Abstract: A process for separating or stripping lighter components from a heavier hydrocarbon feedstock contaminated with or otherwise including light components. The separation is accomplished by introducing the feedstock into a column and allowing the feedstock to flow through the column, contacting a first stripping medium and a second stripping medium. The first stripping medium entrains the lighter components. The second stripping medium entrains the first stripping medium and any lighter components remaining in the feedstock. Preferred first stripping media include hydrogen, methane, propane, and other inert gas and preferred second stripping media include nitrogen and other inert gas.

Abstract: A process for the preparation of mixtures of chlorotetrafluoroethane and octafluorocyclobutane from the gas stream from the pyrolysis of chlorodifluoromethane at temperatures above 600.degree. C. is described in which the principal constituents tetrafluoroethylene and hexafluoropropylene as well as hydrogen chloride are removed in advance. The mixtures are obtained by withdrawal as a side fraction during the rectifying distillation of the residue remaining, a clean separation of the perfluorocyclobutenes advantageously taking place. The mixtures are used for obtaining hexafluoropropylene by pyrolysis.

Abstract: Disclosed herein is a process for removing chloroprene by subjecting chloroprene-containing 1,2-dichloroethane to heat treatment at a temperature in the range of from the boiling point (85.degree. C.) of 1,2-dichloroethane to the thermal cracking temperature (300.degree. C.) of 1,2-dichloroethane. In particular, the process can be suitably applied to a liquid distillate from a low-boiling material separation column in a step in which 1,2-dichloroethane used as a raw material for production of vinyl chloride is purified by using a fractionation column.

Abstract: A method of separating and recovering components of a mixture having a gap in the range of miscibility and including organic compounds and water in a pervaporization process with the aid of membranes. The mixture is first separated into an organically loaded water phase and a water-saturated organic phase. Subsequently, the organically loaded water phase and the water-saturated organic phase are separately subjected to parallel, different pervaporization processes, resulting in retentates as water on the one hand and organic liquid on the other hand. The permeates that result during the pervaporization processes are subsequently returned to the mixture that is to be separated.

Abstract: The waste heat from a steam turbine is condensed and used to desalinate sea water at the same time. The waste steam from a turbine is fed to a condenser through which cold sea water passes. As the cold sea water condenses the waste steam, it is warmed. It is then introduced into a first chamber which includes a number of spray heads disposed over fill (packing) that acts as an evaporator. Any water not evaporated is collected in a sump at the bottom of the first chamber, and the evaporated vapor is passed upwardly under the influence of a fan and ultimately to a second chamber. The second chamber may either be stacked above the first chamber, or in side-by-side relationship with it. A condenser, such as a number of dimpled metal plates, or plastic membranes defining a closed loop, or another set of spray heads and fill, are provided in the second chamber. Air typically recirculates from the bottom of the second chamber back into the first chamber.

Abstract: A fractional distillation column and method for its use are provided which employ n sets of trays, where n is an integer and n.gtoreq.2. An equivalent number n of separate liquid streams are passed generally downwardly through the column so that each liquid stream flows onto and between individual trays of its corresponding set of trays.

Abstract: In a method of optimizing the operation of a distillation column with a side heating device for reconditioning of extract which is received during the extraction of hydrocarbon-containing initial products with N-substituted morpholines whose substituents have not more than seven C-atoms as selective solvents a liquid is withdrawn to a side heating device through a chimney plate arranged above a feed plate, so that between 5 and 30 volume percent of the liquid supplied to the chimney plate is not withdrawn to the side heating device but instead supplied directly to a plate located underneath the chimney plate. A vapor-liquid mixture which has escaped through a top from the side heating device is returned back to the distillation column. The returned vapor-liquid mixture is fed either to the feed plate or to the plate located underneath the chimney plate. An arrangement for performing the inventive method is also provided.

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 process for the production of pure dimethylether by feeding the dehydration product from a dimethylether-synthesis reactor into a distillation column for the production of pure dimethylether at defined trays of this column and withdrawal of pure dimethylether and a fraction containing contaminations at defined trays of the same column, whereby in addition washing liquids and bases can be added.

