Abstract: Crude ammonia is separated into a low boiler fraction, a high boiler fraction and an intermediate-boiling pure fraction by continuous fractional distillation in a distillation apparatus configured either as a dividing wall column or as a system of thermally coupled distillation columns. In the process of the present invention, the low boiler fraction is taken off at the top of the distillation apparatus. The intermediate-boiling pure fraction is obtained at a side offtake which is preferably provided with droplet precipitators. In addition, the gas loading of the distillation column is restricted so that the operating pressure is in the range from 2 to 30 bar and the F factor does not exceed 2.0 Pa0.5.

Abstract: A tert-C4–C8-alkyl (meth)acrylate is prepared by reacting (meth)acrylic acid with an olefin of the formula where R1 and R2, which may be identical or different, are methyl or ethyl and R3 is H, methyl or ethyl, in homogeneous phase in the presence of an acidic catalyst and isolating the tert-C4–C8-alkyl (meth)acrylate from the reaction mixture, by a process in which the catalyst is separated off as residue by a two-stage distillation of the reaction mixture and the tert-C4–C8-alkyl (meth)acrylate is isolated from the distillates. The novel process makes it possible to use acetic acid-containing (meth)acrylic acid. The danger of cleavage of the ester and of polymerization of (meth)acrylic compounds is reduced.

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: This invention relates to a continuous process for the preparation of silane by catalytic disproportionation of trichlorosilane in a reactive/distillative reaction zone having a catalyst bed of catalytically active solid.

Abstract: A method of separating and purifying conjugated dienes includes a step of obtaining a first bottom product by taking out a hydrocarbon mixture including conjugated diene under an environment in the presence of a polymerization inhibitor including at least one of nitrite and di-lower aklylhydroxylamine in a first extractive distillation column; a step of obtaining a second bottom product and a distillation portion by distilling the first bottom product in a first diffusion column; a step of obtaining a third bottom product by taking out the distillation portion under an environment in the presence of the polymerization inhibitor in a second extractive distillation column; a step of obtaining a fourth bottom product by distilling the third bottom product in a second diffusion column; a step of recovering the second bottom product and fourth bottom product and supplying to the first extractive distillation column and/or second extractive distillation column; a step of measuring concentration of a polymerization

Abstract: An apparatus comprising first to third columns, wherein the outlet of a first column reboiler and the inlet of a second column condenser are connected by a first introduction conduit, and the outlet of a second distillation column reboiler and the inlet of a third column condenser are connected by a second introduction conduit, and additionally the outlet of the second column condenser and the inlet of the first column reboiler are connected by a first return conduit, and the outlet of the third column condenser and the inlet of the second column reboiler are connected by a second return conduit.

Abstract: By using a dephlegmator which conducts distillation concurrently with heat exchange within at least one distillation column, or a portion of one distillation column, of a distillation cascade, the quantity of liquid holdup within the distillation apparatus is reduced and the start-up time is shortened. Consequently, the operational costs associated with startup are reduced, and productivity is improved markedly.

Abstract: To improve the columns used so far for producing phthalic anhydride, and to make them less expensive and easier to install, it is proposed that in the column for concentrating phthalic anhydride two distillation stages are arranged, wherein the removal of the low-boiling components of the crude phthalic anhydride by distillation is effected in the first distillation stage (2) and the separation of the high-boiling components from the pure phthalic anhydride is effected in the second distillation stage (3), both distillation stages being arranged side by side and being separated from each other by a vertical wall (4), and that the bottom (7) of the first distillation stage (2) is connected with the bottom (10) of the second distillation stage (3).

