Method for preparing 1,2-dichloroethane with preliminary heating reagents

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of 1,2-dichloroethane by method of liquid-phase chlorination of ethylene. The process is carried out by direct feeding gaseous reagents chlorine and ethylene in liquid reaction medium of reactor. Before feeding into reactor chlorine and ethylene are heated preliminary in heat-exchangers to temperature equal to that of liquid in reactor. Method provides enhancing selectivity of process and reducing formation of by-side substances representing higher chlorine-derivatives of ethane.

EFFECT: improved method of synthesis.

4 dwg, 1 ex

 

The technical field to which the invention relates.

The invention relates to a method for producing 1,2-dichloroethane by means of liquid-phase chlorination of ethylene.

The level of technology.

The closest way to obtain 1,2-dichloroethane is a high-temperature liquid-phase chlorination of ethylene [1].

The closest prototype is a high temperature process, which is carried out at a temperature equal to the boiling temperature of the working environment (83,5-110°depending on the pressure). Reactor high-temperature process is a bubbling gas-lift column 1 with internal circulation tube 4 (Fig 1). The working environment is liquid 1,2-dichloroethane. The catalyst is FeCl3, which is located in the reactor in dissolved form. He is an inhibitor adverse reactions substitution chlorination of 1,2-dichloroethane in the liquid phase [2]. To obtain a solution of chlorine gas through the distributor 2 is fed in the lower part of the annular space. The area between the chlorine dispenser 2 and the ethylene distributor 3 is called the region of absorption of chlorine. The reaction is carried out upstream when entering into the reactor in gaseous ethylene through the distributor 3. The area above the distributor ethylene referred to as the reaction zone. Due to the difference of density in kg is relationnal tube and in the annular space occurs the liquid circulation. In the upper part of the reactor are perforated plates 6, designed to intensify the agitation. The upper part of the reactor plays the role of a separator for separating liquid droplets from the steam. The reaction products are discharged in the form of vapor to the stage rectification through the nozzle in the lid of the reactor. Due to the low volatility of the catalyst remains in the reactor. To maintain the liquid level in the lower part of the reactor is introduced 1,2-dichloroethane.

An important advantage of the high-temperature process is efficiency: heat is consumed for evaporation and distillation products, waste no water, the catalyst consumption is minimal.

The disadvantage of the high-temperature process are low selectivity (98,0-98,7%), associated with an increased rate of adverse reactions with increasing temperature. By-products - trichloroethane, trichlorethylene and other higher chlorinated ethane is formed in the reactor as a result of reactions substitution chlorination of 1,2-dichloroethane by chlorination in the liquid phase [2].

Low-temperature process is carried out in the reactor (figure 2), which is a bubbling column 1, connected at the top and bottom with an external shell and tube heat exchanger 5. The working environment in the reactor is the product of the reaction, 1,2-dichloroethane in the liquid state. Chlorine input is seeking in the lower part of the column through the dispenser 2. Earlier in the resulting chlorine solution through the dispenser 3 is introduced ethylene. Due to the difference of density in the refrigerator and column raises the circulation of the working environment with upward flow in the column. The temperature in the reactor is 65°C. the Removal of the synthesized product by gravity flow through the overflow. The separation of product from catalyst is carried out at the stage of purification. The catalyst after the cleanup phase and not subject to regeneration. The products of the process from the stage of purification act of rectification.

The advantage of the low temperature reactor is a high selectivity (99,6%), owing to the slowdown of adverse reactions substitution chlorination at lower temperature. The disadvantages of the low-temperature process include high consumption of wastewater at the stage of purification of the product from the catalyst, significant consumption of catalyst per unit of production, high energy costs for cooling the reaction mass and irrational use of the heat of reaction.

In addition, known methods for producing 1,2-dichloroethane WO 9801407 A1, US 6235953 B1, US 6252125 B1. In the application WO 9801407 A1, 15.01.1998 and in patents US 6235953 B1 22.05.2001, US 6252125 B1, 26.06.2001 chlorine and ethylene pre-mixed with dichloroethane in the pipeline, and then fed into the reactor. However, this does not exclude the formation of aerosol in the gas phase in which Truboprovod and in the reactor, as the chlorine and ethylene are fed into the pipeline without heating. Therefore, the formation of aerosol in these reactors should lead to a decrease in the selectivity of the process. In the proposed method is preliminary (prior to feeding into the reactor) heat the reactants to a temperature equal to the temperature of the liquid in the reactor (83,5-110° (C)that will prevent the condensation of vapors of chlorine and ethylene dichloride in the gas phase at the inlet of the reactor and will increase the selectivity of the process.

