Abstract: Process for working up a bottom stream wherein high boilers and ionic liquid from an extractive rectification in which the ionic liquid is used as entrainer. The process includes feeding the bottom stream to an evaporation stage which is operated at a pressure of less than 500 mbar or to a stripper which is operated through use of inert gas or steam, and the major part of the high boiler present is separated off in vapor form from the ionic liquid.

Abstract: A process for debottlenecking a system for the separation of a conjugated diolefin the system including a first extraction section having an extractive distillation column and a stripping column and a second extraction section. The process includes the steps of withdrawing a first portion of an extract from the extractive distillation column, the extract having at least the first portion and a second portion, and transferring the first portion of the extract to a flash/separation vessel; separating the first portion of the extract into a vapor phase and a liquid phase by flashing in a flash/separation vessel; and combining the liquid phase of the separated first portion of the extract with the second portion of the extract to produce an extract feed for further processing. A system and process for the separation of a conjugated diolefin from a C4- or C5-hydrocarbon mixture containing the conjugated diolefin and higher acetylenes are also provided.

Abstract: A process for reacting a first component with itself or a second component to produce a third component in which a first material comprising a first component or said first component and a second component is fed to divided wall column having a catalytic distillation structure in at least one of the separate vertical sections of the divided wall column where concurrently: (1) a first component alone or with a second component is contacted with a catalytic distillation structure in a distillation reaction zone thereby catalytically reacting at least a portion of the first component with itself or with the second component to form a product and (2) a first mixture comprising the first component and the product or the first component, the second component and the product; and withdrawing the product from the distillation column reactor; while within the column concurrently with the catalytic reaction and fractionation a second mixture is fractionated, which contains the first component and the product or first a

Abstract: A novel method for connecting multiple existing columns which are retrofitted into vapor-liquid contacting devices with trays or packings suitable for the operation of a three-phase (vapor-liquid-liquid) extractive distillation column for aromatics recovery. The retrofitted columns are connected by a vapor transfer line to transfer the vapor phase from the top of the lower column to the bottom of the upper column, and by a liquid transfer line to transfer the liquid phase from the bottom of the upper column to the top of the lower column of the three-phase extractive distillation column.

Abstract: A method for the solvent extraction recovery of an aromatic wherein an aromatic extract is formed that contains the aromatic and non-aromatics that are both lighter than and heavier than the aromatic, analyzing at least two separate groups of lighter and heavier non-aromatics in the extract, determining from the analyses the distribution of lighter and heavier non-aromatics present and whether the aromatic product that will be recovered from the process will be too far from its predetermined maximum non-aromatic content specification, and making process changes that will cause the process to produce the aromatic product with a non-aromatic content that is closer to its predetermined maximum non-aromatic content specification.

Abstract: A liquid phase process is disclosed for producing halogenated alkane adducts of the formula CAR1R2CBR3R4 (where A, B, R1, R2, R3, and R4 are as defined in the specification) which involves contacting a corresponding halogenated alkane, AB, with a corresponding olefin, CR1R2?CR3R4 in a dinitrile or cyclic carbonate ester solvent which divides the reaction mixture into two liquid phases and in the presence of a catalyst system containing (i) at least one catalyst selected from monovalent and divalent copper; and optionally (ii) a promoter selected from aromatic or aliphatic heterocyclic compounds which contain at least one carbon-nitrogen double bond in the heterocyclic ring. When hydrochlorofluorocarbons are formed, the chlorine content may be reduced by reacting the hydrochlorofluorocarbons with HF. New compounds disclosed include CF3CF2CCl2CH2CCl3, CF3CCl2CH2CH2Cl and CF3CCl2CH2CHClF. These compounds are useful as intermediates for producing hydrofluorocarbons.

Abstract: A process for recovering crude 1,3-butadiene from a C4 fraction by extractive distillation using a selective solvent in a dividing wall column (TK) in which a dividing wall (T) is arranged in the longitudinal direction of the column to form a first subregion (A), a second subregion (B) and a lower common column region (C) and which is preceded by an extractive scrubbing column (K) is proposed.

Abstract: Process for producing a nitric acid of a concentration from 75 to 99.9% from a more diluted nitric acid, wherein a nitric acid of a concentration of about 45 to 70% is rectified in contact with a liquid extraction medium to prevent the formation of a nitric acid-water-azeotropic mixture, and the vapors of the concentrated nitric acid are condensed and a concentrated nitric acid is obtained and wherein additionally the extraction medium is reconstituted through reconcentration and returned into the extractive rectification, wherein the nitric acid to be concentrated is fed as a boiling liquid or partially vaporized to the extractive rectification preferably carried out in two columns (K 1.0, K 1.

