Showing papers on "Raffinate published in 1973"

Process for reduction of high sulfur residue

Abstract: A process for disposing of high sulfur-containing residual oil is disclosed wherein a high sulfur vacuum residual oil is hydrocracked and hydrodesulfurized in an upflow, high pressure, high temperature, ebullated bed reactor, the effluent fractionated, and the 975 DEG F. fraction further subjected to separation by solvent extraction. The extract consists of gas oils, while the raffinate, containing most of the remaining sulfur, is partially oxidized to yield hydrogen which is recycled to the hydrocracking reactor. The heavy gas oil fraction from the extract may also be recycled to extinction in the hydrocracker.

Lead free motor fuel production

Abstract: A two-stage reforming process for the production of high-octane unleaded motor fuel from low-octane naphthas. The paraffinic raffinate from an intermediate extractive distillation step is reformed over a steam-active catalyst. Several product streams produced during the various process steps are combined to produce a high-octane motor fuel.

Catalyst comprising ultrastable aluminosilicates and hydrocarbon conversion processes employing same

Abstract: The catalyst comprises the oxides of cobalt and molybdenum deposited on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline aluminosilicate material and a silica-alumina cracking catalyst. This catalyst may be used in a hydrocracking process or a combination process for converting petroleum hydrocarbons to gasoline blending stock having an unleaded research octane number greater than about 105. The hydrocracking process comprises contacting the catalyst in a hydrocracking reaction zone under hydrocracking conditions with a feedstock having an initial boiling point of at least 350° F. The combination process comprises treating the hydrocarbons in the hydrocracking process, selectively solvent-extracting the aromatics from the resultant hydrocracked product to obtain an aromatic extract and a non-aromatic raffinate, catalytically reforming the non-aromatic raffinate, and blending the resultant catalytic reformate with aromatic extract.

Process for the production of petroleum sulfonate

Abstract: Petroleum sulfonates useful to impart micellar characteristics to mixtures of hydrocarbon and aqueous medium are obtained by reacting a hydrocarbon gas oil feedstock (average molecular weight 250-700; A/AP aliphatic to aromatic proton) ratio 5-50 moles/mole, 30-100% of the feedstock molecules contain aromatic portions and the A/AP ratio of the aromatic portion being about 3-20 moles/mole) with a solution of EDC (ethylene dichloride) containing 0.1-0.3 lb. liquid SO 3 /lb EDC. The SO 3 concentration is about 0.1-0.3 lb. of SO 3 /lb of gas oil feedstock. Reaction takes place in a back-mix tubular reactor wherein at least about 4 parts of reaction products are recycled per 1 part of reaction products withdrawn and wherein the gas oil feedstock plus recycled reaction products and the SO 3 /EDC streams entering the reaction zone are in turbulent flow. Velocity ratio of the feedstock plus recycled reaction products stream to the SO 3 /EDC stream is at least 4:1, respectively. The withdrawn reaction products are neutralized with an aqueous basic liquid, e.g. aqueous solution, NH 4 OH and thereafter the EDC is recovered from the neutralized reaction products to obtain unextracted sulfonate mix. The unextracted sulfonate mix is extracted with an aqueous alcohol solution to obtain a raffinate phase, an extract phase, and a brine phase; the extract phase is withdrawn and stripped of alcohol and water to obtain the desired petroleum sulfonate.

Combination of extractive distillation and liquid extraction process for separation of a hydrocarbon feed mixture

Abstract: An extractive distillation zone is used in combination with a liquid phase extraction zone to provide relatively highly aromatic heavy and light extracts and a relatively aromatic-free raffinate stream. The process allows a feed mixture which contains raffinate materials in at least two fractions of aromatics to contact an extractive distillation zone in which solvent passed thereinto dissolves the heavy aromatics from the feed stock. The overhead vapors from the extractive distillation zone are condensed and passed into a liquid phase extraction zone where the light aromatic fraction of the feed stock is extracted and substantially separated from the non-aromatic raffinate components. The raffinate, light extract and heavy extract materials are separately recovered. The process is applicable to most hydrocarbon separations and in particular can be used in the petrochemical industry to separate close boiling aromatic and non-aromatic materials.

Oil treatment process

Abstract: A method of treating a mineral lubricating oil feedstock comprises contacting the mineral oil feed-stock counter-currently with furfural in a first extraction column and recovering from the first column a primary raffinate and a primary extract. The furfural is removed from the primary extract, which extract is then contacted counter-currently with more furfural in a second extraction column. A pseudo-raffinate and a secondary extract are recovered from the second column, the furfural being removed from the pseudoraffinate. The pseudo-raffinate is then treated with a solvent for wax to remove at least part of the wax and then is catalytically hydrogenated.