Abstract: A thermally-integrated extractive distillation process for recovering anhydrous ethanol from fermentation or synthetic feedstocks has a distillation train of four columns. Two columns are preconcentrators operated in parallel. The remaining columns are an extractive distillation dehydrating tower, and an entrainer-recovery column. The two preconcentrators and the dehydrating tower are operated at three successively increasing pressures so that the condensing vapors of the overhead product of the dehydrating tower supply the necessary heat to the reboiler of the intermediate-pressure preconcentrator. The overhead vapors of this preconcentrator are, in turn, used to supply the required heat to the reboiler of the lowest-pressure preconcentrator. The bottom product from each preconcentrator is used to preheat the dilute feed. Additional energy savings are accomplished by the appropriate heat exchange between the various feeds, overheads, and bottoms.

Abstract: In a vacuum distillation process a feed stream is supplied to a furnace and a heated feed stream containing vapor and liquid is passed from the furnace into a distillation column operating at a subatmospheric pressure. Vapor is allowed to rise inside the distillation column. The rising vapor is contacted with a de-entrainment means to remove entrained liquid from the rising vapor. Wash liquid is sprayed on the de-entrainment means and subsequently passed from the distillation column to a collection vessel. The wash liquid is cooled and then withdrawn from said collection vessel.

Abstract: A feed which contains vapor and liquid is introduced into a distillation column operating at a subatmospheric pressure. Vapor is allowed to rise inside the distillation column and liquid is allowed to drop to the bottom part of the distillation column. From said bottom part a liquid is passed through a transfer conduit to an external collecting vessel from which a liquid stream is withdrawn. The liquid stream is cooled and part thereof is introduced into the transfer conduit.

Abstract: Improved hydrocarbon vacuum distillation process wherein the process steps include introducing a feed which contains liquid hydrocarbons and vaporous hydrocarbons into an inlet section (3) of a distillation column (1) operating at a subatmospheric pressure, removing liquid from a bottom section (6) of the distillation column (1), allowing vapor to pass through three condensation sections (13b, 13a and 13) arranged above each other in the distillation column (1) between the inlet section (3) and a top section (8), removing vapor from the top section (8), spraying into each condensation section (13, 13a and 13b) cooled liquid, and removing liquid from each condensation section (13, 13a and 13b), wherein the cooled liquid which is sprayed into each condensation section (13, 13a and 13b) includes liquid removed from that condensation section (13, 13a and 13b), and wherein the cooled liquid which is sprayed in the uppermost condensation section (13) further includes liquid removed from the condensation sections (1

Abstract: Small amounts of a medium-boiling fraction are removed from a liquid mixture by distillation using a distillation column (main column) having a rectifying part and a stripping part, the liquid mixture containing relatively large amounts of lower-boiling and higher-boiling components, and the rectifying part being connected to the upper end of a second distillation column (side column) and the stripping part to the lower end of the said column, and the medium-boiling fraction being removed in vapor or liquid form from its middle section, by a process in which the concentration of the medium-boiling fraction in the liquid mixture is less than 2%, preferably less than 0.1%, and the amount of vapor passed into the lower end of the side column from the main column is 1-20%, preferably 3-10%, based on the amount of vapor in the main column at the relevant point.

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: An integrated continuous processes for concentrating "weak" nitric acid and concurrently reconcentrating the spent dehydrating agent used to break the nitric acid azeotrope to obtain "strong" nitric acid, the processes involving direct coupling of the nitric acid concentration with the reconcentration of the spent dehydrating agent so that less energy input is required. The major proportion of the feed "weak" nitric acid is vaporized before being fed countercurrently into a column to contact a large volume of the dehydrating agent, this vaporization being one of the two major sources of energy input, the second being through the reboiler at the bottom of the column. Energy input is balanced by energy rejection through condensation of strong nitric acid vapor and water vapor.

Abstract: Process for the evaporative concentration of liquids. Vaporization is carried out by indirect heat exchange with a heating fluid in an evaporator. The vapor produced in the evaporator is thereafter condensed in a condenser by indirect heat exchange with a cooling liquid which is mainly composed of the liquid to be concentrated or the liquid which has already been concentrated in the evaporator. The vapor pressure over the cooling liquid in the condenser may be lowered by causing gas to flow in contact with the cooling liquid.

