Method for treatment of alpha-olefins, method for treatment of hexene-1 and unit for its realization

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: crude alpha-olefin is heated, raw vinylidene olefins are isomerized in the presence of catalyst and alpha-olefin is separated from isomerized vinylidene olefin by rectification. Separation of alpha-olefin is carried out for at least two successive steps at similar temperatures on top of vat and reducing pressure of rectifying column at each following step. Condensed phase removing from top of the rectifying column at previous step is fed to feeding zone of the following step and the rectifying column at top and vat section is sprayed. For spraying the top section of column the condensed phase removing from the top of rectifying column at the same step is used and for spraying the vat section of column the vat liquid of rectifying column at the same step is used. Separated alpha-olefin is purified additionally from oxygen-containing impurities by adsorption up to polymerization degree of purity. Raw heating, isomerization, separation and adsorption are carried out in atmosphere in inert gas. The unit used for treatment of alpha-olefin includes reactor for isomerization of vinylidene olefins in raw, rectifying column wherein feeding zone is joined with reactor outlet and wherein alpha-olefin of high purity degree is removed from the column top. The unit includes also at least one rectifying column for additional treatment of alpha-olefin of high purity from isomerized vinylidene olefins and adsorption column for separation of oxygen-containing impurities in alpha-olefin of high purity wherein the column inlet is joined with the top outlet of the last rectifying column used for additional treatment of alpha-olefin of high purity and outlet is used for removing alpha-olefin of the polymerization purity degree. Invention provides enhancing quality of the end product.

EFFECT: improved method for treatment.

8 cl, 1 dwg, 1 ex

 

The invention relates to the field of petrochemicals, more precisely to the field of production of alpha-olefins of high purity, and can be used in particular for the purification of 1-hexene from vinylidene olefins and other impurities.

A known method of purification of alpha-olefins containing vinylidene isomers, by processing these olefins with hydrogen sulfide or mercaptans in the presence of acids (U.S. patent No. 4511753, epubl). However, the use of these agents - hydrogen sulfide and mercaptans, which are very toxic, makes the process environmentally hazardous. Moreover, the process includes a step of washing from sulfides of alkaline reagents, which complicates the process.

A known method of purification of alpha-olefins from vinylidene olefins by selective oligomerization more reactive vinylidene olefins in the presence of catalytic systems based on boron TRIFLUORIDE, water and an organic promoter, followed by the separation of alpha-olefins obtained from oligomers by distillation (U.S. patent No. 5095172, epubl).

The known method according to which medium chain With5-C8alpha-olefins, containing as impurities 2-alkyl substituted isomers of the corresponding olefins, purified by passing the specified olefin over an acid catalyst, such as sulfonic cation exchanger Amberlst 15, with full static volumetric capacity to 4.81 mg·equn+/g at a temperature of 20-30°C, atmospheric pressure and space velocity of the feedstock 10-20 (h-1) (U.S. patent No. 5789646, publ. 04.08.98).

A known method of purification of alpha-olefin, which used hexene-1 containing 2-ethylbutane-1 , including phase isomerization of 2-ethylbutane-1 3-methylpentan-2 on the catalyst and the extraction of hexene-1 of high purity. As the catalyst used macroporous sulfonation average acidity. Selective isomerization of 2-ethylbutane-1 3-methylpentan-2 is carried out at a temperature of 50-80°C, a pressure of 1-3 atmospheres, in an inert atmosphere and a flow rate of 1-10 h-1(patent RF №2206557, epubl).

Known installation for implementing the method containing the reactor and distillation column connected in the power zone with the upper outlet of the reactor and having a lower outlet for withdrawal from Cuba of the target product is purified 1-hexene (ibid.).

However, it should be noted that the known method and installation for its implementation cleanse HEXEN-1 predominantly from isomer 2-ethylbutane-1 and it does not allow you to get HEXEN-1 of the high-polymerization degree of purity, which requires industry to obtain high-quality products from hexene-1 in the further processing, in particular of C is the presence of oxygen-containing impurities, such as water, hydrogen peroxide, alcohols. In addition, the known installation does not allow you to get HEXEN-1 of high purity on an industrial scale.

The basis of the invention is to create a method of purification of alpha-olefins from vinylidene olefins and branched isomers and oxygen-containing impurities and installation for carrying out the method, which could produce alpha-olefins polymerization purity, suitable for further use in industry for high-quality products in industrial output.

