Abstract: The present disclosure provides a novel azeotropic or azeotrope-like composition comprising hydrogen fluoride and 1,1,2-trifluoroethane (HFC-143), 1-chloro-2,2-difluoroethane (HCFC-142), or 1,2-dichloro-1-fluoroethane (HCFC-141); and a separation method using the composition. An azeotropic or azeotrope-like composition comprising hydrogen fluoride and HFC-143. An azeotropic or azeotrope-like composition comprising hydrogen fluoride and HCFC-142. An azeotropic or azeotrope-like composition comprising hydrogen fluoride and HCFC-141. A separation method of a composition comprising hydrogen fluoride and at least one member selected from the group consisting of HFC-143, HCFC-142, and HCFC-141.

Abstract: Methods for recovering valuable compounds and substances from plants after distillation of oils are disclosed. The methods involve various aqueous and non-aqueous solvent extraction of plant material from which oils have been distilled previously.

Abstract: Disclosed is an adjuvant for improving the bioavailability of bioactive compositions. The adjuvant is prepared from a byproduct of mint flavor production. In vitro and in vivo testing confirms effectiveness. The adjuvant contains a mixture of compounds which is effective to improve the oral bioavailability of a bioactive composition normally having limited absorptivity, and it comprises a mixture of nonpolar compounds and compounds with some polar characteristics. In preferred form the nonpolar compounds comprise compounds selected from a group that includes terpene hydrocarbons and terpene derivatives and the compounds with some polar characteristics comprise compounds selected from a group that includes aldehydes, alcohols and ketones. The preferred compositions will have a ratio of nonpolar compounds and compounds with some polar characteristics is within the range of from 5:1 to 20:1. The adjuvants can enhance delivery of CoQ10 and other bioactive compositions, such as carotenoids (e.g.

Abstract: The present invention relates to a process for obtaining food grade hexane, comprising: fractionating a hydrocarbon feed having a boiling point in the range of 50° C. to 140° C. to obtain a hydrocarbon fraction having boiling point in the range of 63° C. to 69° C. and having 3%-15% (wt/wt) of aromatic compounds content; extracting the hydrocarbon fraction by counter current solvent extraction using sulfolane as a solvent to obtain a first raffinate phase; extracting the first raffinate phase by co-current solvent extraction using sulfolane as a solvent to obtain a second raffinate phase; and washing the second raffinate phase with water to obtain a food grade hexane containing less than 100 ppm of aromatic compounds.

Abstract: Processes for the reduction and/or removal of permanganate reducing compounds (PRC'S) formed by the carbonylation of methanol in the presence of a Group VIII metal carbonylation catalyst to produce acetic acid are disclosed. More specifically, processes for reducing and/or removing PRC's or their precursors from intermediate streams during the formation of acetic acid by said carbonylation processes are disclosed. In particular, processes in which a low boiling overhead vapor stream from a light ends column is subjected to a distillation to obtain an overhead that is subjected to an extraction to selectively remove and/or reduce PRC's from the process is disclosed. The processes include steps of recycling one or more return streams derived from the distillation step and/or the extraction step to a light ends column and/or a drying column in order to improve water control in the overall reaction system.

Abstract: A method for removing a contaminant from a hydrochlorofluoroolefin (such as trans-1,1,1-trifluoro-3-chloro-2-propene (1233zd(E))) includes extracting a chlorofluorocarbon (such as trichlorofluoromethane (R11)) from a mixture comprising the hydrochlorofluoroolefin and the chlorofluorocarbon using extractive distillation in the presence of an extractive solvent comprising a chlorinated compound to form a purified hydrochlorofluoroolefin. This separation method provides for removal of a contaminant, such as R11, from a hydrochlorofluoroolefin, such as 1232zd(E), which are not separable by conventional distillation methods. The method may employ a process utilizing two distillation columns, for example, a first extractive distillation column and a second solvent recovery column, which allows for recycle of the extractive solvent to the first extractive distillation column.

Abstract: Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid using an extractive distillation column. The column yields a residue that comprises ethanol, acetic acid, and the extractive agent. The extractive agent may be water and may be separated from the residue and returned to the extractive distillation column.