Disclosure of the invention.

The objective of the invention is to develop a new method for the production of 1,2-dichloroethane by means of liquid-phase chlorination of ethylene preheating the reactants. A typical way to obtain 1,2-dichloroethane temperature of the reactants at the input to the reactor is equal to the ambient temperature, which is considerably lower than the temperature of the working environment in the reactor (83,5-110°). This leads to a decrease in the selectivity of the process.

In the reaction zone in addition to the process of chemisorption of ethylene evaporation of the chlorine solution 2 in gaseous ethylene 1 (figure 3). Since the initial temperature of the gaseous ethylene 1 below the temperature of the liquid in the reactor, a pair of 1,2-dichloroethane with chlorine is condensed in a bubble of ethylene, forming aerosol 3. Bubble ethylene is filled with many small drops of 1,2-dichloroethane, the content is appropriate chlorine. In the liquid phase inhibitor adverse reactions is FeCl3[3]. Because the inhibitor adverse reactions FeCl3non-volatile, it does not evaporate and misses of aerosol droplets. In the absence of inhibitor FeCl3in the drops of spray rate of adverse reactions increases [3]. Thus, in the droplets of the aerosol created favorable conditions for the occurrence of adverse reactions.

In the area of the absorbance at the expiration of gaseous chlorine in 1,2-dichloroethane also the evaporation of 1,2-dichloroethane and its condensation in the volume of the bubble chlorine in the form of an aerosol. In the droplets of the aerosol no inhibitor FeCl3. In the absence of inhibitor side processes the rate of adverse reactions increases [3].

In the area of the absorbance at the expiration of chlorine from the bubbler in 1,2-dichloroethane in the adiabatic expansion and throttling occurs, the temperature reduction of chlorine, thus there is condensation of chlorine in the form of aerosol due to the low boiling point of chlorine (-34°s at 1 ATA). Formed many small drops of 100%liquid chlorine, which when injected into 1,2-dichloroethane create a local high concentration of chlorine. In those areas with a high concentration of chlorine leak adverse reactions with high speed, because the rate of adverse reactions increases with increasing chlorine concentration [4].

Invited to lead the process W is dataseg chlorination of ethylene preheating the reactants (figure 4) to a temperature so that when released into the reaction medium chlorine and ethylene had a temperature equal to the temperature of the liquid in the reactor depending on the pressure 83,5-110°With (at operating conditions). This will prevent the formation of aerosol in the bubbles of chlorine and ethylene. This would lead to higher selectivity in comparison with such methods as WO 9801407 A1, US 6235953 B1, US 6252125 B1. In these methods, the chlorine and ethylene pre-mixed with liquid 1,2-dichloroethane in the pipeline, and then are fed into the reactor. If this is not provided for pre-heating of chlorine and ethylene, which leads to the condensation of 1,2-dichloroethane and chlorine in the gas phase and the formation of aerosol. Resulting in reduced selectivity of the process.

The invention can be obtained the following results:

1. In bubbles of chlorine and ethylene will not condense vapors of 1,2-dichloroethane, which eliminates areas with high rate of adverse reactions and to increase the selectivity of the process.

Calculations show that the condensation of vapors of chlorine solution in the gas - phase ethylene moisture content of 1,2-dichloroethane in a bubble of ethylene is approximately y=0,11 (11%). This value is essential for the formation of side products in aerosol droplets of the liquid phase. In the absence of inhibitor adverse reactions (FeCl3in aerosol droplets is increased speed occurring adverse reactions [3]. According to [3], as a result of experimental studies on laboratory reactor kinetic parameters on the influence of FeCl3on the rate of adverse reactions substitution chlorination of 1,2-dichloroethane. In particular, the rate constant neighborouing process 7.5·10-5with-1while some in the same conditions, the rate constant for the inhibited reaction is only 11,1·10-7with-1. This reflects the inhibitory effect of ferric chloride. Thus, in the absence of inhibitor adverse reactions FeCl3in the droplets of the aerosol flow adverse reactions, which reduce the selectivity of the process of liquid-phase chlorination of ethylene.

