The method of obtaining pentafluoroethane and/or freon
(57) Abstract:The invention relates to the development of industrial technology for Pentafluoroethane and/or freon fluoridation of paliperidone - titrator, trifter-defloration or their mixtures with cobalt TRIFLUORIDE. The process at 220 - 390oC and the concentration of active fluorine in the cobalt TRIFLUORIDE 5 to 12% can achieve output Pentafluoroethane to 67%, freon - up to 94% at high speed feeding of the original product. The optimum temperature for obtaining pentatomoidea - 220 - 260oC, to obtain freon - 320 - 390oC. for 3 h.p. f-crystals, 1 table. The invention relates to methods for pendaftar and/or geksaftorida by fluorination of poliferation of Tetrafluoroethane or triptorelin or diflorasone, as well as their mixtures higher fluorides of metals of variable valence, in particular, cobalt TRIFLUORIDE (CoF3).Pendaftar and HEXAFLUOROETHANE that have zero ozone-depleting potential are promising substitutes OzonAction halocarbons and are used as refrigerants, chemicals for dry etching in the manufacture of integrated circuits and otherKnown with whom ratanov with fewer fluorine atoms CoF3how you can develop low-waste industrial technology, because the substitution of hydrogen by fluorine forms only one by-product hydrogen fluoride.These methods involve laboratory method of fluorination of toratenu - Cryptor and Tetrafluoroethane at temperatures up to 170oC, supplied in a mixture with nitrogen (Journal of the Amtrican Chemical Society, 1950, No. 11, R. 4883). According to the information provided in the fluoridation of 1,1,2-triptorelin received 45% of 1,1,2,2-Tetrafluoroethane, 35% Pentafluoroethane, the content of unreacted raw product in the reaction mixture not specified. When fluoridation 1,1,2,2-Tetrafluoroethane received 50% of Pentafluoroethane and 10% freon, the contents of the original product in the reaction mixture is 40% decomposition or side connections are present. The process was conducted in a typical periodic reactor with a stirrer with flow source Tetrafluoroethane 8 cm3/h with a variable concentration of active fluorine in CoF3from 16% (immediately after regeneration) to almost zero content (before regeneration).This method is adopted for the prototype because of other publications on the fluoridation of Tetrafluoroethane and triptorelin not found.However, a number and a very small flow of the original fluorine-containing compounds, due to the need for maintaining the temperature for a given level;
the yield of the target products containing more than the initial compound amounts of fluoride, and the conversion of the original product is not high enough.The objective of the invention to develop a process suitable for industrial implementation, it is necessary to increase the conversion of the original product and the yield of the target compounds with minimal formation of the degradation products at high productivity due to the optimum conditions of the process of fluoridation.For solving the problem have been conducted a number of studies and experimentally established that in case of further fluorination polyfluorinated saturated aliphatic compounds, including trifter and tetraborates and differetn for optimum heat and mass transfer in the reaction zone, in addition to the optimal temperature regulated flow of the original product and heat, it is necessary that the concentration of active fluorine in CoF3it was constant and was in the range of 5 to 12% of the process Temperature 220 390oC. in the case of pre-emptive get Pentafluoroethane must maintain a temperature of 220 260
FIELD: chemical industry, in particular method for production of value products from lower alkanes.
SUBSTANCE: claimed method includes passing of gaseous reaction mixture containing at least one lower alkane and elementary chlorine through catalytic layer. Used catalyst represents geometrically structured system comprising microfiber with diameter of 5-20 mum. Catalyst has active centers having in IR-spectra of adsorbed ammonia absorption band with wave numbers in region of ν = 1410-1440 cm-1, and contains one platinum group metal as active component, and glass-fiber carrier. Carrier has in NMR29Si-specrum lines with chemical shifts of -100±3 ppm (Q3-line) and -110±3 ppm (Q4-line) in integral intensity ratio Q3/Q4 from 0.7 to 1.2; in IR-specrum it has absorption band of hydroxyls with wave number of ν = 3620-3650 cm-1 and half-width of 65-75 cm-1, and has density, measured by BET-method using argon thermal desorption, SAr = 0.5-30 m2/g, and specific surface, measured by alkali titration, SNa = 10-250 m2/g in ratio of SAr/SNa = 5-30.
EFFECT: method of increased yield.
3 cl, 4 ex
FIELD: organic chemistry, chemical technology, petroleum-chemical synthesis.
SUBSTANCE: invention relates to a method for preparing liquid chloroparaffins. Liquid chloroparaffins are prepared by the hydrochlorination reaction of olefin with hydrogen chloride in the presence of a catalyst wherein α-olefins of (C18-C28)-fraction are used as olefins and water is used as a catalyst taken in the amount 0.02-0.03 wt.-%. The hydrochlorination reaction is carried out at temperature 20-25°C and the volume feeding rate of hydrogen chloride 21-24 h-1 followed by chlorination of the prepared reaction mass with chlorine in the presence of zeolite CaX taken in the amount 2-3 wt.-% at temperature 80-90° and the volume feeding rate of chlorine 19-22 h-1. Using this process promotes to increasing conversion of HCl and chloroolefin, enhances the yield of products, simplifying and reducing cost of the process.