Abstract: A distillation apparatus including a pair of vertical lower vessels each open at its upper end, and a pair of elongate upper vessels each having an open lower end, slidably mounted in a respective one of the lower vessels. A heat exchanger is mounted in each of the upper vessels, with the upper end of one upper vessel being connected to the inlet of the heat exchanger in the other vessel, and vice versa. A reciprocating drive mechanism drives the two upper vessels up and down in opposite directions so as to simultaneously effect compression in the space above the liquid level in the downwardly moving vessel while expanding the space above the liquid in the other vessel, driving vapor from the downwardly moving vessel into the heat exchanger in the other vessel, where it condenses.

Abstract: A process and apparatus are disclosed for the production of gasoline from a C.sub.4.sup.- fuel gas containing ethene and propene and catalytic reformate containing C.sub.6 to C.sub.8 aromatics. The C.sub.4.sup.- fuel gas is contacted with debutanized catalytic reformate over a zeolite catalyst under process conditions to convert ethene and propene in the C.sub.4.sup.- fuel gas to C.sub.5.sup.+ aliphatic and aromatic hydrocarbon gasoline and to convert C.sub.6 to C.sub.8 aromatics in the reformate to C.sub.7 to C.sub.11 aromatic hydrocarbon gasoline. Reformer fractionation system containing debutanizer column and separator stabilizes effluent gasoline and recycles unconverted light aromatics.

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: An extractive distillation process for separating at least one cycloalkane from at least one close-boiling alkane employs as solvent a mixture of (a) at least one saturated C5-C9 alcohol (preferably cyclohexanol) and (b) at least one glycol compound (preferably tetraethylene glycol).

Abstract: Tetrahydrofuran is recovered by a two stage distillation procedure from a crude hydrogenation product resulting from vapor phase hydrogenation of diethyl maleate and containing water, ethanol and a minor amount of n-butanol, and possibly also dissolved hydrogen, in addition to butane-1,4-diol, gamma-butyrolactone and "heavies" such as diethyl ethoxysuccinate. In the first distillation stage, conveniently operated substantially at atmospheric pressure, ethanol, water, and tetrahydrofuran are recovered as overhead product, are condensed to separate the condensible components from a hydrogen stream which can be vented, and then redistilled in the presence of a molar excess of a hydroxylic solvent containing at least two hydroxyl groups, such as butane-1,4-diol, in a second distillation zone.

Abstract: A process for removing volatile acids from aqueous solutions which involves steam stripping a volatile acid from an aqueous solution and contacting the vaporized acid with a reactable cation to form a salt of the acid. A preferred embodiment of apparatus comprises an elongated distillation column having therein a plurality of zones or stages wherein the volatile acid in the aqueous feed stream is vaporized by steam and then the vaporized acid is carried by the steam into a salt formation zone or stage to react with a reactable cation to form a salt of the acid.

Abstract: A volatile component is separated from a mixture by vaporization in an evaporator and condensation in a condenser. The vapor is transported by a carrier gas that is circulated in and between the evaporator and the condenser. A flow of a liquid is circulated in subsequent heat transfer steps from contact with the mixture via a cooler, via contact with the carrier gas in the condenser, via a heater, and back to contact with the mixture.

Abstract: A liquid product (4) leaving a furnace (2) is introduced into a series of cyclone separators (5, 6, 7). The liquid product to be vaporized is introduced tangentially into the top portion (5a, 6a, 7a) of each cyclone to place the product into contact with a side wall (5b, 6b, 7b) of the cyclone. A gaseous phase (11, 12, 13) formed in each cyclone is collected in the central zone (8, 9, 10) of the cyclone and is then introduced into a vacuum distillation column (3). The liquid phase obtained in each cyclone is collected at the bottom (5c, 6c, 7c) of the cyclone and then is introduced tangentially into the top (6a, 7a) of the following cyclone or, in the case of the last cyclone, is introduced directly into the vacuum distillation column (3). The side wall (5b, 6b, 7b) of each cyclone (5, 6, 7) is heated to a temperature near the maximum temperature allowable for avoiding all thermal deterioration of the product.

Abstract: A water distillation apparatus having a distilled water storage tank and a water boiling tank. Components associated with the boiling tank control the level of water therein and production of steam from the water contained therein. A steam flow line permits steam flow from the boiling tank into the storage tank. A distilled water cooling coil disposed in the storage tank at a lower region below the distilled water level is connected with a cool water infeed flow line. A steam condensing coil disposed in the storage tank at an upper region thereof above the desired water level and the cooling coil is connected with the cooling coil. Steam which enters the storage tank can directly contact the condensing coil exterior surface for causing the steam to condense into distilled water in the storage tank.