Abstract: A distillation apparatus includes a column body; a partition for dividing the interior of the column body; a first distillation section composed of an enriching section and an exhaust section; a second distillation section composed of an enriching section formed above an upper end of the first distillation section, and an exhaust section located adjacent to the enriching section of the first distillation section; a third distillation section composed of an enriching section located adjacent to the exhaust section of the first distillation section, and an exhaust section formed below a lower end of the first distillation section; a condenser; a negative pressure generation system for generating a negative pressure to thereby withdraw vent gas; a gas cooler for cooling the vent gas; a first discharge system disposed at the side of the column body and adapted to discharge liquid rich in a medium-boiling-point component formed from a high-melting-point material; and a second discharge system disposed at the botto

Abstract: The present invention is a distillation system with individual fractionator tray temperature control, with the use of either a heating element or a cooling element, and in some preferred embodiments, the use of both a heating element and a cooling element in a plurality of fractionator trays. There is at least, and typically more than one distillation column having a plurality of fractionation trays, and having feed input, liquid removal, and vapor removal with the plurality of trays including at least one of a heating element and a cooling element. Controls are included for separate control of each of the heating element(s) and/or said cooling element(s). These controls may be regulated by a programmable microprocessor, and feedback from temperature sensors may be employed to provide discrete tray-by-tray temperature controls.

Abstract: A heat integrated distillation column provides heat at each theoretical stage of distillation in a heating portion and coolant at each theoretical stage of distillation in a cooling portion.

Abstract: An extractive distillation tower 4 supplied with a feedstock containing butadiene and a solvent and for distilling the feedstock to separate and purify the butadiene.

Abstract: Phenol is separated from a mixture containing hydroxyacetone, cumene, water and phenol, by fractionating the mixture in a process with a fractional distillation step and a phase separation step to provide a single phenol fraction containing less than 300 ppm of hydroxyacetone. In the work-up by distillation of cleavage product mixtures, the hydroxyacetone can be removed from the cleavage product mixture together with a phenol fraction from which the hydroxyacetone has to be removed. A process can be used for purifying cleavage product mixtures obtained in the cleavage of alkylaryl hydroperoxides such as cumene hydroperoxide. The process allows separation of phenol and acetone from mixtures obtained in the cleavage of cumene hydroperoxide.

Abstract: A distillation apparatus includes a column body; a partition for dividing the interior of the column body; a first distillation section composed of an enriching section and an exhaust section; a second distillation section composed of an enriching section formed above an upper end of the first distillation section, and an exhaust section located adjacent to the enriching section of the first distillation section; a third distillation section composed of an enriching section located adjacent to the exhaust section of the first distillation section, and an exhaust section formed below a lower end of the first distillation section; a condenser; a negative pressure generation system for generating a negative pressure to thereby withdraw vent gas; a gas cooler for cooling the vent gas; a first discharge system disposed at the side of the column body and adapted to discharge liquid rich in a medium-boiling-point component formed from a high-melting-point material; and a second discharge system disposed at the botto

Abstract: The present invention is directed to an apparatus and method for the distillation of a readily polymerizable vinyl aromatic compound employing a polymerization inhibitor. The vinyl aromatic compound is subjected to distillation in at least one fractionation column having at least one reboiler for maintaining the bottoms of said column at a proper temperature. The reboiler includes a heating section and a vapor phase section. The bottoms fraction from the fractionation column is cycled to the reboiler and subjected to heat to vaporize at least a portion of the bottoms fraction to form a vapor phase in the vapor section, A slip stream of the bottoms fraction is introduced to the vapor phase section of the reboiler. The slipstream contains polymerization inhibitor that had been added to the process at the fractionation column. The invention reduces fouling at the reboilers. The slipstream is optionally introduced to the reboiler using one or more spray nozzles.

Abstract: An apparatus for conducting reactive distillations comprising a first distillation column, a first primary catalyst bed for carrying out a hydrogenation of unsaturated compounds comprising diolefins. The first primary catalyst bed is positioned in the distillation column to provide a first reaction zone for diolefins, and optionally, a first secondary catalyst bed above the first primary catalyst bed is provided as a second reaction zone for diolefins remaining in the first distillation column after the first reaction zone. A mixed saturated/unsaturated compound feed entry is provided below the first primary bed with a hydrogen feed below the primary bed. An overhead line connects to a second distillation column comprising a second primary catalyst bed for carrying out hydrogenation of unsaturated compounds comprising mono olefins from said first distillation column.

Abstract: Apparatus and process are disclosed for the distillation separation of styrene monomer from ethylbenzene utilizing a split feed to two distillation columns in conjunction with cascade reboiling utilizing thermal energy from the overhead of one column to supply heat to the second.