In the proposed method of producing 1,2-dichloroethane, chlorine and ethylene after preheating will have a temperature above the dew point (at operating conditions). As a result, when the evaporation of the chlorine solution into the bubble ethylene pair will not condense in the bubble of ethylene, which will prevent the formation of an aerosol, and will increase the selectivity of the process, i.e. will reduce the amount of by-products in the product 1,2-dichloroethane.

2. At the expiration of chlorine dispenser will not condense chlorine due to the effect of throttling, which would exclude the possibility of formation of local participation the Cove with a high concentration of chlorine and to increase the selectivity of the process.

It is known [4]that the increase in the chlorine concentration increases the rate of formation of by-products. Preheating chlorine will prevent condensation of chlorine at flow (throttling). In this case, will not be formed aerosol chlorine and predotvratite the formation of regions with high concentration of chlorine in the liquid phase. In accordance with the data [4] this will reduce the rate of adverse reactions and, consequently, to increase the selectivity of the process.

Thus, the method preheating the reactants are created more favorable conditions for the process than in the patents WO 9801407 A1, US 6235953 B1, US 6252125 B1, in which chlorine and ethylene pre-mixed with dichloroethane in the pipeline, and then fed into the reactor. However, in this case is not precluded by the formation of aerosol in the gas phase in the pipeline and in the reactor, as the chlorine and ethylene are fed into the pipeline without heating, as a consequence, the selectivity decreases. In the new method of producing 1,2-dichloroethane provides preheating of the reactants to a temperature equal to the temperature of the liquid in the reactor. Depending on the pressure, the temperature is 83,5-110°C. this action prevents the condensation of the vapors of chlorine and ethylene dichloride in the gas phase at the inlet of the reactor, which will improve the shape selectivity of the process.

A brief description of the drawings.

List of figures:

figure 1 - bubbling gas-lift reactor high-temperature liquid-phase chlorination of ethylene.

figure 2 - bubble reactor low-temperature chlorination of ethylene.

figure 3 - mass transfer at the stage of formation of a bubble in a bubble reactor.

4 is a bubbling gas-lift reactor liquid-phase chlorination of ethylene with preheating of the reactants.

In figures 1 and 2 describe the analogue of the invention. Figure 3 describes the mechanism of transfer of a substance from the liquid phase in the gas (bubble ethylene). Figure 4 describes the reactor, which can be implemented in the invention.

The implementation of the invention.

The invention is carried out in a bubbling reactor liquid-phase chlorination of ethylene (figure 4). Bubble reactor 1 production of 1,2-dichloroethane by means of liquid-phase chlorination of ethylene with preliminary heating of the reagents is as follows. Chlorine gas is heated in the heat exchanger 5 and through the dispenser 2 is fed in the lower part of the annular space. Over the chlorine dispenser is dissolving chlorine in the ascending stream of 1,2-dichloroethane. Gaseous ethylene is heated in the heat exchanger 7 through the valve 3 is fed into the formed chlorine solution. Due to the difference of density in kg is relationnal pipe 4 and into the annular space occurs the liquid circulation. In the upper part of the reactor are perforated plates 6, designed to intensify the agitation. The upper part of the reactor plays the role of a separator for separating liquid droplets from the steam. To maintain the liquid level in the lower part of the reactor is fed with liquid 1,2-dichloroethane.

After preheating in the heat exchanger at the inlet of the reactor chlorine and ethylene will have a temperature equal to the temperature of the working environment in the reactor 83,5-110°depending on the pressure. As a result, when the evaporation of the chlorine solution in ethylene vapours will not condense in the gas phase ethylene. In the absence of an aerosol of a solution of chlorine inside bubbles ethylene liquidated zone of by-products formation. It follows from the work [3], according to which in the absence of inhibitor FeCl3increases the rate of formation of by-products. The result will increase the selectivity of the process, i.e. reduced content of by-products in the product 1,2-dichloroethane.

The results of the tests of a new method of producing 1,2-dichloroethane with preheating of the reactants.

