The method of producing allylchloride and reactor for its implementation

 

(57) Abstract:

Describes how to obtain allylchloride gas-phase chlorination of propylene under pressure at 420-470°C. Chlorination are in a confined reaction path with forced circulation of the reaction gases. The feed gas is separated at a molar ratio of propylene and chlorine is 1.2 to 3.0 : 1.0, the ratio of the volume of the circulating gases and the output is 1-30 : 1. Also described reactor for implementing the method, in which the feed area of the initial reagents and the tubular reactor to form a single closed loop in the cavity which are devices for forced circulation, input, chlorine, propylene and the discharge device of the gaseous products. These devices have a certain location. Technical result - increase the selectivity of the process. 2 S. p. f-crystals, 1 tab., 1 Il.

Group of inventions relates to the chemistry and technology of halogenoalkanes compounds, in particular to a method of producing allylchloride and reactor for its implementation.

Allylchloride is an intermediate for a number of organic production - allyl alcohol, epichlorohydrin, glycerol, etc.

The known method of gas-phase is, at a temperature of 450-530oC and a pressure of 1-3 kg/cm2in the reactor, which has three working areas. In highly turbulent zone of intense mixing of the reagents, the temperature quickly rises to 450-530oC. In the zone of intensive recirculation of reaction occurs in the largest extent. In the last zone of mixing of the reaction is finished (1) /patent CPP N 57828, class C 07 C 17/02, B 01 J 11/00, 1974/.

The disadvantage of this method is the high temperature, its wide range, resulting in reduced selectivity of the chlorination reaction to the target product.

This method is carried out in a special reactor. The reactor is a vertical metal tube with a ratio of height to diameter (D) 15:1-30: 1, is provided in the lower part of the cooling system and continue from the top nozzle ejector type, inside the shape of a truncated cone, extending downward (d - small diameter, d1- large diameter of the cone, the ratio of the height: d1= 2:1-5:1 and d:d1= 0.1:l to 0.7:1). Truncated cone - zone A highly turbulent zone, limited downwards by the intersection of imaginary extensions forming a cone with the walls of the tube zone B - zone mixing with intensive recycling, the rest of the tube-elendra. From the inner cylinder surrounded by a water jacket, through duzu in the reactor comes chlorine, and through the annular section between duty and the external cylinder - hydrocarbon (1).

The disadvantage of this reactor is that its design does not provide the optimal parameters of the chlorination process and requires additional energy consumption for preheating the hydrocarbon feedstock.

The closest to the technical nature of the claimed group of inventions is a method of obtaining allylchloride, which consists in the interaction of propylene with halogen at a molar ratio of not less than 2.5:1.0 at a temperature of 400-525oC (2) /W 09637450, class C 07 C 17/10, 28.11.96/.

This method is carried out in a reactor having two working zones. In the feed area of the source reagent is a mixture of propylene and halogen at a temperature of 400-525oC. After which the reaction products are displayed in the area where the reaction proceeds at a temperature of 400-525oC until complete conversion of the chlorine.

The disadvantage of this method is that the chlorination process occurs with the presence of areas of high concentrations of chlorine at a high temperature of the reaction mixture in zone mixed with the chlorine is all, affects the selectivity of the process, i.e., leads to its reduction, especially to increased output high and trudnoperevarivaemym products.

The closest reactor of the same purposes of the claimed device in the group of inventions on the totality of symptoms is the reactor that includes a feed area of the initial reagents, tubular zone, connected to the feed area of the source components, one or more devices supplying gaseous reagents in the appropriate zone, and one or more discharge devices of the tubular part of the reactor (2).

For reasons that impede the achievement of specified following technical result when using the known device, taken as a prototype, is that its design contributes to the process of chlorination of propylene in unmanaged temperature in the feeding zone of the initial reagents. Completion of the process in the device occurs at high temperatures, which also leads to a reduction considered horizontally isothermal surface and, consequently, to increased output high products.

When high-temperature chlorination of propylene in substantial excess of propylene are formed, in the main, MES is Denmark 1,2-dichloropropane to monochloropropane.

At temperatures below 400oC chlorine attached to propylene mainly at the double bond with the formation of 1,2-dichloropropane, the disposal of which requires significant resources due to the high complexity of its processing.

At temperatures 430-460oC chlorine interacts with propylene mainly with the formation of substitution products of the chlorination of propylene - monochloropropane, 95-97% of 3-chloropropanol-1 (allylchloride).

