Showing papers on "Raffinate published in 1972"

Process of comprising solvent extraction of a blended oil

Abstract: A petroleum oil of improved stability (e.g., as an electrical insulation medium), can be prepared by a process comprising blending 25-98 parts (preferably 50-95) of a severely hydrorefined oil (preferably, a hydrorefined naphthenic or mildly aromatic oil having a VGC from 0.820-0.940, a viscosity from 30 to 200 SUS at 100*F. and an ultraviolet absorptivity (UVA) of less than 0.04 in the 335 millimicron region (i.e., 335 UVA)) with from 75-2 parts (preferably 50-5) by weight of unhydrogenated naphthenic distillate (which preferably is free of naphthenic acids, and more preferred, has a pour point less than 0*F.), and then extracting the blend with an aromatic selective solvent (e.g., furfural, phenol) to obtain a raffinate oil product. The raffinate can be finished, as by adsorbent contact with attapulgite, acid activated clay or mixtures of such adsorbents. From 0.1-30 weight percent of a cycle oil can be added to the blend before extraction or to the raffinate oil product.

Multi-stage process for producing high ur oil by hydrogenation

Abstract: REFINED MINERAL OILS (USEFUL AS TEXTILE OILS, WHITE OILS AND AGRICULTURAL SPRAY OILS) WHICH HAVE A VISCOSITY IN THE LUBRICATING OIL RANGE AND A VOLUME PRECENT UNSULFONATED RESIDUE (UR) OF AT LEAST 94.5 8TYPICALLY AT LEAST 96) ARE PRODUCED FROM A DEWAXED RAFFINATE OF A DISTILLATE OIL, PREFERABLY A SUBSTANTIALLLY WAX-FREE DISTILLATE, OBTAINED FROM A CRUDE OIL CLASSIFIED AS PARAFFINIC OR MIXED-BASE BY ASTM VISCOSITY-GRAVITY CONSTANT (VGC). ONE PREFERRED DISTILLATE IS A DE-WAXED RAFFINATE HAVING A UR LESS THAN 93. A PREFFERED PROCESS OFR PRODUCING SUCH A REFINED MINERAL OIL (WITH A UR OF AT LEAST 96) COMPRISES (A) INTRODUCING A MINERAL OIL DISTILLATE OF LUBRICATING VISCOSITY INTO A REACTION VESSEL CONTAINING A FIRST REACTION ZONE, A SECOND REACTION ZONE AND AN INTERMEDIATE ZONE BETWEEN SAID FIRST AND SAID SECOND REACTION ZONES; (B) CONTACTING SAID DISTILLATE IN SAID FIRST ZONE WITH A HYDROCARBON-RICH GAS AND A CATALYTIC AMOUNT OF A SULFUR-RESISTANT HYDROGENATION CATALYST TO DESULFURIZE SAID DISTILLATE; (C) PASSING THE DISTILLATE FROM SAID FIRST ZONE TO SAID INTERMEDIATE ZONE CONTAINING THEREIN A PACKING MATERIAL WHICH IS SUBSTANTIALLY INERT TO HYDROGENATION AND WHEREIN THE FLOW OF HYDROGEN IS COUNTERCURRENT TO THE FLOW OF DISTILLATE WHEREBY HYDROGEN SULFIDE WHICH WAS FORMED IN SAID FIRST ZONE IS STRIPPED FROM SAID DISTILLATE; (D) CONTACTING THE DESULFURIZED DISTILLATE IN SAID SECOND ZONE WITH HYDROGEN AND A HYDROGENATION CATALYST; (E) SAID CONDUCTED AT A TEMPERATURE OF SAID SE AID SECOND ZONES BEING CONDUCTED AT A TEMPERATURE OF ABOUT 550 TO 750* F. AND A PRESSURE IN THE RANGE OF 5006000 P.S.I.G.; AND (F) WITHDRAWING MINERAL OIL PRODUCT FROM SAID SECOND ZONE HAVING AN UNSULFONATABLE RESIDUE OF AT LEAST 96.

Liquid ion exchange process for the recovery of metals

Abstract: An ion exchange process for selectively recovering a first metal in solution from a second metal without build-up of the second metal in the circuit. The process comprises first separating from the ion exchange recovery circuit for the first metal a bleed stream of the aqueous which is recycled to the leaching stage to maintain a required concentration of first metal in the leaching stage. The remaining aqueous is further contacted countercurrently with barren organic to completely remove all of the first metal from it. The aqueous is then sent to a recovery circuit for the second metal. After the second metal recovery the raffinate from this stage is returned to the leaching stage. The result is that the second metal is removed from the system at substantially the same rate at which it is introduced into the leaching stage in the continuous process.

