The method of separation of isobutylene from the containing hydrocarbon mixtures

 

(57) Abstract:

Use: for production of isobutylene, tertiary butyl alcohol and purification of hydrocarbon fractions from isobutylene. The inventive produce isobutene from hydrocarbon mixtures containing it, by countercurrent liquid-phase contacting the mixture with water in the column in the presence of an acidic heterogeneous catalyst with the conclusion on top of the column unreacted hydrocarbons from the middle of the reaction zone a mixture of hydrocarbons and tert.-Bhutan, from which the hydrocarbon is separated and returned to the column and from the bottom of the aqueous solution of tert.-butanol, which is then subjected to decomposition. Moreover, in the column above and below the reaction zone are extraction zone provided with an inert mass smennymi elements or nozzle. The original hydrocarbon mixture is fed from below the bottom of the extraction zone, and an aqueous solution of tert. -butanol, the waste from the bottom of the reaction zone is divided into two streams in a ratio of 1 to 4 1 to 4, one of which is directed at the bottom of the extraction zone and then from the cube columns returned in its middle part, and another thread napravlyayut in the site and/or decomposition of tert.-butanol and water return on ver the hydrogen phase, and 1.3 5.3 times to reduce the amount of aqueous solution of tert.-butanol supplied for further processing, which allows to reduce the consumption of power and capital costs. 1 Il. table 2.

The invention relates to a method of separation of isobutene from a hydrocarbon fractions by treating them with water in the presence of an acid catalyst with the formation of tertiary butyl alcohol, which is then subjected to decomposition with obtaining isobutylene or used as a commercial product.

Known purification method WITH4-hydrocarbon fractions from isobutylene by countercurrent contact of the initial fraction of water in the column in the presence of molded ionite catalyst located in the reaction zone of the specified columns with output in the form of the top product purified from isobutylene WITH4-hydrocarbon fraction in the form of lower product aqueous solution of tertiary butyl alcohol, which is fed to the rectification.

In the known method the rate of water flow is 5-30 m/h and the speed WITH4-hydrocarbon fraction in the catalyst layer of 0.0005-0,020 m/C. the Process is carried out at 70-130aboutWith pressure sufficient to perform the reaction in Finance this way the efficiency of the process of hydration increases with increasing linear velocity of the water and the concentration of isobutylene in the faction. When the process linear velocity of water more than 10 m/h high conversion can be obtained with a volume ratio of water and C4-hydrocarbon fraction is not less than 8.

The disadvantage of this method is the large number of circulating process water, which entails high costs of energy and the increase in the equipment.

Closest to the proposed method to the technical essence and the achieved result is a cleaning method WITH4-hydrocarbon fractions from isobutylene by countercurrent contact of the initial fraction of water in the column in the presence of ion exchangers molded catalyst located in the reaction zone of the specified columns, with output in the form of the top product is purified WITH4-hydrocarbon fraction, in the form of lower product aqueous solution of tert-butanol and in the form of a side selection of the reaction zone WITH4-hydrocarbon fraction containing 5-50 wt. tertiary butyl alcohol, which serves to further purification by separation of tertiary butyl alcohol and cleaning products. Cleaning product4-hydrocarbon recycle fraction to the reaction zone.

Water is fed into the upper part of the reaction zone is RA 0,0005 at 0.020 m/s Hydrocarbon fraction containing 5-50 wt. tertiary butyl alcohol is withdrawn from the reaction zone and, using known methods (distillation, washing, etc.), carry out the separation of tertiary butyl alcohol from the faction. Purified from tert-butanol hydrocarbon fraction is again fed into the column in the same area.

In the support column temperature of 70-130aboutAnd pressure sufficient to perform the reaction in the liquid phase. Purified from isobutylene WITH4-hydrocarbon fraction selected from the top of the column. An aqueous solution of tert.-butanol deduce from the bottom of the column and serves on the concentration. Tert.-the butanol is separated from C4-hydrocarbon fractions, mixed with a concentrated aqueous solution and further decompose with the release of isobutylene, or used to produce anhydrous tert-butanol. The ratio of water:the faction is about 6./about.

