Abstract: This invention relates to a process for the removal of dissolved species from aqueous solutions, which comprises contacting said aqueous solution with an emulsion, said emulsion comprising an exterior phase which is characterized as being immiscible with said aqueous solution and yet permeable to said dissolved species, and an interior phase which contains a reactant capable of converting said dissolved species to a nonpermeable form. The dissolved species permeate the exterior phase, into the interior phase where they are converted into nonpermeable forms and thus retained in the interior phase of said emulsion. The aqueous solution, depleted in said dissolved species, is separated from said emulsion and the emulsion cycled for reuse. In one preferred embodiment said dissolved species are ions, and an ion exchange compound is incorporated in the exterior phase of the emulsion, to promote the permeation of said ions through the exterior phase.

Abstract: An improved dewaxing aid for solvent dewaxing process comprising a mixture of (A) an .alpha.-olefin polymer having an average molecular weight of from about 10,000 to 1,000,000 and a wide molecular weight distribution exceeding the range of from about 10,000 to 1,000,000 but falling within the range of from about 2,000 to 3,000,000 wherein the .alpha.-olefin polymer is a homopolymer made up of a C.sub.10 to C.sub.25 alpha-olefin monomer or is a copolymer made up of a monomer mixture comprising more than 50 wt. % of at least 2 C.sub.10 to C.sub.25 alpha-olefin monomers and a melt index greater than 1.8 g/10 min. and (B) an olefin vinyl acetate copolymer having a vinyl acetate content of from about 15 to 40 wt. % and an average molecular weight of from about 50,000 to 1,000,000 and a melt index greater than 2 g/10 min. The .alpha.

Abstract: In a solvent dewaxing process wherein a waxy hydrocarbon oil is mixed with a dewaxing aid and dewaxing solvent and chilled to form a slurry comprising solid particles of wax and a mixture of dewaxed oil and solvent, the improvement which comprises using a polymeric dewaxing aid comprising a condensation product of naphthalene and chlorinated wax having an average molecular weight ranging from about 20,000 to 500,000 and a molecular weight distribution exceeding the range of from about 10,000 to 1,000,000.

Abstract: It has been discovered that extraction processes which employ solvents to separate components from a feed stream and which solvents are themselves recovered by stripping from the thus produced extract or raffinate or both are improved in that the solvent is stripped from the extract, raffinate or both by the use of steam which has been previously distilled from a major portion of the process stream in one of the initial stages of the solvent recovery process, which steam rather than being vented or condensed for disposal is employed as a replacement for specifically generated fresh steam. This recycle steam is employed to strip any residual solvent from the extract, the raffinate or both. The steam and any residual solvent thus stripped is recycled from the extract stripper, raffinate stripper or both to the input feed of the solvent recovery train.

Abstract: In hydrocarbon oil dewaxing processes comprising passing the waxy oil through a staged vertical tower, injecting cold solvent at a plurality of stages along the vertical tower under conditions of high agitation to achieve substantially instantaneous mixing at each point, continuing the chilling, preferably at a rate of from 1.degree. to 8.degree. F. per minute, by means of cold solvent injection until a temperature at least 30.degree. F. above the filtering temperature but less than about 40.degree. to 45.degree. F. above the filtering temperature is reached and completing the cooling of the oil to the separation temperature in rotating element scraped surface chillers, the improvement comprising operating the scraped surface chillers at a chilling temperature range of at least 30.degree. F. while reducing the operating speed of the rotating elements in the scraped surface chiller to a speed of from 5 to 20% preferably 8 to 14% of the original design operation speed.