Abstract: There is provided an azeotropic mixture having 1,1,1,3,3-pentafluoropropane and hydrogen fluoride. Further, there is provided a process of separating/purifying R-245fa and/or HF from a mixture of R-245fa and HF wherein the mixture of 1,1,1,3,3-pentafluoropropane and hydrogen fluoride is subjected to a distillation step so that a distillate is obtained which has the azeotropic mixture of 1,1,1,3,3-pentafluoropropane and hydrogen fluoride, and a bottom product is obtained which has separated/purified 1,1,1,3,3-pentafluoropropane or hydrogen fluoride.

Abstract: The invention relates to azeotropic and azeotrope-like mixtures of 1,1,1,3,3-pentafluorobutane (HFC-365) and hydrogen fluoride and a process for separating the azeotrope-like mixtures. The compositions of the invention are useful as an intermediate in the production of HFC-365. The latter is useful as a nontoxic, zero ozone depleting fluorocarbon useful as a solvent, blowing agent, refrigerant, cleaning agent and aerosol to propellant.

Abstract: A process for recovering crude 1,3-butadiene from a C4 fraction by extractive distillation using a selective solvent in a dividing wall column (TK) in which a dividing wall (T) is arranged in the longitudinal direction of the column to form a first subregion (A), a second subregion (B) and a lower common column region (C) and which is preceded by an extractive scrubbing column (K) is proposed.

Abstract: A process is described for preventing plugging of distillation equipment when the distillable liquid comprises a mixture of different liquids containing a dissolved substance tending to precipitate from the distillate. An adjuvant is provided to the mixture to be distilled, which adjuvant forms a composition with the dissolved substance that, if isolated, melts at a lower temperature than the distillation temperature.

Abstract: The present invention involves processes that utilize an olefinic compound, in particular, hexafluoropropene (HFP) or chlorotrifluoroethene (CFC-1113) as extracting agents in the purification of pentafluoroethane (HFC-125). These processes can utilize recovered HFP as a precursor for the production of heptafluoropropane (HFC-227) or other derivatives.

Abstract: The invention relates to a rectifying column for extractive distillation, comprising a column main section (204) and a raffinate section (205) above said main section, an evaporator (208) situated on the lower end of the column, an inlet (214) disposed between the main section of the column and the raffinate section and a solvent inlet (215) arranged on the top side of the raffinate section (205) for feeding an extracting agent. According to the invention, the main section (204) has two chambers (216, 217) connected in parallel. A stripping section (222) is disposed between the bottom of the column (221) and the main section (204), in which concentration of the extracting agent occurs from the top down. The bottom (221) is connected to the solvent inflow (215) by a device (223) for recycling the extracting agent.

Abstract: A method for isolating 32 from a crude mixture containing HCl and an azeotropic mixture of 32 and HF is provided without the need to isolate any HF azeotrope.

Abstract: An apparatus for producing phenol and acetone from cumene hydroperoxide comprises a reactive distillation column comprising at its upper portion a distillation column and at its lower portion a catalyst bed.

Abstract: The present invention aims to isolate the azeotropes formed in a distillation column (B1) by methanol, propane and butane. The azeotropes are then liquefied in heat exchanger (E2) and mixed in contactor (M1) with water in order to dissolve the methanol in water. The mixture is then fed into a decantation tank (D2) to separate the aqueous phase from the liquid hydrocarbon phase. Finally, an aqueous phase containing methanol is discharged and the methanol-depleted hydrocarbon phase is recycled to distillation column (B1) as reflux.

Abstract: A process for refining difluoromethane by removing hydrogen fluoride, which is contained in difluoromethane difficult to remove. The process involves distilling a mixture of difluoromethane with hydrogen fluoride where the mixture is in contact with sulfuric acid. The hydrogen fluoride remains in the liquid phase and the difluoromethane goes into the vapor phase.

Abstract: A method for separating an oxidation catalyst, an oxidation reaction product and a reaction solvent from a reaction mixture obtained by oxidizing a substrate in the presence of an oxidation catalyst containing an aromatic N-hydroxyimide compound and a transition metal, the method including (i) distilling the reaction solvent from the reaction mixture in the presence of an organic solvent which is immiscible with the reaction solvent to obtain the reaction mixture containing the reaction solvent in an amount of 5 parts by weight or less per one part by weight of the N-hydroxyimide compound, and the oxidation catalyst precipitated, and (ii) separating the reaction mixture obtained in the step (i) by a solid-liquid separation method into the oxidation product and the oxidation catalyst.

