Abstract: The present invention provides a method of effectively recovering a hydrocarbon halide and the use of a specific aprotic polar compound for said method. Thus, the present invention provides a method of recovering a hydrocarbon halide comprising absorbing the hydrocarbon halide into an aprotic polar compound which has a 5 or 6 membered ring and a nitrogen atom at an alpha-position of a carbonyl group. In the present method, the absorbed hydrocarbon halide can be easily recovered by usual methods.

Abstract: Chloroform cannot be completely separated from methanol, ethanol or isopropanol by conventional distillation or rectification because of the minimum boiling azeotrope between chloroform and the alcohols. Chloroform can be readily separated from methanol, ethanol or isopropanol by extractive distillation. Typical effective agents are: for methanol, isopropanol or 4-methyl-2-pentanone; for ethanol, n-butanol or isobutyl acetate; for isopropanol, butyl acetate or ethylene glycol ethyl ether.

Abstract: A radioactive decontamination method for decontaminating a radioactive-contaminated object by using methylene chloride in place of conventionally used hydrocarbon fluoride or perchloroethylene. The radioactive-contaminated object is impacted by methylene chloride solution. Before the impacting, a preparatory step is executed as required in which radioactive contaminant, which is usually radioactive-contaminated epoxy-resin paint layer on a part used in a nuclear facility, is impregnated with methylene chloride solution so as to swell, thus facilitating exfoliation of the contaminant from the object. The methylene chloride solution is filtered and distilled so as to be decontaminated and subjected to a repeated use for impacting the radioactive-contaminated object.

Abstract: Methylene chloride cannot be completely separated from ethyl vinyl ether by conventional distillation or rectification because of the minimum boiling azeotrope. Methylene chloride can be readily separated from ethyl vinyl ether by extractive distillation. Typical effective agents are ethylene glycol methyl ether acetate, 2-hexanone and 1-nitropropane.

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: Trichloroethylene cannot be completely separated from n-butanol, isobutanol, 2-butanol or t-butanol by conventional distillation or rectification because of the minimum boiling azeotropes. Trichloroethylene can be readily separated from n-butanol, isobutanol, 2-butanol or t-butanol by extractive distillation. Typical effective agents are: for n-butanol, dimethylsulfoxide; for isobutanol, n-octanol; for 2-butanol, 2-methyl-1-pentanol and for t-butanol, n-butyl acetate.

Abstract: This invention concerns the decolorizing and/or deacidifying of methyl bromide materials by contacting same with zinc.

Abstract: A method of inhibiting fouling in a crude ethylene dichloride stream comprises introducing into the stream an inhibiting amount of an antifoulant selected from (A) an acylated amine (e.g., reaction product of polyisobutylene and maleic anhydride) and a polyamine (B) magnesium alkyl aryl sulfonate, and (C) a mixture of A and B.

Abstract: 1,1,1-Trichloroethane cannot be completely separated from n-hexane by conventional distillation or rectification because of the minimum boiling azeotrope. 1,1,1-Trichloroethane can be readily separated from n-hexane by extractive distillation. Typical effective agents are: methyl isoamyl ketone, amyl acetate and isobutanol.

Abstract: Methylene chloride cannot be completely separated from methyl formate or ethyl formate by conventional distillation or rectification because of the minimum boiling azeotrope. Methylene chloride can be readily separated from methyl formate or ethyl formate by extractive distillation. Typical effective agents are: for methyl formate, n-butyl acetate and 3-hexanone; for ethyl formate, isobornyl acetate and 2-heptanone.

Abstract: Ethyl ester cannot be completely separated from methylene chloride by conventional distillation or rectification because of the maximum boiling azeotrope. Ethyl ether can be readily separated from methylene chloride by extractive distillation. Typical effective agents are t-butyl alcohol, n-propyl acetate or propoxypropanol.

Abstract: A flame retardant product predominant in hexabromocyclododecane is prepared and dried by a process wherein gaseous ammonia is injected into the dryer system to prevent the formation of color bodies which contaminant the product.

Abstract: The invention relates to a process for purifying unreacted 1,2-dichloroethane from a 1,2-dichloroethane pyrolysis process by chlorinating the benzene produced as a by-product and removing the chlorination products by distillation.

Abstract: Methylal cannot be completely separated from methylene chloride by conventional distallation or rectification because of the maximum boiling azeotrope. Methylal can be readily separated from methylene chloride by extractive distillation. Typical effective agents are n-butyl acetate, diisobutyl ether and 4-methyl-2-pentanone.