This task is solved in that in the method of purification of alpha-olefins comprising heating raw materials, isomerization vinylidene olefins in the feedstock in the presence of a catalyst and separation of alpha-olefins from isomerized vinylidene olefins by distillation, the separation of alpha-olefins is carried out in at least two successive stages at the same temperatures of the top and Cuba, and decreasing the pressure of the distillation column each subsequent stage, in the power zone subsequent stage serves condensed phase, taken from the top of the rectifying column of the previous stage, each stage is applied irrigation distillation column at the top and bottom parts, and for irrigation of the upper part use the condensed phase, Atbara is directly from the top of the rectifying column of the same phase, for irrigation bottom part - cubic liquid of the distillation column of the same phase, and the separated alpha-olefin optionally purified from oxygen-containing impurities by adsorption, and partially returned to the middle part of the distillation column of the first stage for supplemental irrigation, cleaning and adsorption is carried out in an atmosphere of inert gas.

It is advisable that as the inert gas would be applied nitrogen.

It is advisable that in the reactor as the catalyst would be applied selfactivity catalyst or a mixture of cation exchange resin with aluminum oxide or silicon oxide, or a zeolite, or silica gel having a full static volumetric capacity, mg·equn+/g 4,3-4,5.

It is also advisable adsorption carried out at a temperature of 30-50°C.

The problem is solved also by the fact that in the method of cleaning hexene-1, comprising heating raw materials, isomerization vinylidene olefins in the feedstock in the presence of a catalyst and the separation of 1-hexene from isomerized vinylidene olefins by distillation separation of 1-hexene spend at least two successive stages at a temperature of the top of the distillation column each stage equal to 60-65°C, the temperature of the rectifying column bottom of each stage is equal to 70-80°and decreasing the pressure of each subsequent stadiona 20-40 mm RT. Art. in the power zone subsequent stage serves condensed phase, taken from the top of the rectifying column of the previous stage, each stage is applied irrigation distillation column at the top and bottom parts, and for irrigation of the upper part of the use of the condensed phase, taken from the top of distillation columns the same stage for irrigation bottom part - cubic liquid of the distillation column of the same phase, separated hexene-1 is additionally clear of oxygen-containing impurities by adsorption to the polymerization of purity, and partly returned to the middle part of the distillation column of the first stage for supplementary irrigation, and the heat of raw materials, isomerization, the Department and the adsorption is carried out in nitrogen atmosphere.

Suitable adsorption carried out at a temperature of 30-50°and as adsorbent to apply Almagell and molecular sieve.

The problem is solved also by the fact that the installation for the purification of alpha-olefins containing reactor for isomerization vinylidene olefins in raw materials and the distillation column, the zone diet which is connected to the output of the reactor, and from the top of which is selected alpha-olefin of high purity according to the invention contains at least one distillation column for further purification of alpha-olefins you what eye clean from the isomerized olefins, the zone diet which is connected with the output of the previous top of the distillation column, the top of which is connected through the heat exchanger with its irrigation zone top and CBM output is connected through the heat exchanger with its irrigation zone a bottom part, and the adsorption column to remove oxygen-containing impurities in alpha-olefin of high purity, the entrance of which is associated with the release of the top of the last distillation column for further purification of alpha-olefins of high purity, one output is connected to the middle part of the first distillation column, and the other output is used to display alpha-olefin polymerization purity.

It is also advisable to VAT output of the distillation column for further purification of alpha-olefin from isomerized vinylidene olefins would be connected to the middle part of the previous distillation columns.

Further, the invention is illustrated and attached drawing, which shows a schematic diagram of installation for the purification of alpha-olefins according to the invention.

The proposed method of purification of alpha-olefins is as follows.

Raw materials - crude alpha-olefin in a continuous mode in a current of inert gas, for example nitrogen, is heated to a temperature isomerization vinylidene olefins and served in the from the reactor, being in the same atmosphere of inert gas. The raw material used any alpha-olefins, which are obtained by oligomerization of ethylene, such as octene-1 or hexene-1. B reactor, the raw material passes through the layer sulfocationites catalyst, which provides selective isomerization vinylidene olefins in the feedstock to internal olefins.

