Abstract: A process for recovering heavy metal ions or heavy metal ions and halogen values from a solution comprising a lower aliphatic monocarboxylic acid, which comprises the steps of:(1) contacting a lower aliphatic carboxylic acid solution containing heavy metal ions or heavy metal ions and halogen values with an anion exchange resin, at least 60% of the ion-exchange groups of said anion exchange resin being in the bromide or chloride state, while the water concentration in the lower aliphatic monocarboxylic acid solution has been adjusted to a level lower than 20% by weight, thereby to adsorb the heavy metal ions or the heavy metal ions and the halogen values on the anion exchange resin; and(2) desorbing the adsorbed heavy metal ions or the adsorbed heavy metal ions and the adsorbed halogen values from the anion exchange resin by elution with an eluent.

Abstract: Disclosed herein is a process for recovering a phosphate ester type hydraulic fluid from a waste liquid containing water, organic solvents and other impurities, such as polychlorinated biphenyls (PCB). After filtering to remove particulate matter, a heavy fraction separated from the waste liquid and consisting primarily of the hydraulic fluid is first subjected to a distillation step. A substantial portion of the PCB is removed as overhead from the distillation step and the bottoms containing the hydraulic fluid is subsequently evaporated, preferably in a thin film evaporator. The overhead from the evaporation step is condensed to recover the hydraulic fluid.

Abstract: Acrylic acid is separated from its solutions in tri-n-butyl phosphate by establishing from such a solution a vapor phase comprising substantially all of the acrylic acid and a portion of the solvent, at a temperature below the degradation point of the acrylic acid; next partially or totally condensing said vapor phase; and then distilling the acrylic acid from such condensation product, while maintaining an amount of acrylic acid at the base of the distillation column, and conducting the distillation under conditions such that neither solvent degradation nor acrylic acid crystallization results.

Abstract: This invention is concerned with a continuous process for separating higher boiling, heat sensitive components from a liquid product stream. It involves a rapid evaporation of the desired product of the stream in an evaporator which minimizes residence time, such as a falling film evaporator, and feeding the vapors and the remainder of the stream to a separation column where the vaporized products rise in the column. Part of the vaporized products are removed after condensation and then recycled back to the column as a reflux. This reflux after contacting one or more trays is collected and recycled to the evaporator and mixed with the product feed being treated. The liquid remainder of the feed stream is collected at the bottom of the column. The bottom of the column can be kept at a temperature which minimizes any breakdown of the heat sensitive components present therein and, if desired, the bottoms in the column can be quickly withdrawn for treatment elsewhere or for recycling back to the process.

Abstract: A process for concentrating at least one of (a) individual halogenoanthraquinones (b) binary mixtures of di-halogenoanthraquinones and (c) binary mixtures of trihalogenoanthraquinones, from a mixture containing at least two halogenoanthraquinones, comprising subjecting said mixture containing at least two halogenoanthraquinones to fractional vacuum distillation in a heated rectification column having an efficiency corresponding to about 20 to 50 theoretical stages with an absolute pressure at the top of about 0.5 to 50 mm Hg and a reflux to take-off ratio of about 5/1 to 50/1.

Abstract: The purification of high-melting organic products, such an anthraquinone and substituted anthraquinones, which is substantially free from lower-boiling impurities, by melting the product to be purified by heating, while mechanically conveying the same along a path with a screw conveyer, as for example, in a melting screw; degassing the melt at a reduced pressure in a column, as for example, at a pressure of 50 to 400 mm Hg; passing the degassed melt through a thin film evaporator at a reduced pressure of, for example, 5 to 250 mm Hg to evaporate the high-melting organic product and discharging the remaining high-boiling impurities and such impurities which are not capable of being distilled from the evaporator through a conically tapering sump, while mechanically scraping residue from the sump wall, preferably with the use of a rotating helical screw in the sump; the discharge from the sump being effected into and through an enclosed path at a rate sufficient to prevent liquid accumulating in the sump, while

Abstract: A process for recovering fatty acids and/or rosin acid with a high purity which comprises first introducing a tall oil skimming soap or a tall oil soap into a thin film evaporator equipped with a rake in which the clearance between the blade tips and the surrounding evaporator wall is zero or not more than 1 mm, heating the same at a temperature higher than the melting point of the soap contained therein to evaporate and remove water and unsaponifiables, and then adding an alkali to the thus obtained crude soap to saponify the same, thereby decomposing the esters of rosin acid and fatty acids with sterols and other alcohols; or first saponifying a tall oil skimming soap or a tall oil soap with an alkali to decompose esters of rosin acid and fatty acids with sterols and other alcohols, and then introducing the thus obtained saponification product to the above-said thin film evaporator equipped with a rake, heating the same at a temperature higher than the melting point of the soap contained therein to evaporat

Abstract: Process for the separation of trioxane from aqueous solutions containing it together with formaldehyde, which comprises subjecting the said solutions to evaporation at temperatures of 100.degree. C or lower, at pressures lower than atmospheric, and with residence times of less than 1 minute under the evaporation conditions, with vaporization of a quantity of from about 5 to about 15% by weight of the solution introduced, and recovering the trioxane from the products evaporated in this way.

Abstract: 2,5 DIOXO-1-OXA-2-PHOSPHOLANES OF THE GENERAL FORMULA: ##STR1## in which R.sup.1 stands for an alkyl radical having from 1 to 4 carbon atoms, or a phenyl radical, and R.sup.2 and R.sup.3 each stand for hydrogen or CH.sub.3, are distillatively purified. To this end the respective crude compound is preheated to 120.degree. to 160.degree. C and fed to the head of a distilling column provided with a plurality of individually heatable trays maintained at temperatures increasing from the upper-most tray to the lowermost, the uppermost tray in the column being maintained at 120.degree. to 160.degree. C and the lowermost tray being maintained at 160.degree. to 200.degree. C, the pressure at the head of the column being 20 to 200 mm Hg, preferably 50 to 120 mm Hg; an inert gas preheated to 160.degree. to 200.degree.

Abstract: Glycide is prepared by reacting allyl alcohol with hydrogen peroxide in the presence of a tungsten compound as a catalysts the excess allyl alcohol and the greatest part of the water distilled off, the sump mixture obtained in the distillation is split at 110.degree.-220.degree. C. and 5 to 60 torr in a thin layer evaporator into a volatile portion which is predominantly glycide, high boiling by products and the residual part of the water and a sump portion of glycerine, polyglycerine and catalysts. The volatile liquid portion is broken into glycide, water and high boiling byproducts at 5 to 60 torr in a distillation apparatus directly connected to the thin layer evaporator.

Abstract: Process and apparatus for recovering residual oil from solids previously substantially dehydrated by a process wherein a slurry of water-wet solids in oil is subjected to a heat evaporation step to substantially remove the water. The oil is then largely expressed from the solids after which the solids still containing some oil as residual oil are extracted with a relatively low viscosity and relatively volatile water-immiscible light oil. The light oil-laden solids are then brought into direct contact with steam whereby the presence of the steam effectively reduces the boiling point of the water-immiscible light oil to effect its more efficient removal from the solids. Excess externally supplied steam and light oil vapor are used to supply heat to the overall process.