Showing papers on "Raffinate published in 1971"
TL;DR: In this paper, a pack of non-adsorbing glass particles has been used as a soil model to study the transfer of oil components to ground water, and experiments were carried out with a gas oil raffinate containing very small amounts of 2-isopropylphenol as a model for transferable components.
56 citations
Patent•
04 Mar 1971
TL;DR: In this article, the authors present a solution for separating dissolved copters from an AQUEOUS AMMONIACAL solution, also containing the COBALT and NICKEL, with a concentration of at least 50 grams of ammonium salt per litre.
Abstract: THE INVENTION RELATES TO A SOLVENT EXTRACTION PROCESS FOR SEPARATING DISSOLVED COPPER FROM AN AQUEOUS AMMONIACAL SOLUTION ALSO CONTAINING DISSOLVED COBALT AND NICKEL, THE SOLUTION HAVING A CONCENTRATION OF AT LEAST 50 GRAMS AMMONIUM SALT PER LITRE. THE PROCESS COMPRISES CONTACTING SAID AQUEOUS SOLUTION AT PH 6.5 TO 8.5 WITH AN A-HYDROXY OXIME WHEREBY THE COPPER VALUES ARE EXTRACTED FROM THE AQUEOUS PHASE INTO THE ORGANIC PHASE, AND SEPARATING THE RESULTANT COPPER LOADED ORGANIC PHASE FROM THE REMAINING AQUEOUS RAFFINATE PHASE CONTAINING THE COBALT AND NICKEL IN SOLUTION.
21 citations
Patent•
10 Feb 1971TL;DR: In this article, the authors describe a series of separations and separations of a large-scale OIL-WATER EMULSION in the presence of a polyane-butane solvent at or above the CONDENSATION PRESSURE threshold.
Abstract: TAR-OIL FROTHS AND OTHER HEAVY OIL-WATER EMULSIONS ARE DEMULSIFIED BY THE ADDITION OF A PROPANE-BUTANE SOLVENT AT OR ABOVE THE CONDENSATION PRESSURE THEREOF, AND AT TEMPERATURES IN A RANGE OF 170* TO 240*F., THE PROPORTIONS USED RANGING FROM ABOUT 0.5 TO 10 VOLUMES OF THE SOLVENT PER VOLUME OF OIL CONTAINED IN THE FEED EMULSION. THE COALESCED WATER PHASE AND ONE OR MORE OIL PHASES, ALONG WITH SAND PARTICLES, ARE THEREAFTER SEPARATED AND RECOVERED. WHEN USING ABOUT 3.5 TO 10 VOLUMES OF THE SOLVENT PER VOLUME OF OIL, THE EMULSION MAY BE BROKEN AND SEPARATED INTO A WATER PHASE AND INTO RAFFINATE OIL AND ASPHALTIC FRACTIONS OF CONTROLLABLE QUANTITLY AND PURITY. WHEN USING 0.5 TO 2 VOLUMES OF THE SOLVENT PER VOLUME OF OIL, THE OIL IS DEHYDRATED BUT NOT DEASPHALTED. THE SEVERAL DEMULSIFICATION AND PRODUCT SEPARATION STEPS CAN BE PRACTICED IN A PRESSURE COLUMN WHICH IS PROVIDED NEAR ITS TOP WITH AN INCLINED FEED-DISTRIBUTION TRAY PIERCED BY CYLINDRICAL RISER UNITS AND SLOTTED TO ALLOW THROUGHFLOW DOWNWARD. SAND PARTICLES PRESENT IN THE FEED, ALONG WITH WATER AND OPTIONALLY ASPHALT, PASS DOWNWARDLY THROUGH THE TRAY FOR DIS-CAHRGE INTO ONE OR MORE GRAVITYSETTLING CHAMBERS, WHILE THE REMAINING OIL COMPONENTS OF THE EMULSION ARE CARRIED UPWARDLY EITHER FOR DISCHARGE FROM THE COLUMN OR FOR RETURN TO A LOWER PORTION THEREOF FOR SECOND-STAGE GRAVITY-SETTLING OR FOR DEASPHALTING.
20 citations
Patent•
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TL;DR: In this paper, N-methyl-2-pyrrolidone is used as a deasphalting-solvent refining agent because of its greater thermal stability and solvent capacity.
Abstract: Lubricating oils are prepared by subjecting a residuum containing petroleum fraction to simultaneous deasphaltingsolvent refining using a solvent, e.g., furfural or N-methyl-2pyrrolidone. The resulting raffinate is hydrocracked and then dewaxed. N-methyl-2-pyrrolidone is superior to furfural as a deasphalting-solvent refining agent because of its greater thermal stability and solvent capacity.