Upgrading wide range gasoline stocks

Abstract: A PROCESS FOR UPGRADING WIDE RANGE GASOLINE STOCKS IS DISCLOSED WHEREIN THE FEED IS SEPARATED INTO C5, C6-C8 AND C9+ FRACTIONS, THE C6-C8 AND C9+ FRACTIONS ARE SEPARATELY REFORMED, REFORMATE FROM THE C9+ FRACTION IS DISTILLED TO REMOVE C5-C8 MATERIAL AND YIELD A HEAVY AROMATIC PRODUCT OF HIGH ANTIKNOCK VALUE, SAID C5-C8 MATERIAL IS COMBINED WITH REFORMATE FROM SAID C6-C8 FRACTION AND WITH AROMATIC DEHYDROCYCLIZATE FROM A SUBSEQUENT STEP, THE RESULTING MIXTURE IS EXTRACTED WITH AN AROMATIC-SELECTIVE SOLVENT TO YIELD A RAFFINATE AND C6-C8 AROMATIC PRODUCT OF HIGH PURITY AND ANTIKNOCK VALUE, THE RAFFINATE IS DISTILLED TO OBTAIN A C5-C6 PARAFFINIC FRACTION AND A HEAVY PARAFFINIC FRACTION, THE LATTER IS CATALYTICALLY DEHYDROCYCLIZED TO YIELD SAID AROMATIC DEHYDROCYCLIZATE, THE C5-C6 PARAFFINIC FRACTION IS COMBINED WITH SAID C5 FRACTION AND THE MIXTURE IS CATALYTICALLY ISOMERIZED.

A process for the hydrogenation of pyrolysis gasoline

Abstract: 1301019 Hydrogenation of pyrolysis gasoline SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 2 March 1970 [3 March 1969] 9894/70 Heading C5E Pyrolysis gasoline, from the steam cracking of naphtha to produce ethylene and/or propylene, is selectively hydrogenated at 3 in the liquid phase to convert diolefins to monoolefins and a fraction 7 of the hydrogenated product having an initial boiling point below 80‹ C. is separated at 5, heated to a temperature not exceeding 250‹ C. at a pressure of 20-80 kg./ cm. 2 and hydrogenated at 9 over a sulphidic molybdenum and alumina-containing catalyst at a reaction temperature below 320‹ C. under conditions such that the stream 7 passes into the first part of the catalyst bed as a liquid and the stream is fully evaporated at a point between “ and ¥ of the height of the catalyst bed. The selective hydrogenation at 3 can be carried out at 20-50 kg./cm. 2 and below 160‹ C. using a sulphided catalyst, e.g. containing 5-25% nickel on alumina and/or silica. The catalyst used in the hydrogenation at 9 can comprise 3-25% molybdenum and 1-10% of W, Re, Co and/or Ni. The effluent 10 from the second hydrogenation can be subjected to a third hydrogenation at 320-375‹ C. using a desulphurization catalyst such as a sulphidic molybdenum-containing catalyst on an alumina carrier and which can also contain cobalt at a space velocity between 2 and 10. The stream 13, from which hydrogen, hydrogen sulphide have been removed at 11 and recycled to reactor 9, is separated into an aromatic rich extract phase 16 and an aromatic-poor raffinate 15 by extractive distillation at 14. The aromatic extract is separated by fractional distillation into a benzene stream 18, a toluene stream 21, a mixture of xylenes and ethyl benzene 24 and a stream 27 boiling between 170‹ and 220‹ C. In another embodiment the stream 13 can be separated into a fraction boiling above 150‹ C. and a fraction boiling below 150‹ C. which is passed to the extractive distillation unit. Suitable extractive solvents are diethylene glycol, dipropylene glycol, phenol, sulphur dioxide, N-methyl pyrrolidone, sulpholane, dimethylsulphoxide and acetonitrile and can contain up to 10% of water. Sulphur compounds, such as hydrogen sulphide, carbon disulphide, mercaptans, and dialkyl sulphides can be added to the hydrogen and gasoline feed to the second hydrogenation if the gasoline fraction from the first hydrogenation contains less than 100 p.p.m. in sulphur. The raffinate 15 can be passed to a catalytic reforming plant or recycled to the ethylene cracker. The stream 27 can be hydrogenated with a Pt or Ni catalyst to remove any aromatic compounds therein and blended with aviation gasoline or kerosine.