However, it is advantageous to use as catalyst a mixture of cation exchange resin with aluminum oxide or silicon oxide, or a zeolite, or silica gel. The advantage that the catalyst had a full static volumetric capacity, mg·equn+/g of 4.3 to 4.5. Received isomerizate is taken from the top of the reactor and is fed to the rectification in the power zone of the distillation column of the first stage. Cubic liquid of this distillation column output, with its return for the irrigation of a bottom part and a pair from the top of distillation column condense, part of the formed condensate return to irrigate the upper part and the remaining part is sent to the power zone of the distillation column a later stage. The rectification is carried out in at least two stages at the same temperature of the cube and the top and decreasing the pressure of distillation columns each subsequent stage, each stage is applied irrigation distillation column at the top is her and a bottom part, and for the irrigation of the upper part of the use of the condensed phase, taken from the top of distillation columns the same stage for irrigation bottom part - cubic liquid of the distillation column of the same phase, and the remaining condensed out from the top of distillation columns each stage is fed into the power zone of the distillation column a later stage. The number of stages is determined by the composition of supply of raw materials and may be two, three or more. Condensed output from the top of distillation column last stage in the form of alpha-olefins of high purity additionally cleaned by adsorption from complex oxygen-containing impurities (mainly water, hydrogen peroxide, alcohols) at a temperature of sorption 30-50°C. as adsorbent used adsorbent containing Almagell and molecular sieves. Purified from complex oxygen-containing impurities alpha-olefin is a target product - alpha-olefin polymerization purity. Part of his return in the middle part of the distillation column of the first stage for supplementary irrigation, and the rest of the output as the target product.

Installation for purification of alpha-olefin according to the invention contains raw capacity 1 to one input of the 2, which includes raw materials - crude alpha-olefin, and the second input of the 3 - inert gas, apremilast, reactor 4 for isomerization vinylidene olefins, one input of which the pipe 5 through the heat exchanger 6 is connected to the output of a raw material tank 1, while the other input 7 which serves inert gas, for example nitrogen, capacity 8 to collect isomerate, one input of which the pipe 9 is connected to the output of the reactor 4 and the other input 10 submit inert gas, such as nitrogen distillation column 11, which pipe 12 is connected in the area of power output capacity 8 to collect isomerate and the output below displays the cubic product and the pipe 13 through the heat exchanger 14 is connected to a bottom zone of the distillation column 11, the collector 15 for collecting the cubic product of the distillation column 11, the entrance of which the pipe 16 is connected with kubovy output of the rectifying column 11, the other input 17 which serves to supply an inert gas, for example nitrogen, and the output 18 is used to output the product of the collector 15.

The installation also contains reflux tank 19, the entrance of which the pipe 20 through the heat exchanger 21 is connected to the top outlet of the distillation column 11, where selected pairs of alpha-olefins of high purity, exit 22 displays of excess condensate, and the other output line 23 is connected to the irrigation zone of the distillation column 11.

According to the invention the apparatus comprises rectifying the number of the nnu 24, for additional purification of alpha-olefin from isomerized vinylidene olefins, which in the area of power supply are connected by a pipe 25 with the output of the reflux tank 19, the VAT which the pipe 26 is connected to the power zone of the distillation column 11, and the pipe 27 through the heat exchanger 28 with the bottom part of the distillation column 24.

The installation also contains reflux tank 29, the entrance of which conduit 30 through the heat exchanger 31 is connected to the top outlet of the distillation column 24, the output of the 32 outputs of excess condensate, and the other the outlet pipe 33 is connected to the irrigation zone of the distillation column 24, the collector 34, one input of which the pipe 35 is connected to the output reflux tank 29, and the other input 36 serves inert gas, for example nitrogen.

The installation according to the invention can contain multiple distillation columns for additional purification of alpha-olefin selected from the top rectificative columns, from isomerized vinylidene olefins. Their number is determined by the composition of supply of raw materials and may be two, three or more.

According to the invention, the installation also contains an adsorption column 37, the entrance of which is in the lower part of the pipe 38 is connected to the output capacity of 8 to collect isomerate and pipe 39 to the output of the collector 34 and the other input 40 serve the inert-gas supply, for example nitrogen, and the output of the upper part is connected by a pipe 41 to the power zone of the distillation column 11, the collector 42 of alpha-olefin polymerization purity, which is connected to the top outlet of the adsorption column 37 pipeline 43 and 44 for selection of commodity alpha-olefin.

The best variant embodiment of the invention.

The method according to the invention perform the installation according to the invention as follows.