The high selectivity of the new method of producing 1,2-dichloroethane is heated reagents was confirmed by the experimental studies on gas-lift reactor with a capacity of chlorine 60 m3/h Pressure p is the actor was 1 ATA. Temperature 85°C. For comparison experiments on the reactor in two modes: heated reagents and without heating. When this was measured concentration of one of the by-products of substitution chlorination (hydrogen chloride HCl) vapour phase at the top of the reactor exit. Concentration of by-product HCl at the outlet of the reactor is possible to judge the intensity of adverse reactions in the reactor and the selectivity of the process [4]. In the absence of heating of the reactants at the temperature of the supplied chlorine 10°With the concentration of HCI in the vapour phase at the outlet of the reactor was 1250-3100 mg/m3. When pre-heated chlorine in the heat exchanger with water vapor to a temperature of 85°With the concentration of HCl at the outlet of the reactor was decreased to 310-430 mg/m3. In accordance with the methodology described in [4], the concentration of HCl in the gas phase corresponds to a selectivity of 99.97%. The results of the experiments indicate that at low temperature chlorine is the formation of aerosol, which reduces the selectivity of the process and increased the yield of by-products substitution chlorination (HCl). The temperature rise of chlorine and ethylene to a temperature of the liquid in the reactor (83,5-110°depending on pressure) increases the selectivity of the process.

Literature

1. Leba is s NN. Chemistry and technology of basic organic and petrochemical synthesis. Ed. 2nd Per. M.: Chemistry, 1975 - 736 S.

2. Avetyan MG, Sonin EV, zeidman O.A. and others Research process direct chlorination of ethylene in an industrial environment. // Chemical engineering, 1991, No. 12, s-713.

3. Rozhkov V., zeidman O.A., Sonin EV and other Liquid-phase chlorination of 1,2-dichloroethane in the presence of ferric chloride. // Chemical engineering, 1991, No.5, pp.5-7.

4. Malchukov AV Thesis for the degree of candidate of technical Sciences. Hydraulics, heat and mass transfer in the reactor chlorination of ethylene with ejection mixers. Angarsk, AGT, 2000.

Method for producing 1,2-dichloroethane by means of liquid-phase chlorination of ethylene with separate gaseous reagents chlorine and ethylene directly in the liquid reaction medium of the reactor, characterized in that prior to being fed into the reactor chlorine and ethylene pre-heated to a temperature equal to the temperature of the liquid in the reactor.



 

Same patents:

FIELD: chemical industry; designs of the bubble-type reactors for production of 1.2-dichloroethane.

SUBSTANCE: the invention is pertaining to the design of the bubble-type reactors for production of 1.2-dichloroethane by the method of the liquid-phase chlorination of ethylene with the reaction heat removal at boiling of the working medium. As the contact device the reactor uses two layers of the metallic nozzle. The liquid 1.2-dichloroethane is fed from above to the nozzle, into the space between the layers of the nozzle feed the gaseous chlorine with nitrogen, and under the lower layer of the nozzle feed the gaseous ethylene with nitrogen, that allows to reduce the diameter of the reactor in 1.5-2 times due to the increased effectiveness of stirring and formation of the developed contact surface of the phases. At that the heat of the reaction is removed by evaporation of 1.2-dichloroethane in nitrogen. At that the temperature of the liquid is maintained below the boiling temperature. The technical result of the invention is the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

EFFECT: the invention ensures the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

1 ex, 4 dwg

FIELD: organic chemistry.

SUBSTANCE: 1,2-dichloroethane is obtained by liquid phase ethylene chlorination with discharging of reaction heat due to operation medium boiling. In claimed process nitrogen is added to chlorine and ethylene reagents. Ratio of chlorine volume consumption to nitrogen volume consumption is maintained as 1:1. Reaction is carried out at temperature lower than 1,2-dichloroethane boiling point, and discharging of reaction heat is carried out by evaporative cooling of operation medium in nitrogen.

EFFECT: process of increased selectivity; decreased yield of by-products.

1 tbl, 5 dwg

FIELD: organic synthesis catalysts.

SUBSTANCE: catalyst includes Cu and Mg compounds deposited on alumina as carrier and has copper compounds, expressed as Cu, from 2 to 8%, Mg/Cu atomic ratio ranging from 1.2 to 2.5, wherein concentration of copper atoms is higher in the interior of catalyst particle than on the surface (layer 20-30 Å thick) thereof and concentration of magnesium atoms prevails on the surface of catalyst particle, while specific surface of catalyst ranged from 30 to 130 m2/g. Oxychlorination of ethylene is carried out under fluidized bed conditions using air and/or oxygen as oxidants in presence of above-defined catalyst. Catalyst is prepared by impregnating alumina with aqueous Cu and Mg solutions acidified with hydrochloric acid solution or other strong acids using volume of solution equal or lesser than porosity of alumina.