19 citations
Patent•
01 Dec 1971
TL;DR: In this article, a C4 THROUGH C6 PARAFFIN FRACTION from a STRIAGHT Run GASOLINE is passed into a reformation zone, which separates normal paraffins from non-normals such as AROMATICS and ISO-PARAFFINS.
Abstract: HIGH OCTANE GASOLINE IS PRODUCED BY ISOMERIZING A C4 THROUGH C6 PARAFFIN FRACTION FROM A STRIAGHT RUN GASOLINE, THE HIGHER BOILING PORTION OF THE STRAIGHT RUN GASOLINE IS PASSED INTO A REFORMING ZONE. THE EFFLUENT FROM THE ISOMERIZATION ZONE IS PASSED INTO A MOLECULAR SIEVE SEPARATION ZONE WHICH SEPARATES NORMAL PARAFFINS FROM NON-NORMALS SUCH AS AROMATICS AND ISO-PARAFFINS. A PORTION OF THE EXTRACTED NORMAL PARAFFINS ARE THEN RECYCLED TO THE ISOMERIZATION ZONE TO EFFECT FURTHER PRODUCTION OF BRANCHED CHAIN PARAFFINS. THE RAFFINATE MATERIAL RECOVERED FROM THE MOLECULAR SIEVE SEPARATION ZONE IS SUFFICIENTLY HIGH IN OCTANE NUMBER TO BE UTILIZED AS A CLEAR GASOLINE. THE REFORMING AND ISOMERIZATION ZONE EFFECT THE CONVERSION OF THE RESPECTIVE FEED TO THOSE ZONES THROUGH THE USE OF SUITABLE CATALYTIC COMPONENTS. THE SEPARATION ZONE UTILIZES A TYPE A CRYSTALLINE ALUMINOSILICATE TO SELECTIVELY EXTRACT NORMAL PARAFFINS FROM A FEED CONTAINING NORMAL PARAFFINS AND OTHER NON-NORMAL COMPONENTS.
18 citations
Patent•
22 Jul 1971
TL;DR: A HYDROCARBON OIL can be pre-processed by a process of blending 50-98 PARTS (Pas discussed by the authorsERABLY 70-95) of a SEVERELY HYDROas discussed by the authorsINED NAPHTHENIC OIL HAVING a VGC from 0.820-0.899, a VISC from 40 to 200 SUS at 100*C.P. and a ULTRAVIOLET ABSORPTIVITY (UVA) of LESS THAN 0.04 in the 335 mill-scale region of the
Abstract: A HYDROCARBON OIL, USEFUL AS AN ELECTRICAL INSULATION MEDIUM, HAVING AN IMPULSE BREAKDOWN STRENGTH OF AT LEAST 150 KV., AN ASTM D-1313 TEST VALUE NO GREATER THAN 0.1 AND WHICH WILL PASS AT LEAST 50 HOURS OF THE ASTM D-943 STABILITY TEST, CAN BE PREPARED BY A PROCESS COMPRISING BLENDING 50-98 PARTS (PREFERABLY 70-95) OF A SEVERELY HYDROREFINED NAPHTHENIC OIL HAVING A VGC FROM 0.820-0.899, A VISCOSITY FROM 40 TO 200 SUS AT 100*C. AND A ULTRAVIOLET ABSORPTIVITY (UVA) OF LESS THAN 0.04 IN THE 335 MILLMICRON REGION WITH FROM 50-2 PARTS (PREFERABLY 30-5, FOR GOOD D-1313 TYPICALLY 10%) BY WEIGHT OF UNHYDROGENATED NAPHTHENIC DISTILLATE ( WHICH PREFERRABLY IS FREE FROM NAPHTHEMIC ACIDS). THE UNHYDROGENATED DISTILLATE CAN BE A RAFFINATE FROM EXTRACTION WITH AN AROMATIC SELECTIVE SOLVENT (E.G. FURFURAL, PHENOL). ANOTHER BLENDED OIL HAVING A SLUDGE-FREE DOUBLE LIFE OR UP TO 75 HOURS, CAN BE PREPARED BY THE PROCESS OF BLENDING THE UNHYDROGENATED DISTILLATE, THE HYDROGENATE DISTILLATE, AND A CYCLE OIL, IN SUCH BLENDS THE CYCLE OIL CAN BE FORM 0.1-10 WEIGHT PERCENT OF THE BLEND, THE CONCENTRATION PREFERABLY BEING SUCH THAT THE RATIO OF THE ULTRAVIOLET ABSORPTIVITY AT 335 MILLIMICRONS TO THE ABSORPTIVITY AT 330 MILLIMICRONS IN THE BLENDED PRODUCT IS NO LESS THAN 1.0. PREFERABLY, THE BLENDED OILS COMTAIN LESS THAN 25 P.P.M. OF TOTAL NITROGEN AND LESS THAN 5 P.PM. (TYPICALLY LESS THAN 1 P.P.M.) OF BASIC NITROGEN. BLENDS OF UNHYDROREFINED DISTILLATE, WITH A PARAFINIC LUBE OIL ( WHICH CAN BE HYUDROREFINED) ARE USEFUL AS TEXTILE OILS OR AS TECHNICAL WHITE OILS. SUCH BLENDS CAN ALSO CONTAIN A HYDROREFINED NAPHTHENIC OIL.