Abstract: The present invention relates to a process for the treatment of heavy residues produced in the manufacture of chlorinated products, in which process a chemical compound chosen from certain fatty compounds is added to the heavy residues in order to form fluid and stable liquid suspensions.

Abstract: A process for the dehydrohalogenation of a feed comprised of an admixture of primary, secondary and tertiary alkylhalides to selectively convert the secondary and tertiary alkylhalides of the admixture to olefins by dehydrohalogenation, with minimal conversion, if any, of the primary alkylhalides. The reaction, which is particularly applicable to the selective dehydrobromination of an admixture of primary, secondary and tertiary alkylbromides, is carried out in a distillation-reaction zone, column, or distillation-reactor, to simultaneously (i) convert the secondary and tertiary alkylbromides to olefins and hydrogen bromide, and (ii) separate the olefins and hydrogen bromide, (iii) and the primary alkyl bromides, from the reaction mixture.

Abstract: Hydrogen chloride evolution is reduced in the distillation of chloroform from its admixture with an amide solvent when in contact with stainless steel, by incorporation of certain tertiary aliphatic amines.

Abstract: Free chlorine values are removed by radical chlorination from uncombined admixtures thereof, notably admixtures of free chlorine and at least one halogenated organic compound that is not completely chloro-substituted.

Abstract: Industrial grade chloroform is purified to remove traces of cis-1,2-dichloroethylene, bromochloromethane, and amylenes by a two-step process. The chloroform is first treated by contacting with aqueous sulfuric acid to remove amylenes and thereafter passed over a zeolite having an average pore size of 3 to 6 Angstroms and a Si/Al atomic ratio in the range of about 1.6/1 to 3/1, preferably calcium chabazite, to remove cis-1,2-dichloroethylene and bromochloromethane.

Abstract: Off-color liquid ortho-chloro-para-xylene compositions are decolorized by contacting the compositions with particles of diatomaceous silica, magnesium oxide or soda ash.

Abstract: A method for producing dichloroethane (EDC) by reacting ethylene and chlorine in a liquid reaction medium composed mainly of EDC at a temperature of not less than the boiling point of EDC measured at ordinary pressure, characterized by leading the vapor of the reaction medium generated in a reactor from the top of the reactor to a heat exchanger so as to recover and utilize the latent heat resulting from condensation of the vapor in the heat exchanger. According to the present invention, high heat utilization efficiency can be attained with advantages as compared with conventional EDC production methods.

Abstract: The oxychlorination process for producing ethylene dichloride is carried out by reacting ethylene with hydrogen chloride and oxygen in an oxychlorination reactor. Thereby, ethyl chloride and perhaps vinyl chloride are produced as by-products. The effluent from the reactor is at least fractionated into an ethylene dichloride-rich fraction (I) and an ethyl chloride-rich fraction (II) so that fraction (I) contains less than 50 percent of the total weight of ethyl chloride produced in step (a) and the sum of the weight of ethylene dichloride and vinyl chloride in fraction (II) is less than 30 percent of the weight of ethyl chloride in fraction (II). The ethyl chloride-rich fraction (II) is subjected to a cracking reaction in the presence or absence of an inert diluent wherein ethyl chloride is converted into ethylene and hydrogen chloride in the presence of a catalyst.

Abstract: A catalyst, such as FeCl.sub.3, useful in the production of chlorinated hydrocarbons such as 1,1-dichloroethane is removed from the effluent of a process reactor and recycled. Hydrochloric acid is removed from the process stream resulting in the catalyst present in the process stream in solution precipitating out of solution. Then it can be removed from the process stream by conventional separation techniques. Alternatively, the catalyst present in the process stream as a solid, without the removal of HCl, is separated from the liquid present by means of a cyclone and recycled. In both cases, the catalyst retains its catalytic activity.

Abstract: The water content of crude 1,2-dichloroethane compositions containing chloral hydrate is reduced by stripping under superatmospheric pressure.