EFFECT: increased activity of catalyst at high temperatures and avoided adhesion of catalyst particles and loss of active components.

8 cl, 2 tbl, 5 ex

FIELD: chemical technology.

SUBSTANCE: invention relates to a method for preparing 1,2-dichloroethane. Method involves the oxychlorination reaction of ethylene with hydrogen chloride and oxygen-containing gas and alkaline treatment of dichloroethane also. Before alkaline treatment of 1,2-dichloroethane carbon dioxide is removed that is carried out by decrease of the reaction mixture pressure comprising 1,2-dichloroethane, or by addition of inert gas wherein nitrogen is used, or by heating. Before separation of carbon dioxide the product of the 1,2-dichloroethane-containing the oxychlorination reaction is quenched, cooled and/or condensed. After separation of carbon dioxide the 1,2-dichloethane-containing reaction mixture is treated with an aqueous alkaline solution followed by its separation. The prepared 1,2-dichloroethane-containing reaction mixture is characterized by the content of chloral and/or chloral hydrate less 0.02 wt.-% but preferable less 0.005 wt.-%, and especially preferably, less 0.002 wt.-%. Invention provides reducing consumption of an alkaline solution, prevention of formation of by-side products of chloral and chloral hydrate, and preparing the pure 1,2-dichloroethane with respect to such by-side products.

EFFECT: improved preparing method.

16 cl, 3 dwg, 3 ex

FIELD: petrochemical and industrial organic synthesis.

SUBSTANCE: process comprises separating gaseous pyrolysis products to recover ethylene-containing fraction with 54-65% ethylene content and C3-C5-hydrocarbon fraction. Ethylene-containing fraction is subjected to liquid-phase catalytic chlorination. Gas phase of chlorination product is purified via adsorption and fed into furnace as fuel. C3-C5-Hydrocarbon fraction is subjected to exhaustive hydrogenation, hydrogenation product is combined with fresh raw material at weight ratio (0.05ч1):1 and sent to pyrolysis plant.

EFFECT: achieved integration of process, increased reliability thereof, and reduced expenses.

1 dwg, 1 tbl, 15 ex

FIELD: chemistry, in particular utilization of chlorine-containing waste.

SUBSTANCE: claimed method includes passing of organochlorine compound vapors blended with oxygen-containing reaction gaseous mixture through catalyst layer providing oxidation of starting organochlorine compounds. Said catalyst represents geometrically structured system from microfibers with length of 5-20 mum. Catalyst has active centers which are characterized by presence of absorption band in absorbed ammonia IR-spectrum with wave number ν = 1410-1440 cm-1; contains platinum group metal as active ingredient; and glass fiber carrier. Said carrier in NMR29Si-spectrum has lines with chemical shifts of -100±3 ppm (Q3-line) and -110±3 ppm (Q4-line) in integral intensity ratio of Q3/Q4 = 0.7-1.2; in IR-spectrum it has hydroxyl absorption band with wave number ν = 3620-1440 cm-1 and half-width of 65-75 cm-1; has specific surface, measured by BET using argon thermal absorption: SAr = 0.5-30 m2/g; surface area, measured by alkali titration: SNa = 10-250 m2/g, wherein SNa/SAr = 5-30.

EFFECT: selective oxidation of starting organochlorine compounds to safe and easily utilizing substances without toxic by-product formation.

3 cl, 4 ex

The invention relates to petrochemistry, and more specifically to the separation of 1,2-dichloroethane

The invention relates to the management of chemical-technological processes carried out in a cascade of reactors for producing 1,2-dichloroethane by chlorination of ethylene in recogida reaction mass
The invention relates to the chemical industry and plastics

FIELD: chemical industry; designs of the bubble-type reactors for production of 1.2-dichloroethane.