Further chlorination of monochloropropane, in turn, leads to the formation of mixtures of isomeric dichloropropanol. Moreover, at temperatures above 460oC the reaction rate of substitution chlorination of monochloropropane be commensurate with the reaction rates of substitution chlorination of propylene. In addition, the prolonged stay of the propylene feedstock, monochloropropane and, especially, dichloropropanol in the zone temperatures above 460oC is an intensive process their oligomerization and decomposition with the formation of products of osmola and soot, aggravated by contact with the heated surfaces of the walls of the reactor.

A single task, which directed the claimed group of inventions is increases the nd considered horizontally isothermal surface process.

Unified technical result in the implementation of a group of inventions is that with the increase of selectivity of the process decreases the quantity of generated by-products per unit of finished product.

Specified single technical result in the exercise of invention the object of the method is achieved in that in the known method of producing allylchloride gas-phase chlorination of propylene under pressure at a temperature of 420-470oC, the peculiarity lies in the fact that the chlorination process are in a confined reaction path with forced circulation of the reaction gases with separate supply and a molar ratio of propylene and chlorine 1.2-3.0: 1.0, and the ratio of the volume of circulating in the reaction path and the output from the gas is 1-30:1.

The process of obtaining allylchloride gas-phase thermal chlorination of propylene increases output allylchloride due to the high selectivity of the process. High selectivity is achieved by creating conditions maximum considered horizontally isothermal surface, i.e., the process of chlorination at a temperature of 420-470oC. Forced circulation of the reaction mixture with the times is as propylene and chlorine, ensure maximum considered horizontally isothermal surface process, because the relatively cool propylene, mixed with the reaction gases, removes excess exothermic heat of reaction. Forced circulation of the reaction gases in a closed circuit provides maximum mixing of reagents and reaction gases, providing extremely low current concentration of chlorine in the flow of the reaction gases, as well as intensive recycling and heat transfer.

Specified single technical result in the exercise of invention the object of the reactor is achieved by the fact that in the known reactor to obtain allylchloride, including the areas of supply of the raw materials, the tubular area, connected with the filing of the original reagents, equipped with devices supplying gaseous reagents in the appropriate zone, and the exhaust device of the tubular part of the reactor, the peculiarity lies in the fact that the area of supply of the raw materials and the tubular reactor to form a single closed loop in the cavity which has a device for forced circulation, with the location of the input device propylene until a forced circulation, input devices chlorine - before or sobrannyh products before input device propylene.

The reactor works as follows: propylene and chlorine in a molar ratio of 1.2:1-3.0:1, serves in an enclosed reaction space through the input device, the initial reagents. Enter propylene is set to the forced circulation device and the input device, chlorine, so relatively cool propylene, mixed with the reaction gases, removes excess exothermic heat of reaction of chlorination, thus in the reactor temperature is maintained at 420-470oC, providing optimal izotonicnosti the chlorination process. The circulation of the reaction mixture is performed by a special device located in the cavity of the reactor. Recirculation of the reaction gases and intensive mixing is provided by forced circulation with multiplicity 1-30. The conclusion of the reaction gas passes through the discharge device located before the input device of propylene. The output of allylchloride the propylene is 89.71-93.41%.

The claimed group of inventions to meet the requirement of unity of invention, since the group of runobject inventions form a single inventive concept, and one of the claimed objectivation substitution chlorination of propylene, in this case, both the object aimed at solving the same problem for a single technical result.

The method of producing allylchloride gas-phase substitution chlorination of propylene tested on bench installed in the specified conditions at a load of initial reagents in the reactor chlorination (see drawing) 4.5-5.5 kg/H. the results of the examples given in the table.

Example 1. In the reactor, which represents the closed loop pipeline, provided with a device for forced circulation of the reaction mixture, input devices starting reagents and reaction products, is served propylene and chlorine in a molar ratio equal to 2.0:1.0. Temperature chlorination 438-450oC. the Reaction mixture is subjected to circulation in a closed loop reactor with multiplicity circulation, equal to 15.0. The reaction gases are directed to a number of 4.5-5.5 kg/h Output allylchloride the propylene is 89.71% (mole.).

Example 2. Analogously to example 1, the process is carried out at a molar ratio of propylene and chlorine, equal to 2.2:1.0, temperature chlorination 442-460oC and the rate of circulation of the reaction mixture equal to 8.0. The output of allylchloride is 89.18% (mole.).

Example 3. Similarly, PR is 50-460oC and the rate of circulation of the reaction mixture equal to 19.0. The output of allylchloride is 91.61% (mole.).

Example 4. Analogously to example 1, the process is carried out at a molar ratio of propylene and chlorine, equal to 2.7:1.0, temperature chlorination 430-437oC and the rate of circulation of the reaction mixture, equal to 15.3. The output of allylchloride is 93.41% (mole.).