Abstract: Under certain operating conditions, an emulsion of an acidified unfiltrable tarry bottoms stream from a reactor for the chlorination of ethylene to 1,2-dichloroethane can be demulsified and separated in a phase separation tank. The presence of FeCl.sub.3 in an amount more than 5 ppm Fe in the separated organic waste, fouls the reboiler and lower internals of a "heavies" column in which the separated organic waste is concentrated, and deactivates the catalyst in a Catoxid fluid bed reactor in which the concentrate is burned. By maintaining an iron salt chlorination catalyst in a concentration which results in 2000 ppm to 4000 ppm of Fe in the HTC reactor bottoms, and operating the HTC reactor at a temperature in the range from about 90.degree. C. to 120.degree. C. and a pressure in the range from 9 psig to 12 psig, an unfiltrable reactor bottoms drawoff is produced which may be acidified without forming an emulsion.

Abstract: A process is described for the removal of dimethyl ether in methyl chloride by catalytic cleavage by means of hydrogen chloride. Dimethyl ether is present as an impurity in crude methyl chloride produced by the catalytic esterification of methanol. The crude methyl chloride is cooled so that water and hydrogen chloride separate out. Gaseous hydrogen chloride is then added to the methyl chloride in an amount corresponding to at least twice the molar amount of dimethyl ether, and the gaseous mixture is passed over a methanol esterification contact catalyst at an elevated temperature.

Abstract: An improved method of producing vinyl chloride by pyrolysis of purified 1,2-dichloroethane at temperatures from 480.degree. C. to 540.degree. C. at a pressure of 10 to 36 bar absolute with partial utilization of the heat content of the flue gases from the pyrolysis furnace firing to preheat liquid 1,2-dichloroethane almost to its boiling temperature utilizing the flue gas waste heat to generate steam, cool the pyrolysis gas mixture in several stages and separate the hydrogen chloride from the pyrolysis gas mix in a hydrogen chloride column as well as separate vinyl chloride from the pyrolysis gas mix in a vinyl chloride monomer column.

Abstract: A process for recovering brominated acenaphthylene and its condensate in the form of powder, comprising dropping a solution of brominated acenaphthylene and its condensate produced from acenaphthene by reactions of bromination, condensation and dehydrobromination into hot water containing a carboxylic acid ester of polyoxyalkylene sorbitan, while the solvent is being distilled off, to recover the brominated acenaphthylene and its condensate in the form of powder dispersed in water.

Abstract: In a process for producing 1,2-dichloroethane or ethylene dichloride ("EDC") in a high temperature direct chlorination ("HTDC") reactor in which ethylene is reacted with wet chlorine having a water content more than 100 ppm but no more than 1% by wt of the chlorine, the water leaves the reactor with the EDC product draw-off, either in the vapor overhead (if the HTDC is a boiling reactor), or, as a liquid sidestream (if the HTDC is a non-boiling reactor). In a subsequent step, the EDC draw-off is distilled in a product distillation column in which the water leaves in the overhead which is condensed to remove condensables in a first stage, and vent a non-condensable vent streams. The vent stream is corrosive due to the presence of minor amounts of chlorine, HCl and water, along with oxygen which is injected into the HTDC to improve selectivity of the reaction. The vent gases from the first stage are further cooled to a temperature in the range from about -30.degree. C. to about 0.degree. C.

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: Olefins containing at least 7 carbon atoms are used to remove molecular chlorine form compositions comprising 1,2-dichloroethane and a contaminating amount of molecular chlorine.

Abstract: Ferric chloride contained in liquid waste streams comprising higher boiling chlorinated hydrocarbons may be substantially reduced by contacting the waste stream with an amount of water sufficient to convert a substantial amount of the ferric chloride in said stream to solid ferric chloride hexahydrate, and then removing the solid hexahydrate from the waste stream for instance by filtration.

Abstract: A process is disclosed for the economical operation of a commercial ethylene dichloride (EDC) cracking furnace which typically is prone to coking of the tubes through which the EDC is flowed. The EDC cracking furnace is found to be critically sensitive to the presence of trace amounts, 30 ppm or more of FeCl.sub.3 and/or 20 ppm or more of free chlorine, which cause coking of the tubes of the furnace. The coking of the tubes is minimized by maintaining less than 30 ppm by weight of FeCl.sub.3 or less than 20 ppm of free chlorine in the EDC feed to the EDC furnace. In the particular instance where EDC is produced at least in part in a high temperature direct chlorination ("boiling") reactor constructed from mild steel, this goal requires that the chlorine content of the effluent from the boiling reactor be controlled so as not to exceed 20 ppm. But this is to be done without using more than a 2% by weight excess of ethylene over the stoichiometric amount required to produce the EDC in the boiling reactor.