15 citations
Patent•
21 Oct 1971
TL;DR: In this paper, a mixture of iron and non-iron metals is reacted with hydrochloric acid solution to form an aqueous solution of metal chlorides, which solution is oxidized with oxygen or chlorine, or mixtures thereof and then the oxidized solution containing ferric chloride is subjected to liquid-liquid contact with an alkyl, aryl, or aralkyl ketone or ether having four to 10 carbon atoms.
Abstract: Iron material consisting of iron metal having associated minor amounts of other noniron metals is reacted with hydrochloric acid solution to form an aqueous solution of metal chlorides, which solution is oxidized with oxygen or chlorine, or mixtures thereof and then the oxidized solution containing ferric chloride is subjected to liquid-liquid contact with an alkyl, aryl or aralkyl ketone or ether having four to 10 carbon atoms so that the ferric chloride is transferred to the organic extract phase, leaving the noniron metal chlorides in the aqueous raffinate, and back-extracting the organic extract with an aqueous medium and separating the thus obtained aqueous extract solution of ferric chloride
15 citations
Patent•
28 Oct 1971
TL;DR: In this article, the authors proposed a method to add an in-gamer to a deterministic version of a DISTILLATE or a Raffinate from the time when the DISTillate is contacted with air.
Abstract: THE METHOD COMPRISES ADDING AN INHIBITOR TO A HYDROFINISHED DISTILLATE OR A HYDROFINISHED RAFFINATE FROM A DISTILLATE PRIOR TO THE TIME THAT SAID DISTILLATE OR SAID RAFFINATE IS CONTACTED WITH AIR. THE INHIBITOR IS A MEMBER SELECTED FROM THE GROUP CONSISTING OF HINDERED PHENOLS, AMINES, AND METAL COMPLEXES OF MANNICH CONDENSATION PRODUCTS FROM PHENOLS, ALDEHYDES, AND POLYAMINES. IF THE DISTILLATE HAS BEEN HYDROFINISHED IN A TWO-STAGE PROCESS UNDER RELATIVELY SEVERE CONDITIONS, AN INHIBITOR MAY BE ADDED TO THE EFFLUENT FROM THE FIRST STAGE AND AN INHIBITOR MAY BE ADDED TO THE PRODUCT FROM THE SECOND STAGE.
10 citations
Patent•
04 May 1971
TL;DR: In this article, a mixture of cylindrical dynamical dynamical vehicles is used to separate the conventional and non-aromatic dynamical vehicle from a mix-ture of hybrid vehicles in an environment of about 40*C to 80*C.
Abstract: AROMATIC HYDROCARBONS ARE SEPARATED FROM A MIXTURE OF LIQUID HYDROCARBONS. THE MIXTURE OF LIQUID HYDROCARBONS IS EXTRACTED IN THE LIQUID PHASE IN AN EXTRACTION ZONE AT A TEMPERATURE FROM ABOUT 40*C. TO AOUT 80*C. WITH ETHYLENEDIAINE SOLVENT HAVING A WATER CONTENT OF FROM 00% TO 20% BY WEIGHT TO FORM AN EXTRACTED PHASE AND A RAFFINATE PHASE. THE EXTRACTED PHASE COMPRISES PREDOMINANTLY AROMATIC HYDROCARBONS, SOLVENT AND A MINOR AMOUNT OF NON-AROMATIC HYDROCARBONS. THE RAFFINATE PHASE COMPRISES PREDOMINANTLY NON-AROMATIC HYDROCARBONS. THE EXTRACTED PHASE AND THE RAFFINATE PHASE ARE SEPARATELY COLLECTED. THE EXTRACTED PHASE IS COLLED TO A TEMPERATURE AT LEAST 300*C. LOWER THAN THE TEMPERATURE OF THE EXTRACTION STEP AND THEN SEPARATED INTO A HEAVIER SOLVENT CONTAINING PHASE AND ALIGHTER HYDROCARONS CONTAINING PHASE. THE NON-AROMATIC HYDROCARBONS IN THE LIGHTER HYDROCARBONS CONTAINING PHASE ARE SEPARATED A OVERHEAD PRODUCT BY MEANS OF EXTRACTIVE STRIPPING AT ATMOSPHERIC PRESSURE. THE AROMATIC HYDROCARBONS REMAIN IN THE RESIDUE OF THE EXTRACTIVE STRIPPING WHICH IS THEN SCRUBBED WITH WATER TO THEREBY OBTAIN AN AROMATIC HYDROCARBONS PHASE AND AN AQUEOUS ETHYLENEDIAMINE CONTAINING PHASE. THE AROMATIC HYDROCARBONS PHASE IS THEN RECTIFIED.