Example 5. Analogously to example 1, the process is carried out at a molar ratio of propylene and chlorine, equal to 2.8:1.0, temperature chlorination 445-460oC and the rate of circulation of the reaction mixture, equal to 6.8. The output of allylchloride is 90.62% (mole.).

Example 6. Analogously to example 1, the process is carried out at a molar ratio of propylene and chlorine, equal to 2.9:1.0, temperature chlorination 430-450oC and the rate of circulation of the reaction mixture equal to 11.0. The output of allylchloride is 92.03% (mole.).

Example 7. Analogously to example 1, the process is carried out at a molar ratio of propylene and chlorine equal to 3.0:1.0, temperature chlorination 430-450oC and the rate of circulation of the reaction mixture equal to 5.0. The output of allylchloride is 92.81% (mole.).

The results of examples 1-7 are shown in table.

Use open source software is whether the quantity of generated by-products.

1. The method of producing allylchloride gas-phase chlorination of propylene under pressure at 420 - 470o, Characterized in that the chlorination process are in a confined reaction path with forced circulation of the reaction gases with the separate submission and the molar ratio of propylene and chlorine 1,2 - 3,0 : 1,0, and the temperature of propylene 50 - 170oC, and the ratio of the volume of circulating in the reaction path and the output of the gas is 1 to 30 : 1.

2. The reactor for the production of allylchloride, including the areas of supply of the raw materials, the tubular area, connected with the filing of the original reagents, equipped with devices supplying gaseous reagents in the appropriate zone, and the exhaust device of the tubular part of the reactor, characterized in that the zone of initial reagents and the tubular reactor to form a single closed loop in the cavity which has a device for forced circulation, with the location of the input device of propylene to the forced circulation device, the input device of chlorine after the forced circulation device, but after input devices propylene and outlet gaseous products before input device

 

Same patents:
The invention relates to a technology for organochlorine products, namely the method for producing a solid chloroparaffin brand HP-1100, used as additives to polymeric materials to reduce their Flammability

The invention relates to the production of ozone-safe refrigerants ethane series, in particular 1,1,1,2-Tetrafluoroethane, which is obtained by fluorination 1,1,1-triptorelin fluoride of a metal of variable valence in the presence of a diluent

The invention relates to chemical technology, in particular to improvements in the method of producing chlorohydrocarbons methane number, which find use as solvents and raw materials for the production of perchloromethane

The invention relates to methods of chlorination of organic compounds, in particular the production of monochloramine derivatives of adamantane or diamantane catalytic chlorination of the corresponding parent compounds at a temperature of 150-250oC
The invention relates to chlorination to obtain 1,1,1-trichlorotrifluoroethane

The invention relates to the field of organic chemistry, namely the synthesis of paliperidone, also called freon
The invention relates to a method for producing a solid chloroparaffin with the General average formula CnH2n+2-xClxwhere x = 21 - 24

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 invention relates to methods of chlorination of paraffins, widely used in polymer compositions as plasticizers in the production of building materials, paints and varnishes, synthetic films and leathers, rubber industry, as well as ontamarama additives to various polymers

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

FIELD: chemical technology.

SUBSTANCE: invention relates to a method for conversion of hydrofluorocarbons, such as HFC-227, HFC-236, HFC-245, HFC-125, HFC-134, HFC-143 and HFC-152 and their corresponding isomers to a perhalogenated compound. The process is carried out by substitution of one or some hydrogen atoms in hydrofluorocarbon with halogen atom of a halogenating agent to yield perhalogenated compounds. The substitution occurs at temperature 150-400°C in the mole ratio of halogenating agent and hydrofluorocarbon = 0.16-22 in the presence of a solid substrate wherein a halogenating agent comprises one atom among Br, Cl and J, and one of components of solid substrate can represent activated carbon, Fe, Cu, Al, clay and metal oxides. Method for conversion of hydrofluorocarbons can involve additionally interaction of perhalogenated compound with a cleaving reagent to form fluoromonomer, such as hexafluoropropene, pentafluoropropene, tetrafluoroethylene, difluoroethylene and trifluoropropene. Invention provides admissible degree of conversion and selectivity.

EFFECT: improved method of conversion.

13 cl, 15 tbl, 11 ex

FIELD: chemistry.