Abstract: 1,3-Butadiene is isolated from a C.sub.4 -hydrocarbon mixture containing 1,3-butadiene and small amount of propyne and C.sub.5 -hydrocarbons by extractive distillation with a selective solvent and subsequent distillative purification of the crude 1,3-butadiene obtained in the extractive distillation.

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: A fractional distillation system is provided for fractionating unequal liquid mixtures with lower heat throughput and lower energy consumption. For mixtures in which the heavy fraction is predominant (FIG. 1), a stripper (2) pre-fractionates part of the mixture at lower pressure and at no extra energy cost by being reboiled by an intermediate condenser (3). The pre-fractionator temperature range is preferably nested within (overlapped by) the distillation column (6) temperature range.

Abstract: The invention relates to a process for the isolation of vinyl acetate from a gas mixture containing vinyl acetate, ethyl acetate, water and carbon dioxide formed in the reaction of ethylene with acetic acid and oxygen in the gas phase over catalysts containing palladium or palladium compounds. The gas mixture leaving the reaction zone is passed into a distillation column and the gas mixture leaving the top thereof is cooled. The gas which is not condensed during the cooling is washed with acetic acid in a washing column, an acetic acid solution containing vinyl acetate being obtained. The bottom product from the distillation column is passed to a second distillation column and a side stream containing ethyl acetate is removed from an enrichment zone above the bottom thereof, all or some of the bottom product from the second distillation column, which product chiefly consists of acetic acid, being used for the wash in the washing column. The top vapor of the second distillation column is cooled.

Abstract: Deodorizing and/or physical refining of relatively small, varying charges of high-boiling liquids, viz. fatty acids, edible oils, fats, glycerides and other high-boilding esters, is conducted continuously in a single-stage or multi-stage falling-film column (20) through the trickle passages (23) of which stripping steam is passed in counter-current flow. In the supply conduit (15, 15', 15", 15'") leading to the falling-film column and in the discharge conduit (30, 30', 30", 30'") leading away from the bottom (26) of the falling-film column a plug-flow of the liquid is maintained. Upon a change of charge the fresh liquid to be treated is normally introduced into the supply conduit--without any blank charge--directly following the liquid of the preceding charge. Charging of the liquid onto the deflector (22) in the head (21) of the falling-film column is interrupted for a short period of time when the front of the liquid of the fresh charge has reached a check valve (16) disposed adjacent said deflector.

Abstract: This invention relates to a process for preparing 2,2-bis(4-hydroxyphenyl)propane, e.g. bisphenol A and particularly to a process for preparing high quality bisphenol A with good workability by distilling the intermediate adduct of bisphenol A and phenol.The adduct of bisphenol A and phenol is fed to a distillation column. Phenol is recovered from the top of the column and bisphenol A is obtained from its bottom. In this distillation process, the adduct of bisphenol A and phenol is added with a part of recycled bottom liquid. Consequently troubles such as plugging of the distillation column are prevented, continuous operation becomes possible for a long period of time and high quality bisphenol A can be steadily obtained.

Abstract: In the purification of ethylene oxide from an ethylene oxide-containing reaction formation gas produced by catalytic gas-phase oxidation of ethylene with a molecular oxygen containing gas, external thermal energy required for heating an ethylene oxide refiner is economized by a method which utilizes the diffusate obtained from the top of an ethylene oxide stripper as a heat source for the refiner. Further, the bottom liquid of the stripper can be used as a heat source for ethylene oxide refiner and/or a light ends stripper.

Abstract: In a method and arrangement for separating a liquid mixture or a solution by converting a portion of the liquid mixture or portion of a solvent of the solution into a vapor phase and subsequent condensation of the obtained vapor with a porous separating wall, the pores of the porous separating wall are acted upon by a gas or gas mixture supplied through the pores of the porous separating wall in a counterstream to the vapor.

Abstract: A process is disclosed for the separation of aromates from hydrocarbon mixtures of optional aromate content through extractive distillation using N-substituted morpholine displaying substituents having no more than 7 C-atoms as selective solvent. Part of the solvent is delivered to the uppermost plate of the extractive distillation column and the remainder of the solvent, preferably amounting to between 10 and 40% by weight, is introduced into the extractive distillation column in at least two partial streams onto plates above the inlet for the hydrocarbon mixture. The temperature of the respective solvent partial streams is adjusted to neither exceed the temperature of the corresponding delivery plates nor fall below this temperature by more than 10.degree. C.

