Abstract: A process for recovering 1,3-butadiene from a C4 fraction, where the butadiene extraction processes may be operated at an intermediate pressure using a liquid ring type compressor. The use of a liquid ring compressor, among other process options presented herein, may advantageously reduce capital and operating costs, similar to the compressorless option, while mitigating the risks associated with the higher operating temperatures and pressures associated with the compressorless option. Thus, the embodiments of the processes disclosed herein encompass the best features of the conventional design (low pressure, with a compressor) with the advantages of the compressorless design (low capital and operating cost), as well as other advantages unique to the systems disclosed herein.

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 process for recovering butanol from a mixture comprising a water-immiscible organic extractant, water, butanol, and optionally a non-condensable gas, is provided. The butanol is selected from 1-butanol, 2-butanol, isobutanol, and mixtures thereof. The extractant comprises at least one solvent selected from the group consisting of C7 to C22 fatty alcohols, C7 to C22 fatty acids, esters of C7 to C22 fatty acids, C7 to C22 fatty aldehydes, and mixtures thereof.

Abstract: Continuous method for the esterification of free fatty acids in plant and animal fats with alcohols using a heterogenic acid catalyst.

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: Brominated polybutadiene polymers are recovered from a bromination reaction solution by forming the solution into droplets, thermally stripping the solvent from the droplets, and then washing the resulting particles. The washed particles are then recovered from the washing liquid. The droplets can be dispersed into a gaseous medium such as air and then transferred into a nonsolvent liquid for washing, or can be formed directly into the nonsolvent liquid. The process forms a particulate polymer material that is easily filterable and has low levels of volatile impurities and inorganic salts. Brominated polybutadiene polymers recovered in this manner are often very thermally stable.

Abstract: A method of treating a coal-derived liquid byproduct from a coal gasification process includes subjecting the coal-derived liquid to a vacuum distillation process, thereby separating the coal-derived liquid into condensed gas and coal-derived liquid bottoms. The coal-derived liquid bottoms are mixed with a bottoms solvent capable of dissolving the coal-derived liquid bottoms. The solvent/bottoms mixture is introduced along with a linear chain hydrocarbon solvent into a liquid extractor. The Raffinate is separated from the solvent for the coal-derived liquid/bottoms mixture, thereby producing in a heavy extract. The condensed gas is subjected to atmospheric distillation producing a bottoms fraction and another condensed fraction. The bottoms fraction may be used as fuel or for diesel fuel production. The condensed fraction is extracted with a linear hydrocarbon solvent in an extractor to produce light neutral oil and a Raffinate which is a cresylic acid feed stock.

Abstract: A method for removing hydrocarbon impurities from acetic acid is disclosed. The method comprises extracting acetic acid with a hydrophilic imidazolium salt. The imidazolium salt preferably has the general structure of wherein X? is a counter ion and R1, R2, R3, R4, and R5 are independently selected from the group consisting of C1-C6 hydrocarbon substitutes. The method is useful for removing hydrocarbon impurities from the alkane distillation bottoms stream of a methanol carbonylation process.

Abstract: Brominated polybutadiene polymers are recovered from a bromination reaction solution by forming the solution into droplets, thermally stripping the solvent from the droplets, and then washing the resulting particles. The washed particles are then recovered from the washing liquid. The droplets can be dispersed into a gaseous medium such as air and then transferred into a nonsolvent liquid for washing, or can be formed directly into the nonsolvent liquid. The process forms a particulate polymer material that is easily filterable and has low levels of volatile impurities and inorganic salts. Brominated polybutadiene polymers recovered in this manner are often very thermally stable.

Abstract: A method for the separation and purification of an aqueous mixture of main components, namely acetic acid and formic acid and non-volatiles by extraction, uses a solvent in a circulatory system. A raffinate stream is mixed with the larger proportion of water from a solvent stripper column (11) for the removal of water. The extraction stream is introduced into a solvent distillation column (8), from which in a first step involving the use of a mixture (A) containing a larger proportion of the solvent is separated out via a header and a mixture (B) of formic acid, water and solvent is separated out via a side offtake and a mixture (C) of acetic acid and non-volatiles is also separated out. A mixture (B) is introduced into a formic acid distillation column (4) for further processing, and a mixture (C) is introduced into an acetic acid distillation column (5), and purified acetic acid is subsequently isolated in the acetic acid distillation column (5) from the header.