Separation of cyclic hydrocarbons with molecular sieve adsorbent

Abstract: 1. A PROCESS FOR SEPARATING TWO STRUCTURALLY SIMILAR CYCLIC AROMATIC HYDROCARBONS CONTAINING IN THE RANGE OF 1-4 AROMATIC RINGS, AND IN THE RANGE OF 8-36 CARBON ATOMS AND WHEREIN SAID AROMATIC HYDROCARBONS CONTAIN AT LEAST ONE CONDENSED RING, SAID PROCESS COMPRISING: (A) CONTACTING A FLUID FEED MIXTURE COMPRISING SAID CYCLIC AROMATIC HYDROCARBONS WITH A SOLID ABSORBENT COMPRISING A PARTIALLY DEHYDRATED, SUBSTANTIALLY CRYSTALLINE ALUMINO-SILICATE ZEOLITE HAVING A CRITICAL PORE DIAMETER GREATER THAN ABOUT 6A, THE RATIO AL/SI OF THE ALUMINO- SILICATE FRAMEWORK OF THE ZEOLITE BEING IN THE RANGE OF 0.65-0.2, THE ZEOLITE HAVING BEEN PARTIALLY DEHYDRATED BY EXPOSURE TO A TEMPERATURE IN THE RANGE OF 80-300* C., WHEREBY THERE IS OBTAINED A RICH ADSORBENT CONTAINING AN ADSORBATE WHICH IS RICHER IN ONE SAID CYCLIC AROMATIC HYDROCARBON THAN WAS SAID FLUID FEED MIXTURE, AND A RAFFINATE PRODUCT WHICH CONTAINS LESS OF THE ONE SAID CYCLIC AROMATIC HYDROCARBON THAN DID SAID FLUID FEED MIXTURE; (B) SEPARATING SAID RAFFINATE PRODUCT FROM SAID RICH ADSORBENT AND, (C) REMOVING THE ONE SAID CUCLIC AROMATIC HYDROCARBON FROM SAID RICH ADSORBENT.

Method of producing jet fuel by upgrading light catalytic cycle oil

Abstract: JET FUEL IS PRODUCED BY EXTRACTIVE DISTILLATION OF LIGHT CATALYST CYCLE OIL BOILING IN THE JET FUEL BOILING RANGE USING CATALYST FRACTIONATOR BOTTOMS AS THE SOLVENT, AND SUBSEQUENT FINISHING SUCH AS MILD HYDROFINING OF LOWAROMATICS RAFFINATE.

Method of preparing dimethylsulphoxide

Abstract: A METHOD OF PREPARING DIMETHYLSULPHOXIDE BY OXIDIZING DIMETHYL SULPHIDE BY HIGH CONCENTRATED (70-100%) SOLUTIONS OF ORGANIC HYDROPEROXIDES E.G. ISOPROPYLBENZENEHYDROPEROXIDE OR ETHYLBENZENE HYDROPEROXIDE. THE PROCESS IS CARRIED OUT AT TEMPERATURES OF 20* -80* C. IN A TWOPHASE SYSTEM; THE FIRST PHASE IS AN AQUEOUS SOLUTION (1-8 MOLES H2O/MOL DMS) WITH AN ACID REACTION IN WHICH THE HYDROGEN ION CONCENTRATION IS FROM 10-6 TO 1 G./DM.3 SOLUTION, WHILE THE SECOND PHASE IS AN ORGANIC PHASE. EXTRACTION OF DIMETHYLSUPHOXIDE FROM THE REACTION SOLUTION IS EFFECTED BY THE AQUEOUS PHASE AND ANY REMAINING DIMETHYLSULPHOXIDE IN THE ORGANIC PHASE IS OBTAINED BY MEANS OF WASHING WITH AN AQUEOUS SOLUTION OF THE SAME HYDROGEN ION CONCENTRATION AS BEFORE. THE EXTRACTS ARE DISTILLATED UNDER REDUCED PRESSURE GIVING PURE DIMETHYLSULPHOXIDE. THE RAFFINATE IS A READY PRODUCT OR CAN SERVE AS A RAW MATERIAL FOR FURTHER SYNTHESES.

Raffinate hydrocracking process for uv stable lubricating oils

Abstract: HIGH QUALITY UV STABLE LUBRICATING OIL STOCKS ARE PREPARED BY SOLVENT EXTRACTING A HYDROCARBON FEEDSTOCK WITH A SOLVENT HAVING PREFERENTIAL SOLUBILITY FOR AROMATICS, THEREBY REDUCING THE AROMATIC CONTENT THEREOF AND RECOVERING A RAFFINATE PHASE THEREFROM. THE RAFFINATE IS STRIPPED OF SOLVENT AND SUBSEQUENTLY HYDROCRACKED MILD CONDITIONS TO INCREASE THE VISCOSITY INDEX OF THE RAFFINATE. THE HYDROCRACKATE PRODUCT IS THEN SOLVENT EXTRACTED WITH A SOLVENT HAVING PREFERENTIAL SOLUBILITY FOR AROMATICS, WHICH SOLVENT MAY BE THE SAME OR DIFFERENT THAN THE SOLVENT USED IN THE FIRST EXTRACTION, THEREBY FORMING A SECOND EXTRACT PHASE AND A SECOND RAFFINATE PHASE. THE EXTACT AND RAFFINATE PHAESE ARE SEPARATED AND THE EXTRACT PHASE STRIPPED OF SOLVENT AND RECYCLED TO THE HYDROCRACKER .