8 citations
Patent•
13 Jul 1971
TL;DR: A continued process for separating AROMATIC HYDROCARBONS from Mixed-hydraconians was described in this paper, where the authors investigated the feasibility of separating the two groups.
Abstract: A CONTINUOUS PROCESS FOR SEPARATING AROMATIC HYDROCARBONS FROM MIXED HYDROCARBON FEEDSTOCK CONTAINING ALIPHATIC AND AROMATIC HYDROCARBONS, SAID AROMATIC HYDROCARBONS BEING COMPRISED OFBENZENE, TOLUENE, AND C8 AROMATICS, COMPRISING THE FOLLOWING STEPS: (A) CONTACTING THE FEEDSTOCK WITH A PRIMARY SOLVENT AND A SECONDARY SOLVENT IN APRIMARY EXTRACTION ZONE AT A TEMPERATURE IN THE RANGE OF ABOUT 500*C. TO ABOUT 1500*C, AND A PRESSURE IN THE RANGE OF ABOUT ATMOSPHERIC PRESSURE TO ABOUT 200 P.S.I.A. WHEREIN THE PRIMARY SOLVENT IS A WATERSOLUBLE ORGAIC SOLVENT, WHICH HAS A HIGHER BOILING POINT THAN ANDIS NON-AZEOTROPIC WITH THE FEEDSTOCK, AND THE SECONDARY SOLVENT IS SELECTED FROM THE GROUP CONSISTING OF PARAFFINIC AND NAPHTHENIC HYDROCARBONS AND MIXTURES THEREOF, SAID HYDROCARBONS HAVING HIGHER BOILING POINTS THAN AND BEING NON-AZEOTROPIC WITH THE FEEDSTOCK, AND WHEREIN THE PRIMARY SOLVENT IS MAINTAINED IN SUFFICIENT AMOUNT TO EXTRACT ESSENTIALLY ALL OF THE AROMATIC HYDROCARBONS FROM THE FEEDSTOCK AND THE SECONDARY SOLVENT IS MAINTAINED IN SUFFICIENT ABOUT TO ACT AS A REFLUX FOR THE FEEDSTOCK, (B) WITHDRAWING FROM THE PRIMARY EXTRACTION ZONE PRIMARY EXTRACT COMPRISING AROMATIC HYDROCARBONS AND PRIMARY SOLVENT AND RAFFINATE COMPRISING ALIPHATIC HYDROCARBONS AND SECONDARY SOLVENT, (C) CONTACTING SAID PRIMARY EXTRACT WITH THE SECONDARY SOLVET IN ASECONDARY EXTRACTION ZONE WHEREIN THE TEMPERATURE AND PRESSURE ARE IN THE SAME RANGE AS IN STEP (A) AND THE SECONDARY SOLVENT IS MAINTANED IN SUFFICIENT AMOUNT TO EXTRACT ESSENTIALLY ALL OF THE ROMATIC HYDROCARBONS FROM THE PRIMARY EXTRACT, (D) WITHDRAWING FROM THE SECONDARY EXTRACTION ZONE PRIMARY SOLVENT AND SECONDARY EXTRACT COMPRISING AROMATIC HYDROCARBONS AND SECONDARY SOLVENT, (E) SUBJECTING THE RAFFINATE TO DISTILLATION IN A RAFFINATE DISTILLATION ZONE WHEREBY THE ALIPHATIC HYDROCARBONS ARE SEPARATED FROM THE SECONDARY SOLVENT, (F) WITHDRAWING THE SECONDARY SOLVENT FROM THE RAFFINATE DISTILLATION ZONE AND RECYCLING SAID SECONDARY SOLVENT TO AT LEAST ONE OFTHE EXTRACTION ZONES, (G) RECYCLING THE PRIMARY SOLVENT WITHDRAWN FROM THE SECONDARY EXTRACTION ZONE TO THE PRIMARY EXTRACTION ZONE, (H) SUBJECTING THE SECONDARY EXTRACT TO DISTILLATION IN AN AROMATICS DISTILLATION ZONE HAVING A MAXIMUM TEMPERATUURE OF 225*C., THETEMPERATURE GRADIENT BEING SUCH THROUGHOUT THE ZONE THAT ABOUT 90 TO 99 PERCENT BY WEIGHT OF THE BENZENE AND TOLUENE IN THE EXTRACT ENTERS INTO THE VAPOR PHASE AT THE TOP OFTHE ZONE, THE C8 AROMATICS AND ABOUT 1 TO 10 PERCENT BY WEIGHT OF THE BENZENE