Abstract: A method is disclosed for the selective removal of basic nitrogen compounds (BNC) from natural and synthetic hydrocarbon feedstocks, preferably petroleum feedstocks, most preferably lube and transformer oils, which method comprises mixing the feedstock oil with a nonaqueous solution of anhydrous nonpolymeric Group IVb, Group Vb, Group VIb, Group VIIb, the non-noble (iron group) metals of Group VIII, copper, zinc, cadmium, and mercury halides (except TiCl.sub.4 or FeCl.sub.3) or tetrafluoroborates, complexed with non-aqueous polar solvents under conditions of agitation and mild heating whereby the basic nitrogen compounds exchange with the polar solvent to complex with the above-recited metal halides and metal tetrafluoroborates. The preferred halide is bromide, and the preferred polar solvent is methanol. The oil is then decanted to separate it from the metal halides: BNC complexes and the decantate washed with a polar solvent, which preferably includes water, and dried.

Abstract: Finely divided, high surface area, small crystallite (0.1 micron or less) di- and poly-transition metal chalcogenides are prepared by mixing in the absence of an aqueous solvent a transition metal salt with a source of chalcogen yielding a precipitate. The salt and the chalcogen source can be mixed either neat or in the presence of a nonaqueous solvent. The precipitate which results before removal of the anion salt is a finely divided product.

Abstract: A continuous autorefrigerant solvent dewaxing process is disclosed wherein a waxy oil is prediluted with a non-autorefrigerative solvent, such as ketone, preferably a mixture of MEK/MIBK, and then passed, at a temperature above its cloud point, to the top of a chilling zone, which is an autorefrigerant chilling zone operating on a continuous basis, and comprises a vertical, multi-staged tower, operating at constant pressure. In this chilling zone, wax is precipitated from the oil to form a waxy slurry and the so-formed slurry is further chilled down to the wax filtration temperature by stage-wise contact with liquid auto-refrigerating preferably propylene, which is injected into a plurality of said stages and evaporated therein so as to cool the waxy slurry at an average rate of between about 0.1.degree. to 20.degree. F. per minute with an average temperature drop across each stage of between about 2.degree. and 20.degree. F.

Abstract: In a solvent dewaxing process wherein a waxy hydrocarbon oil is mixed with a dewaxing aid and dewaxing solvent and chilled to form a slurry comprising solid particles of wax and a mixture of dewaxed oil and solvent, the improvement which comprises using a polymeric dewaxing aid comprising a condensation product of naphthalene and chlorinated wax having an average molecular weight ranging from about 20,000 to 500,000 and a molecular weight distribution exceeding the range of from about 10,000 to 1,000,000.

Abstract: Finely divided, small particle (0.1 micron or less) small crystallite (about 50 A.times.100 A or less) chalcogenides of manganese, rhenium and technetium are described. These compositions are prepared by mixing the absence of an aqueous solvent, a manganese, rhenium or technetium salt with a source of chalcogenide yielding a precipitate. The manganese, rhenium or technetium salt and the source of chalcogen can be mixed either neat or in the presence of a nonaqueous aprotic solvent. The precipitate which results before removal of the anion salt is a finely divided product. In the case of rhenium dichalcogenide the product possesses a layered structure. The anion salt may be removed by any technique common to the art, pumping under vacuum being one such technique, washing with a suitable solvent being another.A method is described for the preparation of di- and poly-chalcogenides of the formula MX.sub.

Abstract: Dichalcogenides of Group IVb, Vb, molybdenum and tungsten of two new forms have been discovered. The two new forms are the amorphous and layered-sheet configurations. In particular, the dichalcogenides of Group IVb, Ib, molybdenum and tungsten, i.e. Z(MX.sub.2).sub.n wherein M is the metal and X is the chalcogen, n is at least about 20,000 and Z is the number of such (MX.sub.2).sub.n sheets ranging from 1-10, can be described as possessing a "rag-like" structure representing a system consisting of single or several stacked but randomly folded and disordered layers or sheets having dimensions (as determined by TEM) corresponding to about 6.2 to 62 A in thickness, about 500 A minimum length by about 500 A minimum width. Broadly the rag-like (MX.sub.2).sub.n can be likened to a stack of polymer sheets wherein each sheet is one atom thick. These sheets of (MX.sub.2).sub.n are prepared by the controlled heating (in a flowing stream of H.sub.2 /H.sub.2 S) of amorphous MX.sub.