Abstract: A waste photopolymer plate washout fluid solvent distillation apparatus includes a single enclosure enclosing a waste washout fluid container, a recovered solvent container, and a distillation unit in which waste washout is distilled by application of heat and vacuum pressure to the waste washout, and by supplying a metered supply of a surrogate solvent to the distilled waste washout as a desired solvent is distilled from the waste washout. The apparatus, by supplying the surrogate solvent to the waste washout as the desired solvent is distilled from the waste washout, enables a greater percentage of the desired solvent to be recovered from the waste washout than has been heretofore possible with prior art apparatus, and also enables the waste washout to be disposed of as a liquid.

Abstract: A process is disclosed for producing compositions including (a) a compound selected from the group consisting of CHF2CF3, CHF2CHF2, CH2FCF3, CH3CF3, CH3CHF2, CH2FCF2CHF2 and CHF2CF2CF2CHF2 and (b) at least one saturated halogenated hydrocarbon and/or ether having the formula: CnH2n+2−a−bClaFbOc wherein n is an integer from 1 to 4, a is an integer from 0 to 2n+1, b is an integer from 1 to 2n+2−a, and c is 0 or 1, provided that when c is 1 then n is an integer from 2 to 4, and provided that component (b) does not include the selected component (a) compound, wherein the molar ratio of component (b) to component (a) is between about 1:99 and a molar ratio of HF to component (a) in an azeotrope or azeotrope-like composition of component (a) with HF.

Abstract: The disclosure relates to removing impurities from hexafluoroethane (CF3CF3), also known as Perfluorocarbon 116 (PFC-116) or Fluorocarbon 116 (FC-116), by using azeotropic distillation such that an overhead product consisting essentially of HCl-hexafluoroethane is formed, optionally combined with a phase separation step to break the HCl-hexafluoroethane azeotropic or azeotrope-like composition thereby permitting recovery of substantially pure hexafluoroethane. Unreacted hydrogen fluoride (HF) may be removed from hexafluoroethane during the above azeotropic distillation with HCl or alternatively by an azeotropic distillation wherein an HF-hexafluoroethane azeotropic or azeotrope-like composition exits overhead and substantially pure HF exits in the bottoms stream.

Abstract: The divinyl ethers of diethylene glycol or triethylene glycol are separated from the monovinyl ether of the corresponding oligoethylene glycol by distillation, a metal hydroxide being added to the vinyl ether mixture.

Abstract: Propylene oxide obtained by an epoxidation process which uses methanol as a solvent may be effectively treated to remove acetaldehyde by subjecting the crude epoxidation reaction product to fractional distillation. The methanol solvent is utilized during such distillation to lower the relative volatility of the acetaldehyde impurity, thereby making it possible to obtain a bottoms fraction containing substantially all the acetaldehyde. Purified propylene oxide having a reduced acetaldehyde concentration is removed as an overhead stream. Water may also be effectively separated from the propylene oxide using this procedure.

Abstract: A process is disclosed for the monohydrogenolysis of 2,2-dichlorohexafluoropropane to 2-chloro-2-hydrohexafluoropropane. The process involves reacting the 2,2-dichlorohexafluoropropane with hydrogen at an elevated temperature of about 150.degree. C. or less in the presence of a catalyst containing a catalytically effective amount of palladium supported on trivalent chromium oxide in the presence of an acid of the formula HZ (where Z is Cl and/or F) to produce 2-chloro-2-hydrohexafluoropropane with a selectivity of over 70% based upon the 2,2-dichlorohexafluoropropane converted. Azeotropes of 2-chloro-2-hydrohexafluoropropane with HF are also disclosed; as are processes for producing such azeotropes.

Abstract: A process for separating HCl from pentafluoroethane, chloropentafluoroethane, chlorotrifluoroethane, trifluoromethane, and other fully saturated and unsaturated fluorocarbons, chlorofluorocarbons and chlorocarbons.