Abstract: The invention relates to a distillation and reaction device having a reaction section and a distillation-reaction section. The distillation-reaction section has a distillation zone with at least one device for circulation of the effluent from the reaction section to the distillation zone. Effluent from the reaction section is circulated to the distillation zone. The distillation-reaction section also has at least one distillation-reaction zone having at least one catalyst bed. The distillation-reaction zone is distinct from the distillation zone and provides at least partly the reflux of the distillation zone. The distillation-reaction section can also have at least one complementary reaction zone containing at least one catalyst bed. The invention further relates to a process for preparing at least one aliphatic monoalcohol, generally in excess, and at least one olefin.

Abstract: A process and apparatus are provided for recovering diluent, unreacted monomer, and unreacted comonomer from a polymerization reactor effluent. The comonomer has a boiling point higher than the boiling point of the monomer and the diluent has a boiling point between the boiling points of the monomer and comonomer. The process and apparatus employ at least one flash tank, a first fractionation stage including a first column and operating at a first fractionation pressure, and a second fraction stage including a second column and operating at a higher second fractionation pressure. Comonomer is withdrawn from the first column as a fractionation product, and overhead vapor containing diluent and monomer is substantially condensed to yield a substantially condensed overhead stream. Liquid and vapor from the stream are separated in an accumulator.

Abstract: A compact apparatus of the distillation of solvent from a mixture of the solvent with oil seed for the extraction thereof according to the invention, the primary module includes a vapor scrubber forming a vapor contactor, a main evaporator and a first condenser while the secondary module has an after evaporator combined in a unit with the stripping column and the second condenser.

Abstract: Process technology is described making possible substantial improvements in the separation and recovery of highly pure vinyl aromatic monomers, notably styrene. A number of design, construction and operational features are made available for selection and use both for new plant facilities and for upgrading existing plant facilities. One major aspect of the invention is reduction in retention or residence times in the distillation towers.

Abstract: A monotube or multitube 2 is coupled to a body shell 1 via tube plates 3a and 3b at both ends, so that a tube interior 4 and a tube exterior 5 of the monotube or multitube 2 are isolated from each other. A difference is made in operating pressure between the tube interior 4 and the tube exterior 5, so that one of the tube interior 4 and the tube exterior 5 is used as a lower-pressure column and the other is used as a higher-pressure column. A wall of the tube is used as a heat transfer surface, so that heat is transferred from the higher pressure side (higher temperature side) to the lower pressure side (lower temperature side).

Abstract: The production of high purity benzene and high purity toluene is obtained by utilizing the initial gas separating column for the treatment of the aromatic containing starting material as a separating column for separating a benzene rich from a toluene rich component. The benzene rich component is subject directly to distillation while the toluene is subject to predistillation to separate high boiling components and only then to extractive distillation is distilled to separate the high purity benzene from the high purity toluene.

Abstract: A method is provided for depositing ultra high purity of greater than 99.998% titanium films which comprises generating gaseous TiI.sub.4 in situ by reacting titanium metal starting material with gaseous iodide in a reaction chamber, purifying the TiI.sub.4 by a double distillation process at reduced pressure to produce ultra high purity of greater than 99.998% TiI.sub.4, transferring the ultra high purity TiI.sub.4 in liquid form to a deposition chamber to vaporize the liquid TiI.sub.4 and contacting a heated titanium substrate with the TiI.sub.4 vapor, thereby depositing the ultra high purity Ti films on the substrate.

Abstract: A heat exchanger is provided which is suitable for use as a condenser/reboiler in a double distillation column. The heat exchanger has alternating first and second passages and a reservoir located above the first and second passages for receiving a first fluid and for containing a froth. A series of orifices can be provided by a distributor tray to provide flow communication between the reservoir and the first passages to allow at least a liquid phase of the froth to weep into the first passages and to be partly vaporized through indirect heat exchange with a second fluid flowing through the second passages. The partial vaporization produces a vapor phase of the froth which can at least in part escape from the orifices and interact with the first fluid to thereby form the froth. A remaining part of the liquid phase, not vaporized through the indirect heat exchange, is discharged from the bottom of the first passages into a sump.