Abstract: A method is described for the preparation of chalcogenides of ruthenium, rhodium, osmium and iridium transition metals of the Periodic Table of the Elements which comprises mixing in the absence of an aqueous solvent a Group VIII transition metal salt with a source of chalcogenide, said chalcogenide being selected from the group consisting of sulfur, selenium, tellurium and mixtures thereof, yielding a precipitate of the formula MX.sub.y wherein M is selected from the group consisting of ruthenium, rhodium, osmium and iridium, X is sulfur, selenium, tellurium and mixtures thereof and y is a number ranging from about 0.1 to about 3, preferably 0.1 to about 2.5. By the practice of the nonaqueous synthesis technique, Group VIII chalcogenides are prepared which are finely divided, have a high surface area, small particle size and small crystallite size which are also free of excess sulfur, water and/or hydrolysis products. Layered stoichiometric osmium disulfide is prepared by this technique.

Abstract: A method is described for the preparation of chalcogenides of ruthenium, rhodium, osmium and iridium transition metals of the Periodic Table of the Elements which comprises mixing in the absence of an aqueous solvent a Group VIII transition metal salt with a source of chalcogenide, said chalcogenide being selected from the group consisting of sulfur, selenium, tellurium and mixtures thereof, yielding a precipitate of the formula MX.sub.y wherein M is selected from the group consisting of ruthenium, rhodium, osmium and iridium, X is sulfur, selenium, tellurium and mixtures thereof and y is a number ranging from about 0.1 to about 3, preferably 0.1 to about 2.5. By the practice of the nonaqueous synthesis technique, Group VIII chalcogenides are prepared which are finely divided, have a high surface area, small particle size and small crystallite size which are also free of excess sulfur, water and/or hydrolysis products.

Abstract: A method is described for the preparation of high surface area metal fluorides and metal oxyfluorides comprising reacting high surface area metal oxides with a fluorocarbon vapor wherein the fluorocarbon is selected from the group consisting of CH.sub.4-Q F.sub.Q wherein Q is 1 to 3 and totally or partially fluorinated C.sub.2 -C.sub.6 alkanes, alkenes and alkynes and C.sub.5 -C.sub.6 cyclic alkanes, preferably fluoroform (CHF.sub.3) wherein the metal oxides and the fluorocarbon vapors are contacted at a temperature of from about 300.degree. to about 800.degree. C., for a time sufficient to effect the essentially complete conversion of the metal oxides into metal fluorides or the partial conversion of the metal oxides into metal oxyfluorides.

Abstract: Higher molecular weight hydrocarbons of from C.sub.2 to C.sub.7 carbon number are prepared from CO and H.sub.2 by the method of passing the CO and H.sub.2 at a ratio of from 10-0.1, a space velocity of from 100 hr.sup.-1 to 50,000 hr.sup.-1 over a bulk nickel catalyst promoted with from 0.001 to 25 wt. % titanium containing oxide (calculated as TiO.sub.2), for a time sufficient to effect the generation of the desired hydrocarbon products, at a temperature of from 100.degree. to 500.degree. C. and a pressure of from 103 to 1.03.times.10.sup.5 kPa. The hydrocarbon products obtained are clean, stable paraffin liquids. The activity of the instant process employing titanium promoted bulk nickel is from 3 to 5 times that of the process employing bulk nickel.

Abstract: Olefins and aromatic compounds in mixed hydrocarbon streams boiling above about 200.degree. F. are hydrogenated at a temperature ranging between about 400.degree. F.-720.degree. F. using a zeolite-containing catalyst that has been treated with a hydrocarbon stream relatively high in organic nitrogen compounds to suppress the cracking activity of the catalyst. The catalyst comprises (1) an amorphous base component, (2) a crystalline aluminosilicate component preferably comprising 5-30 wt. % of the total catalyst and having a silica/alumina mole ratio of at least 2.5 and an alkali metal content of less than about 2.0 wt. %, and (3) a transition metal hydrogenation component. The process is particularly useful in the manufacture of jet fuels and technical white oils and white oil bases with a minimum conversion of feed (<20%) to substantially lower boiling products.