EFFECT: improved preparing method.
2 cl, 7 tbl, 7 ex
FIELD: organic chemistry, chemical technology.
SUBSTANCE: invention relates to processes for the oxidative halogenation reaction of hydrocarbons, in particular, for synthesis of haloidmethanes, their following processing to value chemical compounds. Method involves contacting methane, halogenated methane or their mixture with halogen source and oxygen source in the presence of catalyst to yield halogenated C1-hydrocarbon having more amount of halogen substitutes as compared with the parent hydrocarbon, Process is carried out at temperature above 200°C but less 600°C and under pressure 97 kPa or above but less 1.034 kPa and at the volume rate of raw feeding above 0.1 h-1 but less 100 h-1. Catalyst comprises rare earth metal halide or oxyhalide no containing iron and copper. The atomic ratio of rare-earth element to iron or copper exceeds 10:1 under condition that if catalyst comprises cerium in the amount less 10 atomic percent of the total amount of rare-earth components then catalyst comprises also one additional rare-earth element. Reacting hydrocarbon is chosen from the group consisting of methane, chloromethane, bromomethane, iodomethane, dichloromethane, dibromomethane, diiodomethane, chlorobromomethane and their mixtures. The molar ratio of hydrocarbon to halogen is above 1;1 but less 20:1 and that to oxygen is above 2:1 but less 20:1. The reaction mixture comprises additionally a diluting agent as nitrogen, helium, argon, carbon monoxide or dioxide or their mixtures. Formed methyl chloride or methyl bromide can be fed to the hydrolysis step to yield methyl alcohol or used in process of catalytic condensation to form light olefins and/or gasolines. It is possible contacting methyl halide with the condensation catalyst to form ethylene and the following preparing vinyl halide monomer, for example, vinyl chloride or acetic acid under carbonylation conditions. Invention provides enhancing output of the process at the expense of using the effective modified catalyst based on rare-earth elements.
EFFECT: improved halogenation method.
33 cl, 1 tbl, 1 ex
FIELD: chemical industry; apparatuses for production of the chlorinated allyl.
SUBSTANCE: the invention presents the reactor for production of the chlorinated allyl intended for realization of the method of production of the chlorinated allyl by the direct gaseous phase chlorination of the propylene. The reactor includes the closed circuit of circulation of the reaction gases, the devices of injection of the source propylene and chlorine, the device of the forced circulation of the part of the reaction gases and the device of withdrawal of the other part of the reaction gases. At that the closed circuit of the reaction gases circulation forms the jet pump, which includes in series connected the reception chamber, the mixing chamber and the diffuser, and the pipe of the circulation circuit connecting the outlet of the diffuser with the appropriate inlet of the reception chamber of the injector and acting as the main reaction zone of the ideal displacement with the presence time of 0.7-0.9 s, in which the scatter of the temperatures does not exceed ±10°С. The reception chamber contains the nozzles used as the devices for injection of the source propylene and chlorine. The jet pump ensures fulfillment of the concerted functions: introduction of the streams of the source propylene and chlorine, which are the working injecting streams; the forced circulation pump with the repetition factor of 5-10 of the reaction gases stream, which is the injected stream; the high-velocity mixer and the preheater of the source reactants in the mixing chamber due to the strong turbulence during (0.01-0.04)s, which is formed by the combination of the nozzles of the injected gases at the arrangement of the nozzle/ nozzles of the chlorine coaxially to the main nozzle of the propylene arranged on the shaft of the mixing chamber. The technical result of the invention is, that the presented design of the reactor allows to increase the selectivity of the process of production of the chlorinated allyl.
EFFECT: the invention provides, that the presented design of the reactor allows to increase the selectivity of the process of production of the chlorinated allyl.
1 ex, 1 dwg
FIELD: chemical industry; methods of production of the chloroform.
SUBSTANCE: the invention is pertaining to the method of production of the chloroform by chlorination of methylene chloride in the liquid phase at the temperature of 35-50°С at photoinitiation with the subsequent separation of the chloroform by rectification. At that before the chlorination methylene chloride is saturated with chlorine, and for chlorination feed the solution of chlorine in methylene chloride. The methylene chloride is saturated in the darkness, the saturation is conducted by the electrolysis chlorine with separation of the volatile components - hydrogen, nitrogen, oxygen present in the electrolysis chlorine, from the solution of the chlorine in methylene chloride at the temperature being within the limits from minus 10 up to plus 5°С, in the counter-currentmode at sprinkling of the absorption column by the cooled methylene chloride or in the bubbling mode in the conditions of bubbling by the electrolysis chlorine through the cooled methylene chloride. The technical result of the invention is suppression of the inhibition of the process of chlorination of the methylene chloride at usage of the electrolysis chlorine, the increase of conversion of chlorine and selectivity for chloroform.
EFFECT: the invention ensures suppression of the inhibition of the chlorination process of methylene chloride at usage of the electrolysis chlorine, the increased conversion of chlorine and selectivity for chloroform.
5 cl, 4 ex, 1 tbl