Abstract: Hydrogen chloride is recovered from a mixture with propylene by extractive distillation with an inert extraction solvent to minimize reaction between hydrogen chloride and propylene during such distillation. The temperature and pressure conditions are coordinated with the extraction solvent and amount thereof to prevent the presence of hydrogen chloride in a liquid state. The process is particularly suitable for recovering hydrogen chloride in the production of allyl chloride by thermal chlorination of propylene.

Abstract: A trace amount of free chlorine, present along with comparable amounts of ethylene, oxygen and water vapor in the ethylene dichloride (EDC) effluent from a direct chlorination reactor, may be effectively scavenged by exposing the effluent to ultraviolet ("u-v") light having a wavelength less than about 4000.ANG. which is absorbed by the chlorine, but to which both ethylene and EDC are essentially transparent. In this process, contaminant chlorine in substantially pure (99..sup.+ %) EDC is catalytically activated and reacts with EDC to form an unwanted byproduct, namely 1,1,2-trichloroethane ("triane"). The process is effective in either the gaseous phase or the liquid phase.

Abstract: An improvement of a method for purifying 1,2-dichloroethane by passing through a distillation column a crude 1,2-dichloroethane produced by oxychlorination of ethylene with at least one of a crude 1,2-dichloroethane produced by direct chlorination of ethylene and a crude uncracked 1,2-dichloroethane recovered in thermal cracking of 1,2-dichloroethane, the improvement which comprises feeding the oxychlorination-produced 1,2-dichloroethane to an upper plate of the distillation column which is above a plate of the column to which at least one of the direct chlorination-produced 1,2-dichloroethane and the uncracked 1,2-dichloroethane is fed, and recovering 1,2-dichloroethane as a bottom product. The purification method is very useful in the production of vinyl chloride by thermal cracking of 1,2-dichloroethane since carbon tetrachloride effective as a thermal cracking catalyst is recovered in concentrations stabilized within the range of .+-.500 p.p.m.

Abstract: The reaction gases from the chlorination of methane and preferably also methyl chloride, after removal of the HCl and drying, are subjected to the steps of partially condensing the dried stream of reaction gases at a pressure of 5-15 bars and at a temperature of 0.degree.-40.degree. C. which condenses the chloroform and the carbon tetrachloride; contacting the gaseous phase of the partially condensed stream of reaction gases in a countercurrent manner with a stream of liquid methyl chloride; recycling the stream of gases discharging from the contacting stream of liquid methyl chloride to the chlorination stage; and fractionating the contacting stream of liquid methyl chloride.

Abstract: Ferric iron is removed from chlorinated hydrocarbons having less than 6 carbon atoms per molecule by intimately contacting the latter with an oil that comprises one or more hydrocarbons having at least 6 concatenated aliphatic carbon atoms per molecule. The hydrocarbon oil is present in an amount sufficient to interact with a major portion of the ferric iron. The resulting mixture of the chlorinated hydrocarbon stream and the hydrocarbon oil is heated simultaneously with the intimate contacting, and a precipitate is allowed to form. The chlorinated hydrocarbon stream is then separated from the hydrocarbon oil and from the precipitate, and the precipitate is subsequently separated from the hydrocarbon oil, which may be recycled and re-used.

Abstract: Apparatus for recovering chlorocarbons from a vent gas stream which additionally contains a halogen, including an inlet means connected to a source of the gas stream and a heat exchanger means for receiving the stream from the inlet means. The heat exchange means has a cooling capacity sufficient to reduce the temperature of the stream to less than about -60.degree. F. at a pressure of at least 60 psig. Finally, separator means are provided for receiving the stream at the reduced temperature and include means for separating the liquid from the vapor at that point.The apparatus and the method of using the same is particularly suited for use with vent gas streams containing at least 1000 ppm of carbon tetrachloride and approximately 0.2 to 20% of a halogen, particularly chlorine, based upon the weight of the carbon tetrachloride. Preferred operating conditions are from about -60.degree. F. to about -70.degree. F. at a pressure ranging from 80 to 90 psig.

Abstract: A process for the treatment of heavy products resulting from the manufacture of light hydrocarbons. The heavy products are subjected to steam distillation in the presence of a water-soluble surface-active agent.