AND TOLUENE IN THEEXTRACT CONCENTRATE IN THE LIQUID PHASE AT A POINT BETWEEN ABOUT THE MIDDLE OF THE ZONE AND THE TOP OF THE ZONE, AND THE SECONDARY SOLVENT REMAINS ESSENTIALLY IN THE LIQUID PHASE AND ENTERS THE BOTTOM OF THE ZONE, (I) WITHDRAWING THEVAPOR PHASE MIXTURE OF BENZENE AND TOLUENE FROM THE AROMATICS DISTILLATION ZONE IN STEP (H) (J) WITHDRAWING THE LIQUID PHASE C8 AROMATICS, BENZENE, AND TOLUENE FROM THE AROMATICS DISTILLATION ZONE IN STEP (H), AND SUBJECTING SAME TO DISTILLATION IN A SIDE-DISTILLATION ZONE, SAID SIDE-DISTILLATION ZONE CONTAINING ABOUT 40 TO 60 PERCENT OF THE NUMBER OF EQUILIBRIUM STAGES CONTAINED IN THE AROMATICS DISTILLATION ZONE AND HAVING AMAXIMUM TEMPERATUURE OF AT LEAST 75*C. LESS THAN THE MAXIMUM TEMPERATURE OF THE AROMATICS DISTILLATION ZONE, AND SEPARATING THE C8 AROMATICS FROM THE BENZENE AND TOLUENE, (K) RECYCLING THE BENZENE AND TOLUENE FROM STEP (J) TO THE AROMATICS DISTILLATION ZONE, AND (1) WITHDRAWING THE SECONDARY SOLVENT FROM THE AROMATICS DISTILLATION ZONE OF STEP (H) AND RECYCLING SUCH SECONDARY SOLVENT TO AT LEAST ONE OF THE EXTRACTION ZONES.
6 citations
Patent•
04 May 1971
TL;DR: In this article, a mixture of cylindrical dynamical vehicles are separated into two phases: an EXTRACTED phase and a RAFFINATE phase, where the EXTRACTED phase is composed of three phases, i.e., a generator, a generator and a generator.
Abstract: AROMATIC HYDROCARBONS ARE SEPARATED FROM A MIXTURE OF LIQUID HYDROCARBONS. THE MIXTURE OF LIQUID HYDROCARBONS IS EXTRACTED IN THE LIQUID PHASE IN AN EXTRACTION ZONE AT A TEMPERATURE OF ABOUT 40*C. TO ABOUT 80*C. WITH ETHYLENEDIAMINE SOLVENT HAVING A WATER CONTENT OF FROM 0% TO 2/% BY WEIGHT TO FORM AN EXTRACTED PHASE AND A RAFFINATE PHASE. THE EXTRACTED PHASE COMPRISES PREDOMINANTLY AROMATIC HYDROCARBONS, SOLVENT, AND A MINOR AMOUNT OF NON-AROMATIC HYDROCARBONS. THE RAFFINATE PHASE COMPRISES PREDOMINANTLY NON-AROMATIC HYDROCARBONS. THE EXTRACTED PHASE AND THE RAFFINATE PHASE ARE SEPARATELY COLLECTED. THE EXTRACTED PHASE IS COOLED TO A TEMPERATURE AT LEAST 30*C. LOWER THAN THE TEMPERATURE OF THE EXTRACTION. THE COOLED EXTRACTED PHASE IS THEN SEPARATED INTO A HEAVIER SOLVET CONTAINING PHASE, AND A LIGHTER HYDROCARBONS CONTAINING PHASE WHICH IS SCRUBBED WITH WATER TO OBTAIN AN AQUEOUS ETHYLENEDIAMINE CONTAINING PHASE AND A HYDROCARBONS PHASE. THE HYDROCARBONS PHASE IS AZEOTROPICALLY DISTILLED TO OBTAIN AN OVERHEAD PRODUCT COMPRISING NON-AROMATIC HYDROCARBONS, AND A BOTTOM PRODUCT CONSISTING ESSENTIALLY OF AROMATIC HYDROCARBONS WHICH ARE SUBSEQUENTLY RECTIFIED.
Patent•
05 Apr 1971TL;DR: In this article, the authors describe the process of passing a hybrid cycle mixture through a cyclic ADSORPTION TECHNIQUE and passing it through a fixed-bed of an ACTIVATED CARBON.