Abstract: An integral system and method for the separation and purification in a single operation of a heat or oxygen-sensitive liquid feed, such as a plant derived liquid feed mixture of fatty acids, tocopherol compounds and sterols, into a low boiling point purified fraction of Vitamin E tocopherol compounds and a high boiling point concentrate fraction of triglycerides, which system can be maintained in the presence of an inert gas to provide reduced degradation and increased purity of the Vitamin E fraction. The system includes a pre-evaporator, a vapor-liquid separator, a packed bed distillation column, a rotary thin film evaporator and an evaporator-stripper.

Abstract: An improved cryogenic liquefied gas container, or a so-called cold evaporator (CE) for containing a plurality of different liquefied gases such as oxygen and nitrogen gases can be installed on a site with a limited surface area and can store the gases at a substantially equal and constant temperature level to ensure a stable gas supply to consumers that may include medical facilities and manufacturing plants. A plurality of inner tanks 4 are vertically arranged and surrounded by an insulation layer 3 in an outer shell 2 in order to economically utilize the site. The temperature of the high boiling point liquefied gas LG1 contained in the upper inner tank 4a and hence the internal pressure of the upper inner tank are stabilized by means of a heat exchanger section 11 to which the low boiling point liquefied gas LG.sub.

Abstract: An apparatus and method for treating chemical production plant process condensate such that a contaminant-rich stream and a relatively pure aqueous stream is separately recoverable from the condensate, wherein the contaminants are substantially removed from the condensate by steam stripping and subsequent rectification in a relatively low pressure stripping/rectification tower. The tower overhead is then condensed with a portion of the condensed overhead being returned to the top of the rectification section of the tower as reflux and the balance being withdrawn as a concentrated stream for reuse in the plant. In a second embodiment, separate stripping and rectification towers operate in series whereby the overhead of the stripping tower is delivered to the lower section of the rectification tower and the rectification bottoms are returned to the top of the stripping tower.

Abstract: Reprocessing mixtures which contain organic solvents and constituents of low volatility and may contain water: includes introducing the mixture into a concentration apparatus of a solvent recovery system, concentrating the mixture in the concentration apparatus by evaporating off a portion of a readily volatile fraction and feeding this readily volatile fraction to a separation column. A portion of the concentrated mixture from the concentration apparatus is conducted away into a separation apparatus where the constituents of low volatility are separated off from the concentrated mixture and ejected from the solvent recovery system. The concentrated mixture is conducted away, freed from the constituents of low volatility, from the separation apparatus.

Abstract: To heat the circulating reboiler streams of multiple distillation columns a fired reboiler is provided for a first column requiring the most heat. A portion of the bottoms from the first column is passed through the tubes of the heater in the fired reboiler and recycled to the first column as is normal. A slip stream is taken from the recycle after heating and passed on to provide heat by indirect heat exchange to a second reboiler and if desired other reboilers or heat exchangers. The slip stream may then be recycled to the bottoms of the first column directly or to the circulating steam of the first reboiler. A portion of the recycled slip stream can be taken as feed into the second column.

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: Method and apparatus for the distillation of liquids which is particularly suited for the removal of soluble impurities and insoluble and non-volatile particles of 10 microns to 0.2 micron or less in size. A substantially elongated distillation chamber having walls equipped with axially disposed concentric boiling rings spaced from the walls near the bottom, and a packing stop, packing redirector rings for condensed vapor, and a reflux condenser in the upper part of the distillation chamber provide, during distillation, a smooth convective upward flow of distilling liquid and vapor proximate the walls and boiling rings and a smooth convective downward flow of distilling liquid and vapor substantially centrally of the distillation chamber.

Abstract: A methanol refining column and method using an intermediate reboiler. Use of the intermediate reboiler reduces methanol production energy requirements. A side stream at or near a fusel oil takeoff point is heated in an intermediate reboiler by a low temperature heating medium (relative to a bottoms reboiler) and returned to the column at or near the fusel oil take-off tray. The take-off tray is operated at 85.degree.-110.degree. C., and 70-90 percent of the reboiler duty is supplied through the intermediate reboiler. The remaining heat load is supplied by a bottoms steam reboiler.