Abstract: A steam generator, especially a pure steam generator, having a feed line for conducting feed water to the same, an electrode system for heating the feed water, a steam outlet for removing generated steam, and a separating space in a lower part of the generator 10, along with a droplet separator through which the steam that has been generated is disposed to flow from the separating space to the steam outlet. Electrodes have been placed in small tubular spaces in a water space (i.e. a space receiving incoming feed water). The steam generator may be used in a multi-stage distilling apparatus by conducting the steam that has been formed to a second column or stage of the distilling apparatus, to constitute feed steam therefor.

Abstract: A method for passivating the surface of the strippers of the urea plants, where the temperatures are very high, where the pressures range from 120 to 240 Kg/cm.sup.2 and where the effluent process flow from the synthesis reactor undergoes one or more falling-film evaporations, preferably in countercurrent with a driving gas consisting of NH.sub.3 or CO.sub.2, characterized by the fact that the passivation is carried out by means of a sinergistic combination of oxygen, preferably injected into the bottom of at least one stripper, and of a second passivating agent, preferably injected into the process flow entering the head of at least one stripper, wherein said second passivating agent is injected in the liquid state or as a liquid solution, before or contemporaneously to the start of the evaporation.

Abstract: A process for the purification of 1,2-dichloroethane is described, in which the crude product, containing not more than 3% by weight of high-boilers, is distilled in a first column at 125.degree. to 180.degree. C. in such a way that the bottom product contains not more than 7% by weight of high-boilers. The purified, vaporous 1,2-dichloroethane discharged at the head of this column is used to heat product streams containing 1,2-dichloroethane. The bottom product from the first column is distilled in a second column, advantageously at a pressure of 5 to 40 kPa, together with a feed composed of vaporous 1,2-dichloroethane obtained from the reaction of ethylene with chlorine. The process makes it possible to purify 1,2-dichloroethane with a saving in energy.

Abstract: An aqueous effluent is supplied to a stripping column (total stripping column) from which a mixture that is rich in NH.sub.3, CO.sub.2 and H.sub.2 S is withdrawn as a head product. In at least one additional stripping column the mixture is separated into a mixture which is rich in NH.sub.3 and a mixture which is rich in the sour gaes CO.sub.2 and H.sub.2 S. The mixture which is rich in NH.sub.3 is scrubbed with liquid ammonia. The overhead product from the total stripping column is cooled in a condenser under a pressure of 1 to 7 bars and is thus transformed into a liquid phase to such an extent that the liquid phase contains 70 to 100% of the NH.sub.3 which has been supplied to the condenser. The liquid phase is supplied at a temperature of 30.degree. to 90.degree. C. to a second stripping column (NH.sub.3 stripping column), which is operated under a pressure of 1 to 4 bars and from which a gas mixture that is rich in NH.sub.3 is withdrawn as a head product.

Abstract: An apparatus for desalinating sea water, comprising a distillation unit which includes a porous hydrophobic membrane which is pervious to steam but impervious to water, and a condensation surface arranged at a distance from the membrane, the distillation arrangement also including a first unit for heating and conducting the water to be distilled on one side of the membrane, and a second unit arranged to conduct a liquid which is colder than the water, on the side of the condensation surface remote from the membrane, distilled water being collected and drawn-off between the membrane and the condensation surface.

Abstract: A process for purifying a solvent suitable for use in the polymerization of an olefin in the presence of a Ziegler-Natta catalyst, which comprises feeding the polymerization solvent to a stage lower than a chimney tray of a multi-stage distillation column, said chimney tray being provided at a height between the top and bottom of the column, feeding an organoaluminum compound to a stage higher than the chimney tray, drawing out a condensate from the chimney tray, heating the condensate to produce heated vapor, introducing the heated vapor to the chimney tray or to a stage higher than the chimney tray but lower than the stage to which the organoaluminum compound has been fed, and drawing the solvent in a purified state from the top.