Abstract: HYDROCARBON MIXTURES, SUCH AS LIGHT CYCLE OILS FROM A CATALYTIC CRACKING UNIT, PARAFFINIC LUBRICATING OILS AND THE LIKE, ARE SELECTIVELY SEPARATED BY A CYCLIC ADSORPTION TECHNIQUE INVOLVING PASSING THE HYDROCARBON MIXTURE THROUGH A FIXED BED OF ACTIVATED CARBON TO ADSORB SELECTIVELY MORE READILY ADSORBED COMPONENTS OR AN ADSORBATE PHASE WHILE COLLECTING LESS READILY ADSORBED COMPONENTS OR A RAFFINATE PHASE; PASSING A FIRST PORTION OF A PREDETERMINED VOLUME OF CARBON DISULFIDE THROUGH THE CARBON TO DISPLACE THE ADSORBATE PHASE WHILE COLLECTING A PORTION OF THE RAFFINATE PHASE AS A RECYCLE STREAM; PASSING THE REMAINDER OF THE CARBON DISULFIDE THROUGH THE CARBON WHILE COLLECTING AN ADSORBATE PHASE; PASSING A FIRST PORTION OF THE COLLECTED RECYCLE MATERIAL THROUGH THE CARBON WHILE COLLECTING AN ADSORBATE PHASE; PASSING THE REMAINDER OF THE COLLECTED RECYCLE MATERIAL THROUGH THE CARBON WHILE COLLECTING A RAFFINATE PHASE; AND SEPARATING CARBON DISULFIDE FROM THE RAFFINATE AND ADSORBATE PHASE FOR REUSE AS A DISPLACING FLUID.
Patent•
27 Aug 1971TL;DR: In this paper, the authors propose to remove the TERTIARY OLEFINS from their mix-ture with SULFURIC OCCURS by selectively polying them in the presence of a POLYMERIZATION CATALYST.
Abstract: REMOVING TERTIARY OLEFINE FROM THEIR MIXTURE WITH SECONDARY OLEFINS BY SELECTIVELY POLYMERIZING THE TERTIARY OLEFINS IN THE PRESENCE OF POLYMERIZATION CATALYST PREPARED BY REACTING CONCENTRATED SULFURIC ACID WITH AN EXCESS OF SECONDARY OLEFINS UNTIL NO FURTHER REACTION BETWEEN SECONDARY OLEFINS AND ACID OCCURS AND EXTRACTING THE RESULTING DIALKYL SULFATES WITH AN ISOPARRAFFIN HYDROCARBON SOLVENT, LEAVING THE POLYMERIZATION CATALYST AS THE RAFFINATE ACID.
Patent•
04 May 1971
TL;DR: In this paper, the authors describe the process of separating a mixture of conventional and non-aromatic vehicles from a mix of hybrid vehicles in an extraced phase and a raffinate phase.
Abstract: AROMATIC HYDROCARBONS ARE SEPARATED FROM A MIXTURE OF LIQUID HYDROCARBONS. THE MIXTURE OF LIQUID HYDROCARBONS IS EXTRACTED IN THE LIQUID PHASE IN AN EXTRACTION ZONE WITH ETHYLENEDIAMINE HAVING A WATER CONTENT OF FROM 00% TO 200% BY WEIGHT TO FORM AN EXTRACTED PHASE AND A RAFFINATE PHASE. THE EXTRACTED PHASE COMPRISES PREDOMINANATLY AROMATIC HYDROCARBONS, SOLVENT, AND AMINOR AMOUNT OF NON-AROMATIC HYDROCARBONS. THE RAFFINATE PHASE COMPRISES PREDOMINANTLY NON-AROMATIC HYDROCARBONS. THE EXTRACTED PHASE AND THE RAFFINATE PHASE ARE SEPARATELY COLLECTED. THE NON-AROMATIC HYDROCARBONS IN SAID EXTRACTED PHASE ARE SEARATED AS OVERHEAD PRODUCT BY MEANS OF EXTRACTIVE STRIPPING OF THE EXTRACTED PHASE, THE AROMATIC HYDROCARBONS REMAINING IN THE RESIDUE OF THE EXTRACTIVE STRIPPING. THERESIDUE OF THE EXTRACTIVE STRIPPING IS AZEOTROPICALLY DISTILLED, THE AROMATIC HYDROCARBONS AND A MINOR AMOUNT OF ETHYLENEDIAMINE SOLVENT BEING COLLECTED AS THE OVERHEAD PRODUCTS. THE ETHYLENEDIAMINE SOLVENT IS COLLECTED AS THE BOTTOM PRODUCT. THE OVERHEAD PRODUCTS ARE COOLED TO SEPARATE THEM INTO AN ETYLENEDIAMINE CONTAINING PHASE AND AN AROMATIC HYDROCARBONS CONTAINING PHASE. THE AROMATIC HYDROCARBONS CONTAINING PHASE IS SCRUBBED WITH WATER TO SEPARATE OUT A DILUTE AQUEOUS ETHYLENEDIAMINE CONTAINING PHASE, AND AROMATIC HYDROCARBONS PHASE, WHICH IS THEN RECTIFIED.