Abstract: The disclosure relates to removing impurities from hexafluoroethane (CF.sub.3 CF.sub.3), also known as PerFluoroCarbon 116 (PFC-116) or FluoroCarbon 116 (FC-116), by using azeotropic distillation such that an overhead product containing an HCl-hexafluoroethane is formed, optionally combined with a phase separation step to break the HCl-hexafluoroethane azeotropic or azeotrope-like composition thereby permitting recovery of substantially pure hexafluoroethane. Unreacted hydrogen fluoride (HF) may be removed from hexafluoroethane during the above azeotropic distillation with HCl or alternatively by an azeotropic distillation wherein an HF-hexafluoroethane azeotropic or azeotrope-like composition exits overhead and substantially pure HF exits in the bottoms stream.

Abstract: A process for treating C.sub.3 to C.sub.12 petroleum fractions, such as a light cracked naphtha to be used as an etherification feed stock in which H.sub.2 S is removed by distillation of at least the C.sub.3 fraction and mercaptans and diolefins are removed simultaneously in a distillation column reactor using a dual catalyst bed. The mercaptans and H.sub.2 S are reacted with the diolefins in the presence of a reduced nickel catalyst to form sulfides which are higher boiling than the portion of the feed which is fractionated to an upper hydrogenation catalyst bed of palladium for hydrogenating diolefins and acetylenes. The higher boiling sulfides are removed as bottoms along with heavier materials. Any diolefins not converted to sulfides and acetylenes are selectively hydrogenated to mono-olefins in the presence of a palladium oxide catalyst in an upper bed, producing overheads, substantially free of sulfur compounds, diolefins and acetylenes.

Abstract: Hydrogen fluoride is effectively removed from a mixture of hydrogen fluoride, dichloromethane, chlorofluoromethane and/or difluoromethane by distilling the mixture so that two-component azeotropic mixtures of hydrogen fluoride and dichloromethane, hydrogen fluoride and chlorofluoromethane and hydrogen fluoride and difluoromethane are removed, or by liquid-separating the mixture into an upper liquid phase rich in hydrogen fluoride and a lower liquid phase not rich in hydrogen fluoride before each liquid phase is distilled as described above.

Abstract: A method for the separation and recovery of volatiles from a sludge containing about 1 to 80% by weight liquid solvents and 20 to 99% by weight solids, in which said sludge is fed with a reagent powder material in an amount effective to form a mixture having a high surface area to a distillation vessel, said mixture is heated to a temperature up to about 350.degree. C. while said mixture is advanced through the vessel for a time sufficient to distil a sufficient portion of the solvents to yield a solid residue powder, distilled solvents are condensed, and the solid residue powder recovered. The vessel preferably is a mechanical fluidized bed distillation vessel and said mixture is fluidized while being heated therein under a partial vacuum in a non-oxidizing atmosphere. The effective amount of reagent powder material includes about 5 to 70 wt % of the reagent powder material.

Abstract: m-Xylene is very difficult to separate from mixtures of p-xylene and o-xylene by conventional distillation or rectification because of the proximity of their boiling points. m-Xylene can be readily separated from p-xylene and mixtures of p-xylene and o-xylene by azeotropic distillation. An effective agent is tetraethyl ortho silicate.

Abstract: Ethanol is difficult to separate from isopropanol by conventional distillation or rectification because of the proximity of their boiling points. Ethanol can be readily separated from isopropanol by extractive distillation. Effective agents are dipentene, anisole and ethyl benzene.

Abstract: Hydrogen fluoride and 1,1,1-trifluoro-2-chloroethane forms an azeotropic mixture of which molar ratio of HF/1,1,1-trifluoro-2-chloroethane varies, for example, from about 60/40 at a pressure of 1.5 Kg/cm.sup.2 G and a temperature of 20.degree. C. to about 45/55 at a pressure of 15 Kg/cm.sup.2 G and a temperature of 87.degree.C.

Abstract: Phenol plant waste water containing small amounts of phenol and sodium sulfate is successfully distilled through the addition of recovered sodium sulfate to enhance the volatility of the phenol relative to water; at least a portion of the sodium sulfate is recycled, while a significant portion of the phenol can be returned to the phenol plant for recovery.

Abstract: A waste photopolymer plate washout fluid solvent distillation apparatus includes a single enclosure enclosing a waste washout fluid container, a recovered solvent container, and a distillation unit in which waste washout is distilled by application of heat and vacuum pressure to the waste washout, and by supplying a metered supply of a surrogate solvent to the distilled waste washout as a desired solvent is distilled from the waste washout. The apparatus, by supplying the surrogate solvent to the waste washout as the desired solvent is distilled from the waste washout, enables a greater percentage of the desired solvent to be recovered from the waste washout than has been heretofore possible with prior art apparatus, and also enables the waste washout to be disposed of as a liquid.