Raw - raw-HEXEN-1 from the raw material tank 1, under nitrogen atmosphere, which comes in the raw material tank 1 through the inlet 3, is supplied by pipeline 5 into the heat exchanger 6 where it is heated, and then flows into the bottom of reactor 4. Reactor 4 is filled selfactivity catalyst, such as cation exchange resin placed on neprovalnoy lattices. However, it is advantageous to use a mixture of cation exchange resin with aluminum oxide or silicon oxide, or a zeolite, or silica gel. The advantage that the catalyst had a full static volumetric capacity, mg·equn+/g of 4.3 to 4.5. The reactor is at atmospheric pressure in an atmosphere of nitrogen, which enters the reactor through the second inlet 7 and the same with the inert gas received in the raw capacity (hereinafter in the description of the unit operates in the presence of selected inert nitrogen gas). In the reactor 4 in the presence of the utilizator at a temperature of isomerization reactions 40-50° C and space velocity of the raw material, h-15-10, is the isomerization of impurities vinylidene olefins. In the selective isomerization of 2-ethylbutane-1, have very close boiling temperature with 1-hexene, vinylidene olefins are converted to internal olefins, predominantly 3-methylpentene-2, having a boiling point at 5-6°above the boiling point of 1-hexene. Isomerizate containing hexene-1 and samaritane impurities out through the upper exit of the reactor 4 and the pipe 9 is fed to the input capacitance 8 to collect the isomerized product. The container 8 is in the atmosphere of inert gas, which enters through another entrance 10. From the tank 8 through the pipe 12 isomerizate is supplied in the power zone of the distillation column 11. The output from the top of distillation column 11, where selected pairs of purified 1-hexene high purity, the pipe 20 enters the heat exchanger 21, where it cools, condenses and flows into the reflux tank 19. One part of 1-hexene by pipeline 23 is returned to the upper part of the distillation column 11 in the form of phlegmy. Low-boiling isomers of Cuba distillation column 11 partially through the pipeline 13 are received in the heat exchanger 14, where it is heated and returned to the cubic part of the distillation column 11 in the form of irrigation, and the remainder of the line is the gadfly 16 flows into the collector 15 cubic product, under nitrogen atmosphere, which enters through the inlet 17. Rectification in the first stage is performed at a pressure in the cube 850-820 mm Hg, the temperature of the cube 70-80°C, the temperature of the top - 60-65°and reflux among 4,5.

The other part of the partially purified 1-hexene by pipe 25 enters the power zone of the distillation column 24 for additional separation of 1-hexene and low-boiling impurities. The output from the top of distillation column 24 by conduit 30 enters the heat exchanger 31 where it is cooled, condensed and flows into the reflux tank 29. One part of purified 1-hexene by pipeline 33 is returned to the upper part of the distillation column 24 in the form of phlegmy, and the other part of the pipe 35 enters the collector 34 of purified 1-hexene in the atmosphere of inert gas, which is fed through the inlet 36. Part of the bottom liquid of the distillation column 24 through the pipe 27 enters the heat exchanger 28 where it is heated and returned to the cubic part of the distillation column 24 in the form of irrigation. The remainder of the bottom liquid through the pipeline 12 in the form of irrigation is served in the middle part of the distillation column 11. The distillation in the second stage is performed at a pressure 840-810 mm RT. Art., the temperature of the cube 70-80°C, the temperature of the top of 60-65°and reflux 3.

Purified hexene-1 containing kislorodsodyerzhascimi impurities, mostly water, hydrogen peroxide, alcohols, served piping 39 to the adsorption column 37 for complex purification from oxygen-containing impurities. As the adsorbent used Almagell and molecular sieves. The adsorption is carried out at a temperature of sorption 30-50°and a feed rate of 1-hexene 3-5 h-1in the atmosphere of nitrogen, which is fed through the heat exchanger 40.

It is advantageous to apply the adsorption complex purification from oxygen-containing impurities in the raw materials before entering into the reactor 4.

Hexene-1, purified from oxygen-containing impurities, the pipe 43 enters the collector 42 of 1-hexene polymerization of purity, which has an outlet 44 for its selection, and part of it is served in a middle zone of the distillation column 11 in the form of irrigation pipeline 41.

The best example embodiment of the invention.

The method is carried out on the installation according to the invention.