Abstract: Process for obtaining a pure hydrocarbon from a starting material containing the hydrocarbon including performing an extractive distillation of the starting material containing the hydrocarbon in an extractive distillation column using a solvent comprising an N-substituted morpholine having substituents with no more than seven carbon atoms; feeding the sump product of the extractive distillation column into a distillation separator column at an entry point in a center portion of the distillation separator column; distilling off the hydrocarbon from the top of the distillation separator column but advantageously returning a minor portion of it as a reflux; drawing off solvent from the sump of the distillation separator column; feeding the solvent drawn off from the sump of the distillation separator column into an evaporator to form a vapor in the evaporator at the pressure, p.sub.2, the pressure p.sub.2 in the evaporator being lower than the pressure p.sub.

Abstract: A system for continuously recovering renewable volatile compounds by boiling points from waste organic solvent with minimum energy loss, and an improved thin membrane distillation apparatus for efficient distillation of renewable volatile compounds from waste organic solvent and enforced discharge of the residue or sludge. The waste treatment system includes a thin membrane distillation apparatus, a cooling unit, a first distillation unit, and a second distillation unit connected in this sequence. Alternatively, the system includes two thin membrane distillation apparatus, a reduced pressure distillation unit, and a normal pressure distillation unit connected in this sequence. The thin membrane distillation apparatus includes a decompression chamber, a waste inlet, an outlet for volatile compound, an air-tight chamber, and a breaking mechanism with a screw head movable into the air-tight chamber.

Abstract: A liquid waste reduction system uses an evaporator having two packed columns. A reservoir of the evaporator has three level sensor which monitor the fluid level in the reservoir. An input pump delivers waste liquid to the reservoir. When the fluid level has exceeded a low level, a control unit powers an output pump which pumps liquid from the base of the reservoir to an external storage unit. A distributor pump pumps liquid from the reservoir to the top of the packed columns. A blower forces air upward through the packing material to evaporate water from the liquid. When the fluid level has exceeded a high level, the control unit switches on a heating element which heats the air delivered from the blower to the second packed column, thus accelerating the evaporation process. When the fluid level has exceeded the maximum level, the control unit deactivates the input pump to prevent flooding of the evaporator unit.

Abstract: A distillation tower (1) has a plurality of liquid sidestream lines (5, 6, 7) and a multi-stage sidestream stripper (13) which includes a respective stripping section (14, 15, 16) for each sidestream line housed in a common, upright, cylindrical shell (28) which allows vapor to pass freely from each stage to the one above. Partial vaporization of each sidestream is achieved by applying a vacuum to the top of the stripper shell (point 21) and/or introducing strip gas at the bottom (point 20). Because the vapor passes serially through the stripping sections from the bottom of the stripper (13) to the top, the need to supply strip gas separately to the stripping sections and/or apply vacuum individually is avoided. The separation between the sidestream products is improved by including, in each stage, a rectification zone (22, 23, 24) positioned above the stripping section.

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: An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. The olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Abstract: An apparatus and method for reprocessing waste piranha containing contaminated H.sub.2 SO.sub.4 from, for example, a semiconductor processing operation is described. The apparatus and method include a first distillation flask which is maintained under a substantial vacuum. The first distillation flask includes a first column packed with a column packing material and an input pipe for refluxing to retard loss of H.sub.2 SO.sub.4 in the first distillation. The second distillation flask boils off substantially pure H.sub.2 SO.sub.4 and provides for a continuous automatic purge of the contaminants from the second distillation flask thus improving the purity of the H.sub.2 SO.sub.4. The substantially pure H.sub.2 SO.sub.4 flows through a column which is coupled to a condenser which condenses substantially pure H.sub.2 SO.sub.4.

Abstract: A mobile petroleum processor or refinery. In particular a petroleum processor or refinery which has been constructed on railroad flatbed cars. The different units that make up the refinery are mounted on individual flat bed railroad cars and connected together. These cars can be moved over railroad networks to provide a petroleum refinery which can be moved in, set up, operated and taken down in a short time.