SUBSTANCE: invention concerns method of obtaining methyl chloride by selective catalytic chlorination of methane, involving throughput of a source reaction gas mix containing at least methane and chlorinating agent in the form of either elementary chlorine or a mix of chlorine hydride with oxygen, through at least one catalyst layer. At that, the catalyst features additionally active centres with increased acidity and deuterium/hydrogen exchange depth not less than 10% at the temperature of 350-355°C in the deuterium and hydrogen mix containing 0.6% of hydrogen, 0.6% of deuterium, 0.05% Ar and 98.75% nitrogen, at the volume deuterium-hydrogen mix feed rate of 20000 hours-1 in the thermal regulated reaction mode at the heating rate of 10 K/minute. Active catalytic component is either platinum or copper, or silver. Catalyst carrier is microfibre of diametre of 1 to 20 micron, which can be structured in either non-woven or pressed material similar to wad or felt, or fibre of diametre of 0.5-5 mm, or woven material with lattice similar sateen, canvas, or openwork, with weave diametre of 0.5-5 mm.

EFFECT: high activity and selectivity of methane chlorination to methyl chloride at lower temperatures without production of polychlorinated hydrocarbons.

6 cl, 6 ex

FIELD: chemistry.

SUBSTANCE: proposed method of producing chloromethanes involves gas-phase thermal chlorination of methane, condensation of obtained chloromethanes, removal of methyl chloride from the condensate, obtaining a mixture of chloromethanes, distillation of this mixture with separation of the light fraction, liquid-phase chlorination of the light fraction with photochemical initiation, combination of vat fractions with products of liquid-phase chlorination, and separation of individual chloromethanes using known methods.

EFFECT: reduced formation of tetrachloromethane and increased selectivity on chloroform.

2 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: method of processing carbon-carbonate mineral involves burning limestone in a reactor, obtaining calcium oxide, production of calcium carbide by reacting part of calcium oxide obtained from burning limestone with carbon, bringing part of the obtained calcium carbide into contact with water, obtaining acetylene and caustic lime, bringing gaseous wastes from burning limestone into contact with water to obtain carbonic acid. Limestone is burnt using heat obtained from burning part of the volume of acetylene, obtained from part of the volume of calcium carbide. At least part of the obtained acetylene is used in synthesis of ethanol and/or dichloroethane and/or ethyleneglycol and/or acetone. During synthesis of ethanol and/or dichloroethane, acetylene is reacted with hydrogen in the presence of palladium as catalyst, after which at least part of synthesised C2H4 material is reacted with water vapour, obtaining ethanol, and/or reacted with chlorine, obtaining dichloroethane. Also at least part of the obtained acetylene is subjected to hydrolysis, obtaining ethyleneglycol. Also during synthesis of acetone, part of the obtained acetylene is reacted with water vapour, where the hydrogen obtained is used in said synthesis of ethanol and/or dichloroethane and/or burnt in the burning process. Carbon dioxide obtained from synthesis of acetone is used in the process of producing carbonic acid.

EFFECT: wide range of obtained finished products and prevention of formation of industrial wastes.

4 cl, 1 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing vinyl chloride, involving feeding chlorine gas and ethane into an ethane chlorination reaction area lying in the bottom part of a pyrolysis reactor in which there are solid particles; chlorination of ethane when chlorine gas and ethane come into contact with the solid particles such that, the ethane chlorination reaction product and the solid particles rise to the top part of the pyrolysis reactor at the same time and the formed coke settles on the solid particles; the ethane chlorination reaction takes place at 400-800°C and pressure of 1-25 atm, with molar ratio of ethane to chlorine gas equal to 0.5-5 and time of 0.5-30 seconds; the pyrolysis reaction takes place in the pyrolysis reaction area lying in the top part of the pyrolysis reactor when the ethane chlorination reaction product comes into contact with the solid particles such that, the ethane chlorination reaction product and solid particles rise at the same time and the formed coke settles on the solid particles; the pyrolysis reaction takes place at temperature of 300-800°C, pressure 1-50 atm and time ranging from 0.05 to 20 seconds; separation of solid particles obtained from the pyrolysis reaction and the pyrolysis reaction product in a separator; moving the separated solid particles to the regeneration reactor with subsequent burning of the coke settled on the solid particles for regeneration of the solid particles; and feeding the regenerated solid particles into the pyrolysis reactor. The invention also relates to a device for producing vinyl chloride, which includes a pyrolysis reactor having an ethane chlorination reaction area in the bottom part and a pyrolysis reaction area in the top part; a separator which separates the pyrolysis reaction product and solid particles; a regeneration reactor which regenerates separate solid particles through burning and at least one module through which solid particles move.

EFFECT: high product output and reduced formation of coke.

14 cl, 4 tbl, 2 ex, 3 dwg

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

Up!