Patent•
08 Mar 1971
TL;DR: A SELECTED AROMATIC HYDROCARBON is separated from its mixtures with other AROACHs by forming a LITHIUM-ALUMINUM CHLORIDE COMPLEX with an UNSATURATED COMPOUND as mentioned in this paper.
Abstract: A SELECTED AROMATIC HYDROCARBON IS SEPARATED FROM ITS MIXTURE WITH OTHER AROMATIC HYDROCARBONS BY FORMING A LITHIUM-ALUMINUM CHLORIDE COMPLEX WITH AN UNSATURATED COMPOUND WHICH IS USED TO EXTRACT A MIXTURE OF AROMATIC HYDROCARBONS TO FORM A RAFFINATE PHASE AND AN EXTRACT COMPLEX PHASE; THE PHASES ARE SEPARATED AND THE EXTRACT COMPLEX PHASE IS WASHED WITH A PORTION OF THE COMPOUND AND THERE IS RECOVERED FROM THE WASHED EXTRACT COMPLEX PHASE A SECOND EXTRACT PHASE LEAN IN SAID COMPOUND AND A SECOND RAFFINATE PHASE COMPRISING SAID COMPOUND AND A SELECTEDAROMATIC HYDROCARBON WHICH IS THEN RECOVERED FROM THE SECOND RAFFINATE PHASE.
Patent•
10 May 1971TL;DR: In this paper, a solvable process for the separation of 1,1,2-TRICHLOROTriFLyorETHANE from a first LIQUID MIXTURE of 1.1DIFFUORETHANE is described.
Abstract: 1. A SOLVENT EXTRACTION PROCESS FOR THE SEPARATION OF 1,1,2-TRICHLOROTRIFLYORETHANE FROM A FIRST LIQUID MIXTURE OF 1,1,2 - TRICHLOROTRIFLUORETHANE AND 1,2 - DICHLORO-1,1DIFFUORETHANE, COMPRISING: CONTACTING SAID FIRST LIQUID MIXTURE WITH SULFOLANE AT A CONTACTING TEMPERATURE AT WHICH SULFONANE IS LIQUID AND STABLE THEREBY FORMING AN EXTRACT PHASE AND A RAFFINATE PHASE; AND SEPARATING SAID PHASES.
Patent•
05 Apr 1971
TL;DR: In this article, the authors describe a cyclic ADSORPTION TECHNIQUE, in which the mixture of a light cycle oil from a CATALYTIC CRACKING UNIT is selected by a CYCLIC ADSorPTion TECHNIQUE.
Abstract: HYDROCARBON MIXTURES, SUCH AS LIGHT CYCLE OILS FROM A CATALYTIC CRACKING UNIT, ARE SELECTIVELY SEPARATED BY A CYCLIC ADSORPTION TECHNIQUE INVOLVING PASSING THE HYDROCARBON MIXTURE THROUGH A FIXED BED OF ACTIVATED CARBON TO ADSORB SELECTIVELY POLYCYCLIC AROMATIC COMPONENTS AS AN ADSORBATE PHASE WHILE COLLECTING LESS READILY ADSORBED COMPONENTS AS A RAFFINATE PHASE; PASSING A FIRST PORTION OF A PREDETERMINED VOLUME OF CARBON DISLFIDE THROUGH THE CARBON TO DISPLACE THE ADSORBATE PHASE WHILE COLLECTING A PORTION OF THE RAFFINATE PHASE AS A RECYCLE STREAM; PASSING THE REMAINDER OF THE CARBON DISULFIDE THROUGH THE CARBON WHILE COLLECTING AN ADSORBATE PHASE; PASSING A FIRST PORTION OF THE COLLECTED RECYCLE MATERIAL, THROUGH THE CARBON WHILE COLLECTING AN ABSORBATE PHASE; PASSING THE RE- MAINDER OF THE COLLECTED RECYCLE MATERIAL THROUGH THE CARBON WHILE COLLECTING A RAFFINATE PHASE; SEPARATING CARBON DISULFIDE FROM THE RAFFINATE AND ADSORBATE PHASE FOR REUSE AS A DISPLACING FLUID; PASSING THE ADSORBATE TO AT LEAST ONE HYDROGEN TREATING OPERATION UNDER CONDITIONS SUCH THAT RESIDUAL ALIPHATIC HYDROCARBONS ARE CRACKED, RESIDUAL ALKYL MONOCYCLIX HYDROCARBONS ARE DEALKYLATED, POLYCYCLIC AROMATICS REMAIN UNREACTED AND THE MIXTURE IS DESULFURIZED, SEPARATING THE HYDROGEN-TREATED PRODUCT INTO A LIGHT FRACTION AND A HEAVY FRACTION AND SUBJECTING THE HEAVY FRACTION TO A HYDRODEALKYLATION TREATMENT TO PRODUCE SUBSTANTIAL VOLUMES OF NAPHTHALENE.