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: 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: 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 pre-treating a spent caustic stream prior to oxidation which includes countercurrent multi-stage elevated temperature solvent extraction of dissolved organic material from the spent caustic using a solvent to yield a spent caustic raffinate containing only residual amounts of organic solute and steam distilling the spent caustic raffinate to remove the residual organic solutes, yielding a pretreated spent caustic stream substantially free of organic material which is then subjected to wet air oxidation and thereafter to ozonolysis to yield a wastewater stream having a low COD and BOD, which is neutralized to a pH of 8.5 to 9.0.

Abstract: An improved process is provided for the recovery of catalyst components from oligomeric impurities which are formed during the industrial preparation of 2,5-dihydrofuran by the catalytic isomerization of vinyl oxirane followed by an essential separation of the oligomeric by-products which otherwise cause deactivation of the catalyst. The catalyst components consist essentially of (a) an onium iodide and (b) a Lewis acid selected from the group consisting of the chloride, bromide or iodide of the metals zinc, tin, cobalt and bismuth, preferably zinc, where the catalyst optionally includes a donor ligand.

Abstract: The invention concerns a process for preparing a tertiary alkyl ether product. The process comprises reacting the isoolefins of an olefinic hydrocarbon feedstock in a reaction zone (1-3) with an alkanol to form a reaction mixture, which is subjected to distillation in a first distillation zone (4). The bottoms product of the first distillation contains the ether(s), whereas the overhead stream contains unreacted alkanol and a mixture of light hydrocarbons. The overhead stream is subjected to a second distillation in a second distillation zone (15). The overhead product of the second distillation mainly contains the lightest hydrocarbons and a small amount of alkanol, and the bottoms product contains an essentially oxygenate-free hydrocarbon stream which can be used as such for alkylation. In order to increase the conversion of the process, a side drawoff is withdrawn from the second distillation zone (15) and recirculated to the reaction zone (1-3).

Abstract: A process for pretreating a spent caustic stream prior to oxidation includes countercurrent multi-stage elevated temperature solvent extraction of dissolved organic material from the spent caustic using a solvent to yield a spent caustic raffinate containing only residual amounts of organic solute. The raffinate is steam distilled to remove the residual organic solutes, yielding a pretreated spent caustic stream substantially free of organic material. The pretreated spent caustic is suitable for use in a Kraft paper process or for oxidation prior to recycle or disposal. Solvent extract from the extractor is regenerated in a solvent regenerator having an overhead stream for purging light ends, a bottom stream for purging heavy ends, and a heart-cut side stream for recycling solvent to the extractor.

Abstract: Methyl tertiary butyl ether is prepared from contaminated TBA by reactively distilling the contaminated TBA in a reactive distillation column to provide a lower boiling isobutylene fraction and a higher boiling aqueous TBA fraction, by distilling the higher boiling aqueous TBA fraction to provide a lower boiling TBA fraction, by charging the lower boiling isobutylene fraction, the lower boiling tertiary butyl alcohol fraction and methanol to an etherification reactor to form an etherification reaction product, by distilling the etherification reaction product to provide a lower boiling fraction containing isobutylene, methanol and methyl tertiary butyl ether by charging the lower boiling fraction to a finishing reactor to react the isobutylene and methanol contained therein to from additional MTBE and by recovering MTBE from the etherification reaction product and the isobutylene conversion product.

Abstract: A process for removing dienes from etherification uses a hydrogenation zone in the reactor distillation column above the etherification zone. MTBE is produced and the unreacted C.sub.4 stream is also subjected to selective hydrogenation of the butadiene contained in the C.sub.4 feed stream. The C.sub.4 stream is first contacted with methanol in the etherification zone where the MTBE is distilled downward. The unreacted C.sub.4 's then are subjected to selective hydrogenation in the hydrogenation zone where butadiene in the overhead raffinate is reduced by over 90%. The hydrotreated C.sub.4 's are thus suitable for cold acid alkylation or other use wherein butadiene is harmful.

