solvent into the extraction zone at about the top of said extraction zone, said solvent being a water-miscible organic liquid having a boiling point of at least about 200.degree.C.;c. introducing reflux hydrocarbons into the extraction zone at about the bottom thereof;D. contacting the feedstock in the extraction zone with the mixture of water and a solvent, the water phase of step (j), and the reflux hydrocarbons to provide an extract comprising aromatic hydrocarbons, reflux aliphatic hydrocarbons, solvent, and water and a raffinate comprising essentially aliphatic hydrocarbons;E.

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.

Abstract: A hydrocarbon mixture consisting of an aromatic and a non-aromatic component is subjected to a liquid-liquid extraction and/or an extractive distillation. A solvent is used which selectively dissolves the aromatic component so as to form an extract phase. The extract phase is introduced into a distillation column for separating the solvent and the aromatic component. The column is provided with trays and the extract phase is introduced into the column at about the middle thereof from where the solvent flows downwardly and the aromatic component flows upwardly. Sufficient water is introduced into the sump of the column to insure that the trays above the location at which the extract phase enters the column are filled with water during the separation. This improves the operation of the distillation column. An arrangement for carrying out the above process is also disclosed.