Abstract: The present invention describes a process to reduce or eliminate at least one pollutant in a starting material, said starting material is at least one of an oil, a fat, its derivatives and mixtures thereof, of animal, krill, algae or microbial origin or biofuel, being totally or partially esterified or transesterified, or of vegetable origin, being raw, esterified or transesterified, to which optionally it is added a fluid, said fluid is at least one of an ester, a partial glyceride, a monoglyceride, a diglyceride and mixtures thereof, subjecting the starting material to at least one stage of extraction or chromatography or distillation. The process of the invention provides a product suitable to be used in food, pharmacy, cosmetic and as a dietary supplement.

Abstract: Provided are a separation and recovery device for a liquid waste including a radionuclide, and a separation and recovery method using the same. Specifically, the present disclosure relates to a separation and recovery device that may effectively separate a liquid waste, such as a waste detergent including a radionuclide, and simultaneously, may prevent the release of tritium and radiocarbon to the outside, and a separation and recovery method using the same.

Abstract: The present application relates generally to bio-adhesive components isolated from bio-oil prepared from animal waste, methods of preparation of the bio-adhesive components and uses thereof. Such uses include, but are not limited to, asphalt bio-binders, bio-adhesion promoters, asphalt bio-rejuvenators, asphalt bio-extenders, bio-asphalt as well as uses in roofing, soil stabilization, crack and joint sealing and flooring adhesives.

Abstract: A method for cross connecting the lean solvent supply lines between the liquid liquid extraction (LLE) and the extractive distillation (ED) processes thereby using the LLE column as the outlet for removing accumulated heavy hydrocarbons (HCs) and polymeric materials from the solvent loop of both processes to maintain their solvent performance. The unique capabilities of the LLE column in rejecting heavy HCs from the solvent into a raffinate product stream that leaves the system enable the removal of the accumulated heavy HCs and polymeric materials from the closed solvent loop of the ED process when their lean solvent loop are cross connected. Cross connection requires minimum equipment change. In the revamped system, the solvent recovery column (SRC) in LLE process supplies lean solvent for the extractive distillation column while the SRC of the ED process supplies lean solvent for LLE column.

Abstract: Processes and systems for improving the quality and yield of distillate columns.

Abstract: A process for purifying a brine of organic compounds comprising: (a) supplying a brine that comprises at least one organic compound; (b) feeding at least one stripping zone with the brine from (a) and at least one stripping agent; (c) withdrawing from the stripping zone at least one fraction (I) consisting essentially of brine, the content of the organic compound being lower in fraction (I) than in the brine from step (a), and at least one fraction (II) consisting essentially of the stripping agent; wherein the temperature (T1) of the hotter fraction of the two fractions (I) and (II) and the temperature (T2) of the colder fraction of the two fractions (I) and (II), such temperatures expressed in degrees Celsius being the temperatures measured before any possible thermal conditioning which might be carried out before and/or during their withdrawal from the stripping zone, correspond to the following formula: 6×10?7(T1)3.

Abstract: Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid using an extractive distillation column. The column yields a residue that comprises ethanol, acetic acid, and the extractive agent. The extractive agent may be water and may be separated from the residue and returned to the extractive distillation column.

Abstract: A process and device of coupling separation and purification to produce ethyl tert-butyl ether (ETBE) is provided, wherein ethanol containing 1 wt % to 15 wt % of water, and a mixture containing ETBE and ethanol are fed into the distillation-extraction coupling zone for separation and purification. Said distillation-extraction coupling zone is composed of a distillation column and an extraction column. Said process and device can achieve the cogeneration of ETBE and ethanol, and possesses high commercial values.

Abstract: This invention relates to processes for producing acetic acid and, in particular, to improved processes for recovering C2+ alkyl halides and removing permanganate reducing compounds formed during the carbonylation of methanol in the presence of a Group VIII metal carbonylation catalyst to produce acetic acid.

Abstract: This invention relates to processes for producing acetic acid and, in particular, to improved processes for recovering C2+ alkyl halides and removing permanganate reducing compounds formed during the carbonylation of methanol in the presence of a Group VIII metal carbonylation catalyst to produce acetic acid.

Abstract: A top temperature T1 of a distillation tower 1 is held below a liquefying temperature of a light fraction by returning a part of an exhaust gas W, which is cooled by a condenser 5, to the upper zone of the distillation tower 1. A bottom temperature T2 is raised up to 300° C. at highest by returning a part of a liquid product P from a re-boiler 3 to a lower zone of the distillation tower 1. When a liquid hydrocarbon L comes in countercurrent contact with a stripping gas G inside the distillation tower 1 with the temperature profile that an inner temperature gradually falls down along an upward direction, mercury is efficiently transferred from the liquid L to a vapor phase without effusion of the light fraction in accompaniment with the exhaust gas W.