Abstract: A system for diaphragm distillation of a liquid, for example for desalination of salt water, comprising a diaphragm, through which vapor, but not liquid can pass, and a condensation surface for condensing vapor having passed through the diaphragm, and necessary passageways. According to the invention, the system comprises one or several units, each of which comprises a plurality of pipes located one within the other, viz. a first (1) inner pipe, a second (2) pipe located outside thereof and consisting of a diaphragm of the aforesaid kind, and a third (3) pipe located outside the second (2) pipe, which first (1) and third (3) pipes are of a gas-tight material, that said unit is surrounded by a fourth (4) gas-tight pipe, where a first (5) passageway is formed by the first (1) pipe and a second (6), a third (7) and a fourth (8) passageway are formed between said pipes (1,2;2,3;3,4) in successive order in the direction from the inside outward.

Abstract: Method and apparatus are provided for simultaneously producing various forms of alcohol, including ethanol, which can likewise be withdrawn from the apparatus simultaneously. To this end, successive columns in the individual processing stages, each of which includes distillation, rectification, purification and dehydration, are connected in parallel for product flow but in series for energy flow and conservation.

Abstract: A vacuum distillation system uses a tower having an open bottom submerged within a tank of solution exposed to atmospheric pressure. The solution within the tower is elevated to barometric level by a high vacuum or low absolute pressure on the tower top. As solution flows through the open bottom and upward, the solution is heated and then cooled to cause degasification and precipitation, and then withdrawn from the tower top. The treated solution is flowed to a vaporization chamber that is subjected to a low absolute pressure. A heater maintains the solution at a selected chamber temperature above the boiling point of water at the selected chamber pressure. The chamber pressure and temperature may be selected as desired to yield the purest water distillate for almost any solution of water and impurities. Water vapor is pumped from the vaporization chamber by a vapor pump to a condenser, where condensation results from increased pressure and decreased temperature.

Abstract: A method of and 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: A method and apparatus for separating at least one component of a mixture from another without the aid of gravity comprises, in one embodiment, a heat pipe structure having an inlet and spaced outlets, a wick element disposed within the heat pipe for inducing a capillary flow of condensed phase mixture in liquid form therealong and spaced heating and cooling elements for creating zones of higher and lower temperature, respectively, within the heat pipe structure. In an alternate embodiment, a sorbent column is provided having an inlet and spaced outlets, a sorbent material disposed along the inner wall of the column for inducing a flow of adsorbed mixture therealong and spaced heating and cooling elements for creating zones of higher and lower temperature.

Abstract: The present invention provides a process for distillation of styrenes which can be stably operated without loss of energy saving effect, by leading a part or all of low boiling point component vapor from the top to a compressor to use as a heat source for a reboiler and returning the low boiling point components condensed in the reboiler or a mixture of the condensate and a part of the uncondensed vapor to a recycling line of a distillation column.

Abstract: A method of treating a liquid containing radioactive contaminants to produce a vapor containing a reduced amount of radioactive contaminant wherein continuous evaporation is effected in a vessel comprising two interconnected sections, one surrounding the other, the degree of evaporation in the inner section being greater than in the outer section thereof resulting in a greater concentration of radioactive material in the inner section.The outer evaporation section acts as a shield to reduce the release of radiation from the concentration of radioactive materials in the inner section.

Abstract: An apparatus for generating at least two vapor zones, one above the other, by vaporizing a fluid mixture having at least two compounds therein having different vaporizing temperatures. The apparatus includes a chamber with vaporizing means, and vapor condensing means. Condensate recovery means is provided for recovering the condensed vapor and the condensate recovery means is in flow communication with a separation device for receiving the condensate from the condensate recovery means. The flow communication between the condensate recovery means and the separation device is external of the chamber. The separation means revaporizes the liquid with the lower vaporizing temperature for return to the vapor zone in the upper portion of the chamber and separates as a liquid the fluid having a higher vaporizing temperature.

Abstract: A novel fractional distillation process and applications thereof to the production of thermal or mechanical energy from two low level heat sources wherein a mixture of two highly non-ideal reactive solutions such, for example, as of the water/ammonia type, is separated into its water and ammonia components in an apparatus comprising a cascade of condensers and evaporators operating respectively at the temperature of the cold source and at the temperature of the hot source and at staggered pressures. The residue and distillate formed are remixed in a mixing apparatus when it is desired to recover the thermal energy of dilution of the solutions.The invention is applicable, in particular, to the heating of buildings from low level thermal energy and from the thermal energy of "cold wind".