Process for producing unsaponifiablesfree tall oil products

Abstract: CRUDE SOAP SKIMMINGS, FROM THE KRAFT PLUP PROCESS, ARE UP-GRADED BY REMOVING CONTAINED UNSAPONIFIABLES, THIS IS DONE BY ADMIXING THE SKIMMINGS WITH WATER AND A DEEMULSIFYING ALCOHOL (E.G. METHANOL), CLARIFYING THE MIXTURE, AND CONTAINING THE CLARIFIED SOLUTION WITH A HYDROCARBON (E.G. HEPTANE) WHEREBY THE UNSAPONIFIABLES ARE EDTREATED INTO THE HYDROCARBO PHASE. THE COMPOSITION OF THE EXTRACTION FEED IS CONTROLLED TO ENSURE THAT SUBSTANTIALLY ALL THE UNSAPONIFIABLES ARE EXTRACTED WHILE ONLY A VERY SMALL AMOUNT OF THE SOAPS REPORT IN THE HYDROCARBON PHASE. THE RAFFINATE IS THEN DISTILLED TO RECOVER THE ALCOHOL.

Process for the preparation of 1,3-bis(2-pyrrolidonyl) butane

Abstract: Process for the preparation of 1,3-bis(2-pyrrolidonyl butane is provided comprising heating 1,3-bis(2-pyrrolidonyl)-1-butene to a temperature above the melting point thereof under hydrogen pressure in the presence of a hydrogenation catalyst for a sufficient period of time to substantially hydrogenate the 1,3bis(2-pyrrolidonyl)-1-butene and thereafter, recovering the hydrogenated product. Process is also provided for separating aromatic hydrocarbons from mixtures of aromatic/non-aromatic hydrocarbons comprising contacting a mixture of aromatic/non-aromatic hydrocarbons with 1,3-bis(2-pyrrolidonyl)butane to form an aromatic hydrocarbonrich extract phase and a raffinate phase, separating the aromatic hydrocarbon-rich extract phase from the mixture, and recovering the aromatic hydrocarbon from said extract phase.

Separation of unsaturated and saturated hydro - carbons by selective complexing with cuprous

Abstract: Mixtures of the hydrocarbons (pref. 2-20C olefins, paraffins and naphthenes) are treated with a Cu salt complex with an olefin and/or aromatic hydrocarbon (e.g. toluene) with a Cu satl:unsatd. hydrocarbon molar ratio of 0.25:1 to 2:1, at 0-195 degrees (pref. 25-150 degrees). An extract phase and a raffinate phase are obtained, and an unsatd. hydrocarbon-rich fraction is recovered from the former and a satd. hydrocarbon-rich fraction from the latter.

Alkylation acid recovery process with elimination of inert hydrocarbons

Abstract: Process for recovering used sulfuric acid alkylation catalyst and eliminating normal paraffin hydrocarbons from olefin feed stocks for alkylation. Used sulfuric acid catalyst from an alkylation unit is reacted in a first absorber with a first portion of olefin feed employing a stoichiometric excess of acid for substantially complete conversion of olefin to alkyl sulfate. Unreacted paraffin hydrocarbons are separated from the resulting reaction mixture and removed. The acid phase from the first absorber is extracted with isoparaffin hydrocarbon being alkylated and the raffinate acid therefrom is sent to a second absorber wherein the raffinate acid is reacted with a second portion of olefin feed employing a stoichiometric excess of olefin for substantially complete conversion of the free acid and alkyl acid sulfates to dialkyl sulfates. The dialkyl sulfates are then separated and passed to the alkylation unit. Unreacted olefinic hydrocarbons are separated from the reaction mixture and passed to either the first or second absorber.

Raffinate water sol solvent extraction from hydrocarbon - stream produced in primary extraction

Abstract: The solvent is extracted with aqs secondary solvent in an extraction tower contg. a plurality of perforated extraction decks, the solvent contng raffinate being passed through the perforation at a hole velocity of at least 2 ft/sec. pref 5-8 ft/sec. The raffinate stream may be non-aromatic hydrocarbons obtd in a primary aromatic process using sulpholane type solvent of formula (where R1, R2 R3 and R4 are independently H, 1-10C alkyl, 1-12C aralkyl and 1-8C alkoxy) contg. polyalkylene glycol. The raffinate may be passed up the tower in countercurrent to the secondary solvent water.