Abstract: A process for fractionating a crude C4 fraction comprising butanes, butenes, 1,3-butadiene and small amounts of other hydrocarbons including C4-acetylenes, by extractive distillation using a selective solvent, wherein the crude C4 fraction (1) is fed into the middle region of a first extractive distillation column (K I) and the selective solvent (2) is fed into the column at a point above that at which the crude C4 fraction (1) is introduced and a gaseous side stream (3) which comprises the C4-acetylenes together with predominantly the selective solvent and in which the concentration of the C4-acetylenes is below the spontaneous decomposition limit is taken off from the first extractive distillation column (K I) at a point below the feed point for the crude C4 fraction (1) and an overhead stream (5) comprising the components which are less soluble than the C4-acetylenes in the selective solvent is taken off from the top of the first extractive distillation column, is proposed.

Abstract: The present invention No. I is to obtain a high purity 3-alkoxy-1-propanol having the content of alcoholic impurities of not more than 0.3% by weight by allowing to react acrolein with a linear or branched alcohol having a carbon number of 1-4 using acrolein having the content of propionaldehyde of not more than 1% by weight as a raw material, a 3-alkoxy-1-propanol is produced by a hydrogenation reaction using hydrogen of a reaction mass under the presence of a catalyst, followed by recovering through a distillation of the 3-alkoxy-1-propanol having the content of alcoholic impurities of not more than 0.3% by weight from a crude solution in the hydrogenation reaction.

Abstract: A mixture of propylene oxide and methanol is separated by liquid/liquid extraction using water and a hydrocarbon such as n-octane as extractive solvents.

Abstract: Process for the separation of hydrogen fluoride from its mixtures with a hydrofluoroalkane containing from 3 to 6 carbon atoms, by extraction using an organic solvent.

Abstract: Ferrofluid coated particles resulting from a ferrofluid materials separation process are washed with a solvent which is the same material as the liquid carrier employed in the ferrofluid. The result is a “dirty” solvent which is a very weak ferrofluid. The dirty solvent is then filtered or centrifuged to remove dust particles and other impurities and then the solvent is recovered by distillation in a distillation unit. The solvent can then be reused in the materials reclamation process. The residue in the distillation unit is surfactant-coated particles of ferrofluid. This residue is mixed with either clean or unprocessed solvent in the right proportion and the slurry is passed through an attritor to convert it to a high grade ferrofluid. The ferrofluid can also be reused in the materials separation process.

Abstract: Process for the separation of hydrogen fluoride from its mixtures with a hydrofluoroalkane containing from 3 to 6 carbon atoms, by extraction using an organic solvent.

Abstract: A process for purifying at least 90% pure n-butyl chloride which is present in a mixture with other C.sub.1 to C.sub.4 alkyl chlorides, C.sub.1 to C.sub.4 alcohols, esters, ketones, nitrites, and organic sulfur compounds. In this process the mixture is first distilled, with high-boilers being separated off, and then washed in a plurality of stages with water and with dilute alkali metal hydroxide solution, and, optionally, an aqueous solution of H.sub.2 O.sub.2. In this manner, even a typical impurities may be separated off and a >99% pure product may be obtained.

Abstract: A process for separating pentafluoroethane and 1,1,1-trifluoroethane, which comprises extraction distilling a mixed fluid comprising pentafluoroethane and 1,1,1-trifluoroethane in the presence of at least one extracting agent selected from the group consisting of esters and ketones each having a standard boiling point of from -10.degree. C. to 100.degree. C. Also disclosed is a process for separating pentafluoroethane, 1,1,1-trifluoroethane and chloropentafluoroethane, which comprises extraction distilling a mixed fluid comprising pentafluoroethane, 1,1,1-trifluoroethane and chloropentafluoroethane in the presence of at least one extracting agent selected from the group consisting of esters and ketones each having a standard boiling point of from -10.degree. C. to 100.degree. C.

Abstract: A solvent containing low-boiling and high-boiling impurities in an evaporating section, so that the high-boiling impurities is left as a tank bottom waste, and a solvent vapor from the section is guide through a mist separator into a condenser. A condensate produced in the condenser is returned to the mist separator so as to serve as a mist catching liquid. A fraction not having condensed in the condenser is fed to a rectifying section where fractional condensation is performed so that the low-boiling impurities are condensed to be removed. A remainder of the solvent vapor from which the impurities have been removed is also condensed and recovered for reuse in the resist washing/exfoliating step during manufacture of liquid crystal devices or IC, so that the soiled solvent need not be discarded or treated in a remote cite, thereby facilitating the process or the step using the solvent.