Raw materials - crude hexene-1 containing, in wt.%: HEXEN-1 - 95,2, 2-ethylbutane - 1-4,30, hexene-2 - 0,40, oxygen-containing impurities is 0.1, the container 1 in nitrogen atmosphere enters the heat exchanger 6, where it is heated to 45°and with a bulk velocity of 10 h-1enters the bottom of the reactor 4. Reactor 4 is filled selfactivity catalyst is a cation exchange resin, which is posted on neprovalnoy gratings and has full static surround the technology, mg·equn+/g to 4.5. The reactor is in a nitrogen atmosphere at a pressure of 1 ATM. In the isomerization of 2-ethylbutane-1 receive isomerizate containing, wt.%: HEXEN-1 - 93,5, hexene-2 - 2,10, 2-ethylbutane-1 - 0,07, 3-methylpentan-2 - 4,23, oxygen-containing impurities is 0.1.

Isomerizate from the upper outlet of the reactor 4 through the pipeline 9 is fed to the input capacitance 8 to collect isomerate and then in the power zone of the distillation column 11 of the first stage distillation temperature of the top 62°C, the temperature of the cube 72°C, pressure of nitrogen 840 mm RT. senior Rectification in the second stage in a distillation column 24 is performed at a pressure of 820 mm Hg, the temperature of the cube 72°C, the temperature of the top 62°C.

The entire method is carried out in nitrogen atmosphere, which protects the products of the process from contact with air and the formation of peroxide compounds.

Taken from the top of distillation column 24 HEXEN-1 contains oxygen-containing impurities, mainly water, hydrogen peroxide, alcohols, and fed through pipe 39 to the adsorption column 37 for complex purification from oxygen-containing impurities. As the adsorbent oxygen-containing impurities is used as an adsorbent containing Almagell and molecular sieves. The adsorption is carried out at a temperature of sorption 40°and feed speed - 4 hours-1in an atmosphere of nitrogen.

Taken from the top of the adsorption column 37 HEXEN-1 polymerization of purity (target product), contained, wt.%: HEXEN-1 - 99,83, 2-ethylbutane-1 - 0,06, hexene-2 - 0,05, 3 - methylpentan-2 - 0,06, oxygen-containing impurities are absent. Thus, the hexene-1 polymerization of purity, suitable for the production of linear polyethylene.

The present invention can be applied for the production of linear low-density polyethylene, in the production of polyolefin synthetic lubricating oils.

1. The method of purification of alpha-olefins comprising heating raw materials, isomerization vinylidene olefins in the feedstock in the presence of a catalyst and separation of the alpha-olefin from isomerized vinylidene olefins by distillation, characterized in that the separation of the alpha-olefin is conducted in at least two successive stages at the same temperatures of the top and Cuba, and decreasing the pressure of the distillation column each subsequent stage, in the power zone subsequent stage serves condensed phase, taken from the top of the rectifying column of the previous stage, each stage is applied irrigation distillation column at the top and bottom parts, and for irrigation of the upper part of the use of the condensed phase taken from the top of distillation columns the same stage for irrigation bottom part - cubic liquid of the distillation column of the same phase, and separated Alf is-olefin optionally purified from oxygen-containing impurities by adsorption to the polymerization of purity and partially return in the middle part of the distillation column of the first stage for supplemental irrigation, the heating of raw materials, isomerization, separation and adsorption is carried out in an atmosphere of inert gas.

2. The method of purification of alpha-olefins according to claim 1, characterized in that as the inert gas used nitrogen.

3. The method of purification of alpha-olefins according to claims 1 and 2, characterized in that the reactor as the catalyst used selfactivity catalyst or a mixture of cation exchange resin with aluminum oxide or silicon oxide, or a zeolite, or silica gel having a full static volumetric capacity, mg·equn+/g 4,3-4,5.

4. The method of purification of alpha-olefins according to claim 1, wherein the adsorption is carried out at a temperature of 30-50°C.

5. The method of purification of 1-hexene comprising heating raw materials, isomerization vinylidene olefins in the feedstock in the presence of a catalyst and the separation of 1-hexene from isomerized vinylidene olefins by distillation, characterized in that the separation of 1-hexene spend at least two successive stages at a temperature of the top of the distillation column each stage equal to 60-65°C, the temperature of the rectifying column bottom of each stage is equal to 70-80°and decreasing the pressure of each subsequent stage 20-40 mm RT. Art. in the power zone subsequent stage serves condensed phase, taken from the top of the rectifying column of the previous stage, each stage is remaneat irrigation distillation column at the top and bottom part, and for the irrigation of the upper part of the use of the condensed phase, taken from the top of distillation columns the same stage for irrigation bottom part - cubic liquid of the distillation column of the same phase, separated hexene-1 is additionally clear of oxygen-containing impurities by adsorption to the polymerization of purity and partially return in the middle part of the distillation column of the first stage for supplementary irrigation, and the heat of raw materials, isomerization, separation and adsorption is carried out in nitrogen atmosphere.