Abstract: It has been discovered and forms the basis of the disclosure that various acid catalyzed hydrocarbon conversion processes such as catalytic cracking of gas oil; xylene isomerization; toluene disproportionation; dealkylation of aromatics; ethylene, butylene, isobutylene, propylene polymerization; olefin isomerization; alcohol dehydration; olefin hydration; alkylation; heavy ends cat cracking, etc. are dramatically improved insofar as percent conversion, and selectivity are concerned by the use of a catalyst selected from the group consisting of the oxides of tungsten, niobium and mixtures thereof, and tungsten or niobium oxides in combination with one or more additional metal oxides selected from the group consisting of tantalum oxide, hafnium oxide, chromium oxide, titanium oxide and zirconium oxide, supported on an inorganic refractory oxide support. These catalysts may be prepared by the methods known in the art, i.e., incipient wetness, impregnation, coprecipitation, etc.

Abstract: Novel heterogeneous silylhydrocarbyl phosphine transition metal complex catalysts and intermediates therefor are prepared by (a) the selective monoaddition of silane having chlorine, alkoxy or acyloxy groups to an .alpha., .omega.-diene, (b) followed by the addition of a phosphine to the resulting .omega.-alkenyl silanes to form the corresponding silylalkyl phosphines, (c) which are then covalently anchored as such or in the form of their transition metal complexes via condensation of their reactive silane substituents with hydroxy groups of silica and metal oxides, (d) optionally followed by complexing the free phosphine groups of anchored silylalkyl phosphines with transition metal compounds.

Abstract: New heteronuclear noble metal cluster complexes have been discovered and synthesized for the first time. These complexes are (pyridine).sub.2 Pt[Ir.sub.6 (CO).sub.15 ], (pyridine).sub.2 --Pt[Ir.sub.2 (CO).sub.7 ], (pyridine).sub.3 Pt[Ru.sub.3 (CO).sub.12 ], ((C.sub.6 H.sub.5).sub.3 P).sub.2 --Pt[Ir(CO).sub.3 P(C.sub.6 H.sub.5).sub.3 ].sub.2, ((C.sub.6 H.sub.5).sub.3 P).sub.2 Rh(CO)[Ir(CO).sub.4 ], and (pyridine).sub.2 Pt[Rh(CO).sub.2 (P(C.sub.6 H.sub.5).sub.3).sub.2 ].sub.2.These new heteronuclear noble metal cluster complexes are useful as supported mixed noble metal catalyst precursors. These new cluster complexes, of known stoichiometry, are deposited on anhydrous refractory inorganic oxide or carbon supports and then reduced resulting in the formation of a supported heteronuclear noble metal catalyst having the same metals stoichiometry as the starting cluster complexes.

Abstract: An improved process for removing H.sub.2 S from a hydrofiner tail gas wherein said tail gas is passed into a scrubbing zone wherein it is contacted with liquid NMP to remove most of the H.sub.2 S from the gas to form an H.sub.2 S-rich NMP solution and the H.sub.2 S-rich NMP solution is heated and passed into a stripping zone to remove most of the H.sub.2 S from the NMP to form an H.sub.2 S-lean NMP solution, extracting a hydrocarbon oil with an NMP solution, recovering hot liquid, NMP from said extracted oil and combining it with said H.sub.2 S-lean NMP solution and wherein said combined solution comprises at least a portion of said NMP solution used to extract said oil, wherein the improvement comprises heating the H.sub.2 S-rich NMP solution to the required stripping temperature by indirectly contacting same, in heat exchange relationship, with at least a portion of said combined NMP solution.This process is especially useful for scrubbing H.sub.