Abstract: A method of distillation employing a heat pump (which may be driven by a compressor) using a vapor stream from within the distillation system as a heat source and a liquid stream from within the distillation system as a heat sink. The selection of heat-source vapors and heat-sink liquid is such that at least one is withdrawn from the phase-contracting region of the distillation system. The return of streams withdrawn from the phase-contacting region of the distillation system to the distillation system is such that at least one of the streams is returned at a temperature different from that of the point from which it was withdrawn, and all withdrawn streams are returned in manner such that a stream removed as vapor is returned at a point with a temperature at most that at the point it was withdrawn, and a stream removed as liquid is returned at a point with a temperature at least that at which it was withdrawn.

Abstract: A vacuum drying method wherein a solution of a material to be dried which has been adjusted to 1-50 centipoise, is supplied to a steam-heated long tube, solid-vapor mixture of powdery dry material and vapor produced in the tube is blown out under reduced pressure, and the powdery dry material and vapor are separated so as to obtain powdery dry material.

Abstract: A vacuum draft submerged combustion system and method for separating combustible hydrocarbons and other components or liquid solutions from their solvents, usually water, includes evaporating volatile components by a submerged combustion burner and condensing the vaporized volatile components under a partial vacuum. The hot gases from the burner are injected under partial vacuum into the first tank. The hot gases bubbled through the solution cause volatile components in the liquid to be evaporated and collected above the level of the liquid. The collected gasses are drawn into a condensing tank where the condensable particulates are condensed and collected.

Abstract: 1,1-Dichloro-1-fluoroethane, 1-chloro-1,1-difluoroethane and hydrogen fluoride are separated from their liquid mixtures, such as liquid mixtures resulting from the hydrofluorination, of 1,1,1-trichloroethane or vinylidene chloride. 1,1-Dichloro-1-fluoroethane and 1-chloro-1,1-difluoroethane are first separated by distillation into their respective mixtures with hydrogen fluoride, which are thereafter subjected to parallel phase separations resulting in two hydrogen fluoride-enriched liquid phases, a 1-chloro-1,1-difluoroethane-enriched liquid phase and a 1,1-dichloro-1-fluoroethane-enriched liquid phase. 1-Chloro-1,1-difluoroethane and 1,1-dichloro-1-fluoroethane are purified from the respective halohydrocarbon-enriched liquid phases by distillation. The hydrogen fluoride-enriched stream generated from the phase separation of the hydrogen fluoride/1,1-dichloro-1-fluoroethane mixture is recycled to the hydrofluorination reaction mixture.

Abstract: A method of distillation employing a heat pump (which may be driven by a compressor) using a vapor stream from within the distillation system as a heat source and a liquid stream from within the distillation system as a heat sink. The selection of heat-source vapors and heat-sink liquid is such that at least one is withdrawn from the phase-contacting region of the distillation system. The return of streams withdrawn from the phase-contacting region of the distillation system to the distillation system is such that at least one of the streams is returned at a temperature different from that of the point from which it was withdrawn, and all withdrawn streams are returned in manner such that a stream removed as vapor is returned at a point with a temperature at most that at the point it was withdrawn, and a stream removed as liquid is returned at a point with a temperature at least that at which it was withdrawn.

Abstract: A process for separation of components of a mixture of more than one organic substance or of a mixture of at least one organic substance and water by extraction using a supercritical fluid as an extractant. During the extraction an extraction aid having a higher affinity with an unextractable component of the mixture than with an extractable component of the mixture is present. Also disclosed is an apparatus for carrying out this process.

Abstract: 1,1-Dichloro-1-fluroethane and 1,1,1,3,3-pentafluorobutane are separated from their liquid mixtures, such as liquid mixtures resulting from the hydrofluorination of 1,1,1-trichloroethane or vinylidene chloride. 1,1-Dichloro-1-fluoroethane and 1,1,1,3,3-pentafluorobutane are completely separated by distillation, by adding to the mixture thereof a liquid containing at least about 3 moles of hydrogen fluoride per mole of 1,1-dichloro-1-fluoroethane in the mixture subject to separation.

Abstract: The invention relates to a process for obtaining trioxane from aqueous solutions by high-pressure extraction using an extracting agent which is in the form either of a gas in the supercritical state or of a liquid gas. An intermediate separation is advantageous, especially in the former case.The trioxane can be obtained in high concentration and with a saving of energy by the process according to the invention.