6. The method of purification of 1-hexene according to claim 5, characterized in that the adsorption is carried out at a temperature of 30-50°and as the adsorbent used adsorbent containing Almagell and molecular sieve.

7. Installation for the purification of alpha-olefins containing reactor for isomerization vinylidene olefins in raw materials and the distillation column, the zone diet which is connected to the output of the reactor, and from the top of which are selected alpha-olefins, characterized in that it contains at least one distillation column for further purification of alpha-olefin from isomerized vinylidene olefins, the zone diet which is connected with the output of the previous top of the distillation column, the top of which is connected through the heat exchanger with its irrigation zone top and CBM output is outinen through the heat exchanger with its irrigation zone a bottom part, and the adsorption column to remove oxygen-containing impurities in alpha-olefins of high purity, the entrance of which is associated with the release of the top of the last distillation column for further purification of alpha-olefins, one output is connected to the middle part of the first distillation column, and the other output is used to display alpha-olefins polymerization of purity.

8. Installation according to claim 7, characterized in that the VAT output of the distillation column for further purification of alpha-olefins from isomerized vinylidene olefins is connected to the middle part of the previous distillation columns.



 

Same patents:

The invention relates to petrochemistry, namely the production of oligomers of propylene by oligomerization of propylene in phosphoroclastic catalysts and the method of purification of oligomers of propylene

The invention relates to the petrochemical industry, for production of high-purity benzene, used in the petrochemical syntheses

The invention relates to a method of purification of benzene from coke production and benzene obtained from fractions of pyrolysis oil from impurities saturated and unsaturated hydrocarbons, thiophene and carbon disulfide

The invention relates to the petrochemical industry, for the purification of benzene, obtained from a liquid hydrocarbon, C6-C7- fractions of pyrolysis oil from impurities unsaturated hydrocarbons
The invention relates to the field of production of high-purity benzene, namely, to clean it from thiophene

The invention relates to a method of purification of terpene hydrocarbons from sulfur and can be used in the chemical and pulp and paper industry

The invention relates to a technology for purifying styrene from inhibitor and moisture and can be used in the synthetic rubber industry, in particular when cleaning for the synthesis of styrene butadiene-styrene rubber

The invention relates to the processing of natural or associated gas, namely, the drying and cleaning of gas from sulfur compounds, adsorption, and can be used in gas, oil, refining and petrochemical industries

The invention relates to a method for producing polymer products, which after a special cross-linkage become macroplastique (macrostate - approx

The invention relates to the field of organic chemistry, namely the method of purification of benzene from sulfur compounds

The invention relates to the field of adsorptive separation of hydrocarbon mixtures, in particular adsorption methods of purification of liquid paraffins from aromatic hydrocarbons, and can be applied in the refining and petrochemical industry

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: crude alpha-olefin is heated, raw vinylidene olefins are isomerized in the presence of catalyst and alpha-olefin is separated from isomerized vinylidene olefin by rectification. Separation of alpha-olefin is carried out for at least two successive steps at similar temperatures on top of vat and reducing pressure of rectifying column at each following step. Condensed phase removing from top of the rectifying column at previous step is fed to feeding zone of the following step and the rectifying column at top and vat section is sprayed. For spraying the top section of column the condensed phase removing from the top of rectifying column at the same step is used and for spraying the vat section of column the vat liquid of rectifying column at the same step is used. Separated alpha-olefin is purified additionally from oxygen-containing impurities by adsorption up to polymerization degree of purity. Raw heating, isomerization, separation and adsorption are carried out in atmosphere in inert gas. The unit used for treatment of alpha-olefin includes reactor for isomerization of vinylidene olefins in raw, rectifying column wherein feeding zone is joined with reactor outlet and wherein alpha-olefin of high purity degree is removed from the column top. The unit includes also at least one rectifying column for additional treatment of alpha-olefin of high purity from isomerized vinylidene olefins and adsorption column for separation of oxygen-containing impurities in alpha-olefin of high purity wherein the column inlet is joined with the top outlet of the last rectifying column used for additional treatment of alpha-olefin of high purity and outlet is used for removing alpha-olefin of the polymerization purity degree. Invention provides enhancing quality of the end product.

EFFECT: improved method for treatment.

8 cl, 1 dwg, 1 ex

Up!