Abstract: 3-Methyl-1-butanol cannot be separated from 1-pentanol by distillation or rectification because of the closeness of their boiling points. 3-Methyl-1-butanol is readily separated from 1-pentanol by extractive distillation. Effective agents are butyl benzoate, 2-undecanone and diethylene glycol methyl ether.

Abstract: 3-Methyl-1-butanol cannot be separated from 1-pentanol by distillation or rectification because of the closeness of their boiling points. 3-Methyl-1-butanol is readily separated from 1-pentanol by azeotropic distillation. Effective agents are methylcyclohexane, methyl formate and tetrahydrofuran.

Abstract: Vinyl formate containing formic acid, acetaldehyde and water following synthesis is separated from formic acid and water in a first distillation stage and from acetaldehyde in a second stage to give pure vinyl formate.

Abstract: A method for recovering volatile, organic compounds from manure, by:i) acidifying and concentrating the manure;ii) condensing the formed vapor; andiii) separating the volatile, organic compounds from the condensate.Preferably the volatile, organic compounds are removed from the condensate by liquid extraction, crystallization, distillation and/or ion exchange.

Abstract: A method of producing ethanol from a fermentation source for direct blending into gasoline to form gasohol is provided by extracting ethanol from the fermentation broth with a non-toxic solvent compatible with gasoline. The invention includes extraction outside of the fermentor and the recycling of the extracted broth back to the fermentor. An extracting column is used for the extraction and recycling and the extract can be dried before blending it with the gasoline. The preferred solvent is an alkylate.

Abstract: Acetone cannot be easily separated from benzene in high purity by distillation because of the closeness of their vapor pressures. Acetone can be readily removed from benzene by azeotropic distillation using certain aromatic hydrocarbons. Typical effective azeotropic distillation agents are: toluene, ethyl benzene and mesitylene.

Abstract: In a process for the recovery of acetic acid by extracting acetic acid from an aqueous acetic acid solution containing a metallic salt of sulfuric acid with an organic extractant comprising a tertiary amine and an organic diluent and recovering acetic acid from the liquid extract, a mixture of a tertiary amine containing sulfuric acid and an organic diluent is used as an organic extractant so as to suppress energy consumption and to increase extraction efficiency.

Abstract: Distillation of the heavy waste stream from the manufacture of phenol via the cumene process provides an overhead stream containing phenol, acetophenone and 2-phenyl propionaldehyde. Extraction of the overhead stream with aqueous caustic removes the phenol and subsequent distillation of the remaining two components in the presence of a catalytic amount of caustic provides a substantially pure acetophenone distillate.

Abstract: An improved method of stripping unreacted alkylene glycol monoalkyl ethers and unreacted monocarboxylic or halogenated monocarboxylic acids from a mixture containing the monocarboxylic acid ester prepared therefrom by acid catalyzed esterification without any significant loss of the product ester. The method involves the injection of water into the distillate during the stripping and is particularly suitable for the recovery of propylene glycol monomethyl ether and acetic acid from esterification reaction mixtures containing a predominate amount of product propylene glycol monomethyl ether acetate. The process allows for removal and recovery or recycle of the ether and acid and the preparation of a higher purity product ester.

Abstract: Tert.butyl alkyl ethers are produced from a C.sub.4 hydrocarbon feedstock containing isobutene, and the butene-1 is recovered at high purity by extractive distillation of the isobutene-free C.sub.4 hydrocarbon stream in the presence of a solvent chosen from acetone, acetonitrile, dimethylformamide, methanol, n-methylpyrrolidone, formylmorpholine and furfural.After removing the solvent, the extract is rectified, and the butene-1 separates as overhead product of high purity.

Abstract: Low energy process for the production of gasoline-ethanol blends, comprising dehydrating the aqueous ethanolic product from a conventional fermentation process, preferably containing about 6 wt. % ethanol, so as to generate an aqueous ethanolic effluent containing about 90 wt. % ethanol; mixing the effluent with gasoline feedstock; chilling the resultant gasoline-aqueous ethanol mixture to a temperature of about -10.degree. F., without forming ice, thereby to form (1) a gasohol blend containing about 10 wt. % ethanol and (2) an aqueous stream comprising some ethanol and traces of gasoline; extracting the gasoline-containing aqueous stream with a minor stream of the fermentation ethanol product in order to recover the gasoline it contains; and recovering said blend to produce a gasohol product under-saturated with water at all operating temperatures above -10.degree. F.