Abstract: In the multistage distillation of a methyl tertiary butyl ether reaction product comprising methyl tertiary butyl ether, tertiary butyl alcohol, methanol, isobutylene and water, the methyl tertiary butyl ether reaction product is separated in a primary methyl tertiary butyl ether distillation column into a lower boiling methyl tertiary butyl ether fraction and a higher boiling aqueous tertiary butyl alcohol fraction; the lower boiling aqueous tertiary butyl alcohol fraction is separated in a tertiary butyl alcohol distillation column into a vaporized overhead tertiary butyl alcohol fraction and a higher boiling water fraction; cooling water is charged to the reflux condenser for the tertiary butyl alcohol distillation column to liquify the vaporized, overhead tertiary butyl alcohol fraction and to convert the cooling water to wet steam, and the wet steam is independently charged to the reboiler for the primary methyl tertiary butyl ether distillation zone to supply the heat necessary for the distillation to b

Abstract: Process equipment is provided for separating ether, alcohol and hydrocarbon components from various etherifications of C.sub.4 or C.sub.5 isoolefins with an alcohol such as methanol or ethanol, and wherein identical process vessels are utilized for recovery of MTBE, ETBE, TAME, or TAEE. In use the process vessels are serially arranged in three zones. The first zone includes a first water wash vessel followed by a first fractionator and provides the ether product, the second zone includes a second wash vessel followed by a hydrocarbon stripper and recovers a stabilized hydrocarbon stream, the third zone includes a second fractionator which recovers an alcohol suitable for recycling.

Abstract: Purified propylene oxide is recovered from an impure propylene oxide feedstock contaminated with more than 50 ppm of six carbon atom hydrocarbon impurities by a solvent extraction process wherein:an impure propylene oxide feedstock is charged to a liquid/liquid extraction zone and contacted therein with an extractant consisting essentially of water and a paraffinic hydrocarbon containing 8 to 10 carbon atoms, and resolved therein into a raffinate consisting essentially of an aqueous solution of propylene oxide and into an extract comprising the paraffinic hydrocarbon and the 6 carbon atom impurities initially present in the propylene oxide feedstock.

Abstract: A process for removing dimethyl ether (DME) and methanol impurities from C.sub.4 hydrocarbon stream without substantial loss of C.sub.4 hydrocarbons by fractionating a C.sub.4 hydrocarbon stream containing DME and methanol at low levels, e.g., less than 5 wt. % to produce an overhead of about 20 to 40 volume % of the C.sub.4 stream, condensing the overhead, contacting the condensed overhead with about 1 to 5 volumes of water, thereby removing a portion of the DME and methanol from the C.sub.4 stream, returning substantially all of the C.sub.4 stream, except the small amount solubilized in the water, to the fractionation and flashing the solubilized DME and hydrocarbons from the water. The fractionation and extraction are preferably carried out at elevated pressures, e.g., 200 to 300 psig to avoid refrigeration of the overhead condensation. The flashing of the DME and hydrocarbons is carried out by reducing the pressure on the water, e.g. atmospheric pressure at a temperature in the range of 20.degree. C.

Abstract: Apparatus for the manufacture and recovery of alkali-metal tetraorganylborates. A mixed solvent and liquid/liquid contactor configuration is used in the system which aids in the recovery of the product.

Abstract: In the method for the production of an aromate concentrate suitable for use as blending component for gasifier fuel, feed hydrocarbon mixtures having boiling ranges substantially between 40.degree. and 170.degree. C., are subjected, without any previous separation into individual fractions, to an extractive distillation employing N-substituted morpholine, substituents of which display no more than seven C-atoms, as selective solvent. Herewith, the lower boiling non-aromates with a boiling range up to about 105.degree. C., practically completely, and most of the higher boiling non-aromates with a boiling range between about 105.degree. and 160.degree. C., are recovered as raffinate, whereas the aromates, which are to be employed in whole or in part as blending component, come down in the extract of the extractive distillation.

Abstract: Crude phenol, containing AMS by-product, and MBF impurity, is distilled in the presence of water to separate MBF impurity.

Abstract: A process for purifying diethoxymethane from a mixture containing ethanol and, optionally, water. The process involves the addition of an amount of water, DEM, or an appropriate mixture of any two or three of water, DEM and ethanol that is effective in moving the mixture into the two liquid phase region on an equilibrium tie-line which crosses the critical distillation boundary without the need for additional azeotrope-forming agents such as cyclohexane.

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: A process for separating a butene-1/isobutene mixture from a C.sub.4 hydrocarbon fraction is provided which comprises subjecting the C.sub.4 hydrocarbon fraction to extractive distillation using a polar solvent to separate components predominantly containing 1,3-butadiene as an extract and obtain an overhead containing butanes, butene-1, isobutene and butene-2 as main components and being substantially free from C.sub.3 -C.sub.4 diolefinic and acetylenic hydrocarbons, feeding the overhead into a first distillation column, removing isobutane as an overhead component from the first distillation column, feeding high-boiling components from the bottom of the first distillation column to a second distillation column, removing n-butane and butene-2 from the bottom of the second distillation column, and obtaining highly pure butene-1 and isobutene from its top.