SUBSTANCE: the invention is pertaining to the design of the bubble-type reactors for production of 1.2-dichloroethane by the method of the liquid-phase chlorination of ethylene with the reaction heat removal at boiling of the working medium. As the contact device the reactor uses two layers of the metallic nozzle. The liquid 1.2-dichloroethane is fed from above to the nozzle, into the space between the layers of the nozzle feed the gaseous chlorine with nitrogen, and under the lower layer of the nozzle feed the gaseous ethylene with nitrogen, that allows to reduce the diameter of the reactor in 1.5-2 times due to the increased effectiveness of stirring and formation of the developed contact surface of the phases. At that the heat of the reaction is removed by evaporation of 1.2-dichloroethane in nitrogen. At that the temperature of the liquid is maintained below the boiling temperature. The technical result of the invention is the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

EFFECT: the invention ensures the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

1 ex, 4 dwg

FIELD: organic chemistry.

SUBSTANCE: 1,2-dichloroethane is obtained by liquid phase ethylene chlorination with discharging of reaction heat due to operation medium boiling. In claimed process nitrogen is added to chlorine and ethylene reagents. Ratio of chlorine volume consumption to nitrogen volume consumption is maintained as 1:1. Reaction is carried out at temperature lower than 1,2-dichloroethane boiling point, and discharging of reaction heat is carried out by evaporative cooling of operation medium in nitrogen.

EFFECT: process of increased selectivity; decreased yield of by-products.

1 tbl, 5 dwg

FIELD: petrochemical and industrial organic synthesis.

SUBSTANCE: process comprises separating gaseous pyrolysis products to recover ethylene-containing fraction with 54-65% ethylene content and C3-C5-hydrocarbon fraction. Ethylene-containing fraction is subjected to liquid-phase catalytic chlorination. Gas phase of chlorination product is purified via adsorption and fed into furnace as fuel. C3-C5-Hydrocarbon fraction is subjected to exhaustive hydrogenation, hydrogenation product is combined with fresh raw material at weight ratio (0.05ч1):1 and sent to pyrolysis plant.

EFFECT: achieved integration of process, increased reliability thereof, and reduced expenses.

1 dwg, 1 tbl, 15 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention is dealing with production of chlorohydrocarbons exhibiting plasticizing properties in polymer compositions in production of synthetic building materials, varnishes and paints, artificial films and leathers, in rubber industry, and as fire-retardant additives in polymers. Process comprises chlorination of waste obtained in production of C14-C32 fraction by ethylene-α-olefin oligomerization. Chlorination is accomplished in two steps: addition chlorination at 35-55°C followed by substitution chlorination at 40-105°C. Chlorohydrocarbons thus obtained can, in particular, be used as secondary plasticizer in polyvinylchloride compositions.

EFFECT: reduced expenses due to using production waste.

4 tbl, 30 ex

The invention relates to the technology of organic synthesis, in particular, to a method for producing chlorinated hydrocarbons having plasticizing properties of polymer compositions in the industry of synthetic building materials, paints and varnishes, synthetic films and leathers, rubber industry, as well as ontamarama additives to various polymers

The invention relates to the technology of organic synthesis, in particular to a method for producing chlorinated hydrocarbons used as plasticizers for polymeric compositions in the industry of synthetic building materials, paints and varnishes, synthetic films and leathers, rubber industry, as well as ontamarama additives to various polymers

The invention relates to the management of chemical-technological processes carried out in a cascade of reactors for producing 1,2-dichloroethane by chlorination of ethylene in recogida reaction mass

The invention relates to the production of 1,2-dichloroethane by direct chlorination of ethylene in the liquid dichloroethane

The invention relates to the production of dichloroethane by direct chlorination of ethylene in the liquid dichloroethane

The invention relates to a method of producing allylchloride gas-phase chlorination of propylene under pressure at 430-470°C

FIELD: industrial organic synthesis.

SUBSTANCE: invention is dealing with production of chlorohydrocarbons exhibiting plasticizing properties in polymer compositions in production of synthetic building materials, varnishes and paints, artificial films and leathers, in rubber industry, and as fire-retardant additives in polymers. Process comprises chlorination of waste obtained in production of C14-C32 fraction by ethylene-α-olefin oligomerization. Chlorination is accomplished in two steps: addition chlorination at 35-55°C followed by substitution chlorination at 40-105°C. Chlorohydrocarbons thus obtained can, in particular, be used as secondary plasticizer in polyvinylchloride compositions.

EFFECT: reduced expenses due to using production waste.

4 tbl, 30 ex

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