Abstract:
A process comprises the manufacture or preparation of fluorinated benzene, in particular monofluorobenzene, in a vapor-phase fluorination process. For example, the process can comprise a batch or continuous manufacture or preparation of fluorinated benzene, in particular monofluorobenzene, using hydrogen fluoride (HF) in gas phase as fluorination gas. Also, in this process, for example, fluorination catalysts are involved.
Abstract:
A process for the manufacture of a fluorinated benzene starting from benzoic acid by direct fluorination employing a fluorination gas, wherein the elemental fluorine (F2) is preferably present in a high concentration, and subsequent decarboxylation of the benzoic acid hypofluorite obtained by direct fluorination. And a process for the manufacture of a benzoic acid hypofluoriteby direct fluorination of benzoic acid. The fluorination process may be performed batch-wise or in a continuous manner. If the process is performed batch-wise, a column (tower) reactor may be used. If the process is continuous, a micro-reactor may be used.
Abstract:
A working fluid includes one or more halogenated compounds in an amount of at least 80 wt. %, based on the total weight of the working fluid. The working fluid also includes a colorant uniformly disposed throughout the working fluid in an amount such that the colorant is detectable to the unaided human eye. The working fluid is nonflammable.
Abstract:
A process is provided for the chlorination of ethane using chlorine as the chlorinating agent to produce hydrogen chloride (HCl) and vinyl chloride (VCM) and heavies.
Abstract:
The present invention relates, at least in part, to a process for making chlorotrifluoroethylene (CFO-1113) from 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a). In certain aspects, the process includes dehydrochlorinating 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof.
Abstract:
A method of making α,ω-diiodoperfluoroalkanes includes combining: diatomic iodine, at least one perfluoroalkylene oxide represented by the formula wherein Rf represents a perfluoroalkyl group; and at least one of: a) a first metallic compound comprising nickel, and a second metallic compound comprising molybdenum that is compositionally different from the first metallic compound; or b) a metallic alloy comprising from 50 to 70 percent by weight of nickel and from 20 to 40 percent by weight of molybdenum, based on the total weight of the metallic alloy, thereby producing at least one product represented by the formula I(CF2)nI, wherein n independently represents an integer in the range of from 1 to 11. The total weight of the at least one product wherein n is 3 or greater exceeds the total weight of the at least one product wherein n is 1 or 2 by a factor of at least 4.
Abstract:
Processes and systems that include use of a packed wet oxidation reactor for oxidizing aqueous metal bromide salts in a bromine-based process for converting lower molecular weight alkanes to higher molecular weight hydrocarbons. A stream comprising a dissolved metal bromide salt may be oxidized in a wet oxidation reactor comprising a packed section to produce at least a partially oxidized liquid stream comprising oxidized products of the metal bromide salt and a gaseous bromine stream comprising elemental bromine.
Abstract:
Process and system that include the conversion of alkyl bromides to higher molecular weight hydrocarbons in circulating catalyst reactor-regenerator systems. Alkyl bromides may be reacted over a catalyst in at least one conversion reactor to produce at least an effluent stream comprising higher molecular weight hydrocarbons and hydrogen bromide. A portion of the catalyst may be removed from the conversion reactor. The portion of the catalyst may be contacted with a stripping gas to displace hydrocarbons from the portion of the catalyst. The portion of the catalyst may be contacted a first inert gas. The portion of the catalyst may be contacted with oxygen to form a regenerated catalyst by removal of coke. The regenerated catalyst may be contacted with a second inert gas. At least a portion of the regenerated catalyst may be introduced into the conversion reactor.