Abstract: Gasoline-ethanol mixtures useable as motor fuel are produced by a relatively low energy process comprising interrelated distillation and extraction steps. In the first step, aqueous ethanol, such as an ethanol fermentation beer, is subjected to fractional distillation to produce a distillate of at least 75 weight percent ethanol, which is then subjected to extraction with gasoline under conditions producing an extract containing the desired amount of ethanol, such as 8 to 14% by weight. The aqueous phase raffinate from the extraction is returned to the fractionation column for redistillation.

Abstract: Isobutane is oxidized to provide a debutanized oxidate comprising tertiary butyl alcohol, acetone, water and other byproducts including high boiling products. Water is removed by extractive distillation using a combination of water and xylene as the extractant. The molar amount of recycled water is greater than the amount of water to be removed from the oxidate. By thus recirculating water through the decantation zone the acetone is satisfactorily coextracted from the butyl alcohol in such a manner that a stream of acetone and a stream of water, as well as the desired dry stream of tertiary butyl alcohol can be withdrawn. If the water is not recycled, the acetone will concentrate in the upper section of the distillation zone and reduce the volatility of water, thereby inhibiting the water removal from the tertiary butyl alcohol.

Abstract: Esters are treated with alkali metal borohydride to produce alcohols. Substantially constant boiling admixtures of: methanol/methyl heptafluorobutyrate, water/1,1-dihydroheptafluorobutanol, and water/methyl heptafluorobutyrate are described.

Abstract: There is disclosed an azeotropic distillation process for separating and recovering hexamethyl disiloxane (HMDO) from toluene in a spent liquor mixture. An HMDO azeotrope former, pyrrolidone, is added to the liquor. The pyrrolidine is added in an amount of at least about 1.81 parts by weight per 1.0 part by weight of HMDO. Preferably, it is added in excess, as about 2.7 to about 5.4 parts by weight of pyrrolidine per 1.0 part by weight of HMDO. The resulting azeotrope of HMDO and pyrrolidine is then separated by distillation from the liquor. The pyrrolidine may be subsequently recovered from the HMDO by extraction with water. Other HMDO azeotrope formers, such as tertiary butanol, may also be utilized.

Abstract: Alkane dicarboxylic acids of at least 4 carbon atoms particularly the mixture of succinic, glutaric and adipic acids obtained as byproduct in the manufacture of adipic acid are purified by co-distillation with an alkylbenzene having an atmospheric pressure boiling point of 300.degree. to 350.degree. C. especially dodecylbenzene.

Abstract: There is disclosed an azeotropic distillation process for separating toluene from methyl isobutyl ketone (MIBK) in a spent liquor mixture. A toluene azeotrope former, preferably methanol, is added to the liquor in an amount sufficient to form an azeotrope with all of the toluene present in the mixture. The methanol is added in an amount of at least about 2.62, typically an excess amount of about 3.4 to about 6.3 parts by weight of methanol per 1.0 part by weight of toluene. The resulting azeotrope of methanol and toluene is then separated by distillation from the MIBK. The methanol may be subsequently recovered from the toluene by extraction with water. Other toluene azeotrope formers may be utilized.

Abstract: A method for separating and recovering hydroquinone which comprises distilling a by-product-containing acid-cleavage product, which is obtained by acid-cleavage of an oxidation product of para-diisopropyl benzene in a solvent, in the presence of an aromatic hydrocarbon, thereby removing low-boiling fractions including the solvent, bringing the resulting hydroquinone-containing distillation bottoms into contact with water, and crystallizing and separating hydroquinone; characterized in thatA. the distilling off of the low-boiling fractions is effected without the addition of water and in the absence of an azeotropic amount of water and also in the presence of an aromatic hydrocarbon containing 9 to 10 carbon atoms, andB. the contacting of the distillation bottoms with water is effected under conditions which do not induce crystallization of hydroquinone in the distillation bottoms.

Abstract: Methyl tertiary butyl ether may be recovered from etherification reaction effluent by azeotropic distillation to recover methanol-ether azeotrope overhead which latter is azeotropically distilled in the presence of n-pentane to give pure ether bottoms substantially free of water and methanol.