Abstract: An apparatus and method for reprocessing waste piranha containing contaminated H.sub.2 SO.sub.4 from, for example, a semiconductor processing operation is described. The apparatus and method include a first distillation flask which are maintained under a substantial vacuum. The first distillation flask includes a first column with a column packing means and a reflux means to retard loss of H.sub.2 SO.sub.4 in the first distillation. The second distillation flask boils off substantially pure H.sub.2 SO.sub.4 through a column which is coupled to a condenser which condenses substantially pure H.sub.2 SO.sub.4.

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 two-step distillation process provides semiconductor purity, concentrated hydrofluoric acid. Further, the distillation process, occurring under reduced pressures eliminates essentially pure water after the first distillation step. The product output of the second distillation process provides an acid of weight percent greater than 27 weight percent. The product acid is carefully diluted to the required concentrations during the dilution step.

Abstract: A vapor-and-liquid contact structure for distillation, fractionation, rectification, absorption, and the refining, in a column, of various liquid materials such as petroleum, chemical, and alcohol solutions wherein provision is made for the inclusion of vertically-spaced bubble plate chambers, having respective liquid and vapor contact devices, to accommodate contact of counter-current flows of reflux liquid and vapors. A downcomer, including slanted ramps, is disposed outside of the vapor conduit-defining interior, and defines an elongate downcomer structure for liquid flow. Accordingly, descending reflux liquid flow is kept outside of primary vapor flow, with secondary vapor evolving from descending reflux being conducted circuitously back into the primary vapor flow for ascent to the next-above contact device. Plate efficiency is enhanced through maximum plate-area effective use and unidirectional liquid-flow over such plates.

Abstract: An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. Thye olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Abstract: A method and apparatus for removing water from a liquid mixture of water and ethanol contacts it with liquid carbon dioxide so that the ethanol is preferentially transferred into solution, dries the solution using an adsorbent, and then recovers dry ethanol by distilling off the carbon dioxide. This process is particularly energy efficient especially when it includes a fermentation process to generate the ethanol and uses the carbon dioxide generated during the fermentation as the source of liquid carbon dioxide. In this case the method and apparatus provide an additional product of dry carbon dioxide.

Abstract: A continuous catalytic system for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product comprising apparatus for(a) prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefins;(b) vaporizing and contacting the liquid stream from the prefractionating step with hydrocarbon conversion oligomerization catalyst in a catalytic reactor system to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons;(c) fractionating the effluent stream to recover distillate, gasoline and lighter hydrocarbons separately;(d) recycling at least a portion of the recovered gasoline as a liquid sorption stream to prefractionating step (a); and(e) further reacting the recycled gasoline together with sorbed C.sub.3.sup.+ olefins in the catalytic reactor system of step (b).

Abstract: Apparatus for reducing the amount of water in the feed to a methanol-to-gasoline (MTG) conversion reactor is described. The output products of a dehydration reactor and an aqueous methanol feed are supplied to a primary distillation tower or separator. A dimethylether (DME)/methanol mixture is taken as overhead from the primary tower and can be sent to the MTG conversion reactor to produce hydrocarbons boiling in the gasoline range. Bottoms from the primary tower, containing methanol and water, are supplied to a secondary distillation tower or separator. A methanol stream is drawn as overhead from the secondary tower and is passed to an acid catalyzed dehydration reactor where an equilibrium mixture of dimethylether, methanol, and water is produced. The equilibrium mixture is passed from the dehydration reactor to the primary distillation tower. In preferred embodiments, the conversion reactor feed from the primary distillation tower may be of a gaseous or liquid phase.

Abstract: Vapor and liquid contact structure for distillation, fractionation, rectification, absorption, and the refining, in a column, of various liquid materials such as petroleum, chemical, and alcohol solutions. Provision is made for the inclusion of vertically-spaced bubble plate chambers, having respective liquid/vapor contact devices, to accommodate contact of counter-current flows of reflux liquid and vapors. Downcomer means including slanted ramps, disposed outside of the vapor conduit-defining interior, define elongate downcomer structure for liquid flow and thereby, i.e., by such slanted construction, reduce froth or foam passing to a next lower contact device, eliminating unwanted counter-current gas entrainment between contact devices. Liquid flow rates over exit weirs beyond 30 gpm/inch are obtained. Downcomer reflux reservoir depth can be adjusted by an adjustable gate proximate the slot opening to a given contact device.