Solvent extraction of h{hd 3{b po{hd 4

Abstract: Purified phosphoric acid is obtained from phosphate rock by digesting the rock with sulfuric acid, separating the resulting dilute phosphoric acid liquor and solubilized impurities from the calcium sulfate precipitate, concentrating the liquor to at least about 50% P2O5, extracting the phosphorus values from the concentrated liquor with n-hexanol, n-heptanol, n-octanol, isooctanol, or a mixture thereof, and stripping the phosphoric acid values from the solvent liquor with water to recover purified phosphoric acid. The stripped solvent liquor is recycled to the extraction step. The amount of P2O5 values which are recovered from the impure liquor is substantially enhanced by employing at least two countercurrent extraction stages and at least three stripping stages, wherein about one-half of the raffinate from the first extraction stage is concentrated to match the P2O5 level of the aqueous stream from the last extraction stage and the two streams are admixed and fed to the immediately preceding extraction stage. The throughput rate of the system is significantly increased by maintaining the aqueous phase as the continuous phase in the last stripping stage, while the organic phase is maintained as the continuous phase in all the other extraction and stripping stages.

Process for the production of percarboxylic acid solutions in organic solvents

Abstract: There is provided a continuous process for the production of water free or substantially water free peralkanoic acids with 2 to 4 carbon atoms by reaction of aqueous hydrogen peroxide with an alkanoic acid having 2 to 4 carbon atoms in the presence of acidic catalyst at a mole ratio of hydrogen peroxide to alkanoic acid of 0.5 to 30:1, preferably from 0.8 to 20:1, in a reactor by countercurrent extraction of the reaction solution with an organic solvent, recovery of a substantially water free solution of peralkanoic acid as extract and in a given case, eventually after addition of an additional solvent, dehydration of the extract by azeotropic distillation, the entire aqueous raffinate or a portion thereof is led to an evaporator unit, in which the water brought in with the starting materials and formed during the reaction is distilled off under reduced pressure, whereupon the concentrated raffinate as well as in a given case the non-concentrated portion of the raffinate is returned to the reactor and the reactor is replenished with sufficient aqueous hydrogen peroxide and alkanoic acid that the starting conditions are again produced.

Method of recovering uranium

Abstract: Uranium values are obtained from phosphate rock by acidifying phosphate rock containing uranium values and at least one other heavy metal with a mineral acid so as to obtain a crude acid, solvent extracting the crude acid with an organic solvent so as to separate a raffinate from a relatively pure, wet process phosphoric acid and treating said raffinate with a base so as to raise the pH to 1-2 whereby uranium hydroxide or phosphate and other heavy metal hydroxides or phosphates are coprecipitated. The uranium content of the coprecipitate after drying is at least as high as 0.3% which is comparable to that of uranium ores of the highest quality.

Process for the production of petroleum resins of varying softening points

Abstract: A petroleum resin feedstock comprises a C5 stream distilled from a cracked petroleum fraction to which has been added butadiene raffinate which comprises isobutene, butenes-1 and -2 and butanes and which is what remains of a C4 fraction after removal of butadiene. The feedstock may be polymerised to a petroleum resin by means of a Friedel Crafts catalyst.

Purification of fluorocarbons

Abstract: A mixture of a fluorocarbon and a corresponding hydrocarbon is subjected to liquid-liquid solvent extraction. The extraction removes substantially all of the hydrocarbon and the fluorocarbon raffinate containing a small amount of hydrocarbon, such as on the order of 2 weight percent or less, is then distilled to obtain the fluorocarbon of at least about 99 weight percent purity.

Chemical composition of lubricating oils in relation to protective properties

Abstract: 1. Polar and protective properties have been studied for three oil fractions of Sosnino crude and for a distillate, raffinate, extract, and dewaxed oil from Zhirnovsk crude. It has been shown that the most polar products are those containing maximum amounts of medium and heavy aromatic hydrocarbons. 2. The polar oil products have better protective properties, owing to the formation of adsorbed films on the metal. The protection efficiency of these films is still inadequate, so that corrosion inhibitors must be added to the oils.

Distribution of additives used in process of raffinate dewaxing

Abstract: 1. Dielectric constants have been measured and relative polarities and dipole moments calculated for the additives AFK, V-167, and V-526. 2. The ranking of these additives with respect to surface activity and effectiveness in the dewaxing process is as follows: V-167< V-526

Solvent extraction of c --c aromatic hydrocarbons

Abstract: In a solvent extraction system utilizing a counter-current extraction column and an extractive distillation stripper for recovery of C6 --C8 aromatic hydrocarbons, the feed is divided into light and heavy fractions containing, respectively, C6 --C7 and C8 aromatics. The light fraction is introduced to the extraction column at an intermediate level along with the overhead stream from the stripper column, while the heavy fraction is introduced to the extraction column at a lower level. This procedure avoids loss of C8 aromatic components to the raffinate.