Abstract: Halogenated hydrocarbon and uncontaminated water is recovered from a stream of process water contaminated with halogenated hydrocarbon and hydrogen halide. The process water is neutralized and then distilled to obtain a first fraction containing halogenated hydrocarbon and water and a second fraction containing uncontaminated water. The first fraction is allowed to settle into layers of halogenated hydrocarbon and water which are then removed.The contaminated stream may be obtained from a process for the solvent dewaxing of a petroleum fraction.

Abstract: An improvement of a method for purifying 1,2-dichloroethane by passing through a distillation column a crude 1,2-dichloroethane produced by oxychlorination of ethylene with at least one of a crude 1,2-dichloroethane produced by direct chlorination of ethylene and a crude uncracked 1,2-dichloroethane recovered in thermal cracking of 1,2-dichloroethane, the improvement which comprises feeding the oxychlorination-produced 1,2-dichloroethane to an upper plate of the distillation column than a plate of the column to which at least one of the direct chlorination-produced 1,2-dichloroethane and the uncracked 1,2-dichloroethane is fed, and recovering 1,2-dichloroethane as a bottom product.

Abstract: Ethylene dichloride is separated from unsaturated organic impurities such as trichloroethylene and benzene by extractive distillation in the presence of a high boiling chloroalkene solvent, such as perchloroethylene.

Abstract: The method of removing fluorinated olefin byproduct formed during the synthesis of a fluoromethylhexafluoroisopropyl ether product or the like comprises: adding ammonia or an amine to the mixture to react with the fluorinated olefin byproduct, and thereafter distilling the fluoromethylhexafluoroisopropyl ether product to remove it from the byproduct.

Abstract: Methylchloroform undergoing purification distillation is stabilized against decomposition by conducting the distillation in the presence of polyalkylene glycol having an average molecular weight greater than 150.

Abstract: 1,1,1-trichloroethane is recovered in an excellent yield from textile material without deterioration in quality of the textile material by a method in which a textile material is introduced into a hot water bath having a temperature of 64.degree. C. or more and a pH of 4.0 or more, so as to allow 1,1,1-trichloroethane to vaporize together with water, the mixture of vapors of 1,1,1-trichloroethane and water is condensed by cooling it, and then, the condensed 1,1,1-trichloroethane is separated from the condensed water.

Abstract: After quenching the effluent gas from a methanol hydrochlorination reactor to condense most of the water and remove excess HCl, the wet (saturated) methyl chloride is mixed with hydrogen chloride to provide a gas mixture having a methyl chloride:HCl ratio of from about 0.4:1 to about 4:1. This mixture is then contacted with cold (-16.degree. to -21.degree. C.) concentrated (50 to 59%) aqeous hydrochloric acid to remove the water to a low level. Additionally an undesirable by-product, dimethylether, is removed along with the water. Alternatively the wet gas mixture may be cooled to that same temperature by passing over cooling coils, or other convenient means, to remove the water.

Abstract: Ferric iron is removed from chlorinated hydrocarbons having less than 6 carbon atoms per molecule by intimately contacting the latter with an oil that comprises one or more hydrocarbons having at least 6 carbon atoms per molecule. The hydrocarbon oil is present in an amount sufficient to interact with a major portion of the ferric iron. The resulting mixture of the chlorinated hydrocarbon stream and the hydrocarbon oil is heated simultaneously with the intimate contacting, and a precipitate is allowed to form. The chlorinated hydrocarbon stream is then separated from the hydrocarbon oil and from the precipitate, and the precipitate is subsequently separated from the hydrocarbon oil.

Abstract: In recovering the multi-solvent portion of the oil solvent mixture in a solvent dewaxing process, decomposition of a thermally unstable, lower boiling solvent component is substantially avoided by recovering the solvent in a series of controlled evaporations whereby the major portion of the lower boiling solvent component is removed from the mixture prior to the removal of the remaining portion of the solvent. The solvent removal may be conducted in a high pressure evaporator having an upper section and a lower section separated by an annular tray.

Abstract: The invention relates to a process for purifying 1,2-dichloroethane which is recovered during incomplete thermal cracking to vinyl chloride and contains contaminants boiling at a temperature lower than 83.7.degree. C. under a pressure of 1011 millibars, briefly termed low boilers, and contaminants boiling at a temperature higher than 83.7.degree. C. under a pressure of 1011 millibars, briefly termed high boilers. More particularly, low boilers are distilled off overhead from contaminated 1,2-dichloroethane, in a first distilling zone; a portion of low boiler concentrate is continuously treated at 30.degree. to 85.degree. C.