Abstract: A process for separating a butene-1/isobutene mixture from a C.sub.4 hydrocarbon fraction is provided which comprises subjecting the C.sub.4 hydrocarbon fraction to extractive distillation using a polar solvent to separate components predominantly containing 1,3-butadiene as an extract bottom and obtain an overhead containing butanes, butene-1, isobutene and butene-2 as main components and being substantially free from C.sub.3 -C.sub.4 diolefinic and acetylenic hydrocarbons, feeding the overhead into a first distillation column, removing n-butane and butene-2 as bottoms from the column, feeding low-boiling components from the top of the column into a second distillation column, removing isobutane from the top of the second distillation column, and obtaining highly pure butene-1 and isobutene from its bottom.

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: In the production of high purity phenol, a water-phenol mixture recovered from the top of a distillation column is contacted with a water immiscible solvent to extract methyl benzofuran and other by-products and impurities in phenol production therefrom, with the extraction being accomplished at a temperature at which the water-phenol mixture is present as a single phase liquid. The remaining mixture of phenol and water is recycled to the distillation.

Abstract: A process for producing gasoline-ethanol blends comprises purifying dilute ethanol by extractive distillation and concentrating the ethanol by distillation followed by one or both of the following steps: (a) liquid extraction of ethanol into heated gasoline or (b) azeotropic distillation of ethanol with an entrainer followed by blending with gasoline.

Abstract: Methylnaphthalenes, indole and other tar bases are recovered from a base-extracted coal tar distillation fraction. In one form, an aqueous salt solution of pH 0.5-3 extracts other tar bases from the starting material, and thereafter both products are recovered from the raffinate by several alternate methods including ethylene glycol extraction and extractive distillation. In other forms, the starting material is extracted with ethylene glycol and the extract is distilled to recover several products including indole. The raffinate of ethylene glycol extraction contains methylnaphthalenes and other hydrocarbons and can be purified to solvent-grade material.

Abstract: A process for dehydrating an essentially one-phase wet solvent stream obtained in a solvent dewaxing-solvent deoiling process, which solvent stream contains at least 60% toluene with the balance being water and methyl ethyl ketone (hereinafter MEK), is dehydrated by (a) fractionally distilling to produce a bottom fraction of anhydrous MEK-toluene solvent and an overhead fraction containing all the water originally present in the wet solvent stream; (b) condensing and separating said overhead fraction into a toluene-containing, water-lean phase, which is used as reflux in step (a), and a toluene-free, MEK-containing, water-rich phase; (c) extracting into a hydrocarbon stream some MEK from said water-rich phase and from the condensed azeotropic mixture recycled from step (g) hereinafter; (d) recovering from step (c) a second water-rich stream, which water-rich stream contains the MEK not extracted into said hydrocarbon stream; (e) azeotropically distilling said second water-rich stream so as to obtain water as

Abstract: A process for preparing a purified methacrylic acid ester from a crude methacrylic acid ester containing an isobutyric acid ester as an impurity, comprising the steps of azeotropically distilling the crude methacrylic acid ester in the presence of water to separate as the top distillate the isobutyric acid ester and water together with a small amount of the methacrylic acid ester and recover as the bottoms the greater part thereof, separating the distillate into aqueous and organic phases and further azeotropically distilling the separating organic phase in the presence of water to separate as the distillate the isobutyric acid ester and water together with a very small amount of the methacrylic acid ester and recover as the bottoms the remainder thereof, thereby obtaining the purified methacrylic acid ester.

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: An improvement is described on a process for recovery of butadiene from a C.sub.4 hydrocarbon mixture additionally containing minor amounts of C.sub.5 saturated and unsaturated hydrocarbons, said hydrocarbon mixture being obtained as the overhead product of an initial hydrocarbon fractionation employed to separate larger quantities of C.sub.5 and heavier hydrocarbons from the hydrocarbon mixture, wherein the hydrocarbon mixture is subject to extractive distillation in the presence of a polar solvent e.g. acetonitrile, in which butadiene is separated from the fat solvent bottoms of extractive distillation by sequential low pressure flashing and stripping, followed by compression of the combined vapors of flashing and stripping with part of the compressed vapors being recycled as reboiled vapor to the extractive distillation and the remainder being again stripped at a higher pressure to recover butadiene therefrom. In this improved process, butadiene purification problems associated with carry over of C.sub.

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.