Patent•
16 Aug 1971TL;DR: In this article, a process for the preparation of 1,3-bis(2-pyrrolidonyl) butane is provided, which involves heating 1, 3-bis (2-polymorphic acid)-1-butene to a temperature above the melting point under hydrogen pressure in the presence of a hydrogenation catalyst.
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.
Patent•
26 Oct 1971
TL;DR: In this article, a process for separating 2,4,5-T and DIOXIN from SILVEX was described, where the DioXin was used to detect the presence of 2.4-5-t and 2.5-to-3-t ALKALI METAL METAL SALT.
Abstract: 1. A PROCESS FOR SEPARATING 2,4,5-T AND DIOXIN FROM SILVEX CONTAMINATED WITH 2,4,5-T UP TO ABOUT 1-5 PARTS BY WEIGHT PER HUNDRED PARTS BY WEIGHT OF SILVEX, AND WITH DIOXIN UP TO ABOUT 80 PARTS BY WEIGHT PER MILLION PARTS BY WEIGHT OF SILVEX, WHICH COMPRISES: (1) ADMIXING IN AN AQUEOUS MEDIUM SAID CONTAMINATED SILVEX WITH A QUANTITY OF ALKALI METAL HYDROXIDE MATERIAL SUFFICIENT TO CONVERT 2,4,5-T AND SILVEX TO THE CORRESPONDING ALKALI METAL SALTS, WHILE ESTABLISHING AND MAINTAINING THE RESULTING REACTION MIXTURE IN A TEMPERATURE RANGE IN WHICH THE 2,4,5-T ALKALI METAL SALT IS SUBSTANTIALLY INSOLUBLE AND THE SILVEX ALKALI METAL SALT IS SUBSTANTIALLY SOLUBLE, WHEREBY 2,4,5-T ALKALI METAL SALT IS PRECIPITATED; (2) SEPARATING PRECIPITATED 2,4,5-T ALKALI METAL SALT FROM THE RESULTING REACTION MIXTURE; (3) EFFECTING FRACTIONAL LIQUID-LIQUID EXTRACTION OF THE DIOXIN-CONTAMINATED SILVEX ALKALI METAL SALT PORTION OF SAID REACTION MIXTURE WITH A POLAR LIQUID SOLVENT CONSISTING ESSENTIALLY OF WATER, AND A NON-POLAR LIQUID SOLVENT, THE VOLUMERTRIC RATIO OF POLAR LIQUID SOLVENT TO NON-POLAR LIQUID SOLVENT BEING SELECTED SO THAT MORE SILVEX ALKALI METAL SALT IS DISSOLVED BY THE POLAR LIQUID SOLVENT THAN BY THE NON-POLAR LIQUID SOLVENT, WHILE MORE DIOXIN IS DISSOLVED BY THE NON-POLAR LIQUID SOLVENT THAN BY THE POLAR LIQUID SOLVENT, WHEREBY THERE ARE OBTAINED AN EXTRACT FRACTION WITH A SUBSTANTIAL PORTION OF THE DIOXIN, AND A FAFFINATE FRACTION COMPRISING SILVEX ALKALI METAL SALT; AND (4) TREATING SAID RAFFINATE FRACTION TO RECOVER SILVEX THEREFROM.
Patent•
28 Jan 1971TL;DR: In this article, a LIQUID PHASE SOLVENT EXTRACTION PROCESS for SEPARATING ACETALDEHYDE from 3-HYDROXYBUTANAL was described.
Abstract: 1. A LIQUID PHASE SOLVENT EXTRACTION PROCESS FOR SEPARATING ACETALDEHYDE FROM 3-HYDROXYBUTANAL, SAID PROCESS COMPRISING INTIMATELY CONTACTING A MIXTURE COMPRISING ACETALDEHYDE AND 3-HYDROXYBUTANAL HAVING A PH WITHIN THE RANGE OF 3.5 TO 6.0 WITH LIQUID C5-C8 MONONUCLEAR CYCLOALKANE SOLVENT, ALLOWING A RAFFINATE PHASE RICH IN 3-HYDROXYBUTANAL AND AN EXTRACT PHASE COMPRISING ACETALDEHYDE DISSOLVED IN SAID CYCLOALKANE SOLVENT TO FORM, FOLLOWED BY SEPARATING THE RESULTING EXTRACT PHASE FROM THE RESULTING RAFFINATE PHASE, SAID CYCLOALKANE HAVING A RING OF FROM 5 TO 7 CARBON ATOMS.
Patent•
20 Dec 1971
TL;DR: In this paper, a solvent extraction system utilizing a countercurrent extraction column and an extractive distillation stripper for recovery of C6-C8 aromatic hydrocarbons is presented.
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.