Abstract: The process and the device according to the invention relate to the introduction, at a stable, known flow rate, of sublimable tetrachloride into a column for continuous extractive distillation under pressure of the chlorides. The sublimable tetrachloride is dissolved in a hot dissolver in a liquid solvent such as KAlCl.sub.4, and is then recirculated by pump at a stable, known flow rate into an evaporator connected to the column. The solution is then heated in an evaporator in order to sublime the majority of the product which it contains, the sublimed vapors thus passing into the column at a stable, known flow rate. The process according to the invention is adapted, in particular, to a plant for the production of ArCl.sub.4 of nulear purity and of HfCl.sub.4.

Abstract: Removal of aluminum and iron impurities is accomplished using an absorbing column containing potassium or sodium chloride, producing an aluminum and iron chloride-rich bottoms product and purified Zr(Hf)Cl.sub.4 vapor at the top of the column. This invention is a continuous process for removing impurities of iron or aluminum chloride or both from vaporous zirconium chloride (or hafnium chloride or a mixture thereof). When iron is being removed from zirconium tetrachloride using potassium chloride, the process comprises: introducing impure zirconium chloride vapor into a middle portion of an absorbing column containing a potassium chloride-containing molten salt phase, the molten salt phase absorbing the iron chloride impurity to produce a zirconium chloride vapor stripped of iron chloride in the top portion of the column; introducing potassium chloride into a top portion of the column; controlling the top portion of the column to between 300.degree.-375.degree. C.

Abstract: This is an improved method for separating hafnium from zirconium of the type where a complex of zirconium and hafnium chlorides and phosphorus oxychloride is prepared from zirconium-hafnium chloride and the complex is introduced into a distillation column, with the improvement comprising: electrochemical breaking of the zirconium of hafnium chloride complex taken from said distillation column to separate product from the complex. The electrochemical breaking of the complex, possibly by reducing zirconium or hafnium, is done in a molten salt bath. Preferably, the molten salt in said molten salt bath consists principally of a mixture of alkali metal and alkaline earth metal chlorides and zirconium or hafnium chloride. The product can be either chloride, metal, or mixed metal and subchloride for further processing.

Abstract: This is a zirconium-hafnium separation process utilizing a complex of zirconium-hafnium chlorides and phosphorus oxychloride. The complex is introduced into a distillation column and a hafnium chloride enriched stream is taken from the top of the column and a zirconium chloride enriched stream is taken from the bottom of the column. In particular, the invention utilizes prepurification of the zirconium-hafnium chlorides prior to introduction of the complex into the distillation column to substantially eliminate iron chloride; thus, the buildup of iron chloride in the distillation column is substantially eliminated and the column can be operated in a continuous stable, and efficient manner.

Abstract: A method of separating HF from a mixture including HF and HCl is disclosed wherein the mixture is contacted with silica causing the HF to react with the silica to form SiF.sub.4. The concentration of HCl is increased thereby increasing the relative volatility of SiF.sub.4 /HCl. The SiF.sub.4 is then removed as an aqueous distillate. The concentration of the HCl can be increased by various methods including adding gaseous or concentrated HCl to the mixture or by distilling off a portion of the water to thereby increase the concentration of the HCl. This method provides an efficient method of removing SiF.sub.4 and HF from HCl.

Abstract: Isoprene is recovered from a C.sub.5 -hydrocarbon mixture containing isoprene, penta-1,3-diene and cyclopentadiene by separating the said mixture by liquid-liquid extraction or extractive distillation with the aid of a selective solvent, in combination with a distillation upstream or downstream from the liquid-liquid extraction or extractive distillation, by a method in which a stream containing penta-1,3-diene and cyclopentadiene is separated off in the upstream or downstream distillation and is catalytically hydrogenated, and the hydrogenated stream is fed to the upper part of the liquid-liquid extraction or extractive distillation.

Abstract: The invention pertains to improvements in a fluid handling system in which a working fluid passes through a rotor while undergoing a pressure change. A shaft extends longitudinally from and rotates with the rotor. A first seal surrounds the shaft in axially spaced relation to the rotor, and a lubricant having a minimum boiling point is injected into the first seal adjacent the shaft at a pressure sufficient to cause the lubricant to flow axially toward the rotor. A housing surrounds the rotor and shaft and defines a contact zone between the rotor and the first seal for receiving both lubricant and a contact fluid such as the working fluid or a seal buffer gas used to isolate the working fluid from the lubricant. The contact fluid has a maximum boiling point substantially less than the minimum boiling point of the lubricant.