Although the known method reduces the number of circulating process water, the latter remains significant when conducting the process with high productivity and deep degree of extraction of isobutylene.

The invention is directed to increasing the share of tert.-butanol output from the hydrocarbon fraction in the Yu recycling and reduction due to this volume of the apparatus, i.e., capital cost and cost of energy.

The problem is solved in that in the method of separation of isobutylene from the containing hydrocarbon mixtures by countercurrent liquid-phase contacting the mixture with water in the column in the presence of an acidic heterogeneous catalyst located in the reaction zone of the column, with the conclusion on top of the column unreacted hydrocarbons from the lower portion of the reaction zone an aqueous solution of tert.-butanol, then supplied to the decomposition of the isobutylene and water, with a selection from the middle part of the reaction zone a mixture of hydrocarbons and an aqueous solution of tert.-butanol, followed by the separation from the mixture of hydrocarbons is returned to the reaction zone, use the column having top and bottom of the extraction zone, located respectively above and below the reaction zone and is equipped with an inert mass transfer elements or nozzle, and the original hydrocarbon mixture is fed to the lower part of the bottom of the extraction zone, the water in the upper part of the top of the extraction zone, and an aqueous solution of tert.-butanol, the output from the reaction zone is divided into two streams in a mass ratio of from 4:1 to 1:4, one of whom serves on the degradation of sursaut in the reaction zone.

Distinctive features of the prototype features are the following: the presence of two extraction zones located above and below the reaction zone and filled with mass-exchange elements or nozzle, the filing of the original hydrocarbon mixture at the bottom of the extraction zone, separating an aqueous solution of tert.-butanol extending from the bottom of the reaction zone, into two streams in a ratio of from 4:1 to 1:4, one of which is directed at the bottom of the extraction zone, and then from the bottom of the tower is returned to the reaction zone, and the other stream is sent to the node distillation and/or decomposition of tert.-butanol and water after decomposition of tert.-butanol return to the top of the top of the extraction zone.

The drawing is a flow diagram of the proposed method.

The method is as follows. In the upper part of the Hydrator 1, representing the column, the average area of which is filled with catalyst, and the upper and lower zones of the inert mass transfer elements or nozzle, water is supplied through line 2. Hydrocarbon fraction through line 3 serves on the bottom of the bottom of the extraction zone of the column.

The acid catalyst of the type KU-PPP representing a molded mixture of powdered sulfonated copolymer with the Anna mixture of a copolymer of styrene with divinylbenzene and a thermoplastic material, made in the form of granules of various shapes, including cylinders size 5x10 mm

The isobutene reacts with water on the catalyst with the formation of tertiary butyl alcohol, which is distributed between water and the hydrocarbon fraction. The resulting tertiary butyl alcohol is removed from Hydrator two threads: in line 4 with the hydrocarbon fraction from the reaction zone and with the water flow line 5 from the bottom of the reaction zone. The hydrocarbon stream is directed in column 6, where the tertiary butyl alcohol is separated from the hydrocarbon fraction and output in the form of the cubic product.

An aqueous stream containing tert.-butanol, is subjected to the concentration in the column 7, and then with tert-butanol is separated from the hydrocarbon stream is directed to the enhanced removal WITH4-hydrocarbons and further decomposition to obtain isobutylene purity of 99.99% On line 8 water from the column 7 is served on the top of the column 1. Hydrocarbons from the column 6 through line 9 return to the reaction zone.

An aqueous solution of tert.-butanol can be used for decomposition without concentration, and tertiary butyl alcohol is separated from the hydrocarbon fraction can be used to obtain bisognano to perform the reaction in the liquid phase.

Purified from isobutylene hydrocarbon fraction deduce from the top of the top of the extraction zone of the column through line 10.

Water from the bottom of the bottom of the extraction zone is available on line 11 up reaction zone of Hydrator.

In the proposed method, the share of tert.-butanol extracted with a hydrocarbon stream reaches 80% vs. 46% in the known method, for a fraction containing 38-40% of isobutylene.

Saving energy is 0.4 kg/t of isobutylene.

The method is illustrated by the examples presented in table. 1, 2.

P R I m e R s 1-4. In Hydrator representing a column of steel 18CR10NITI height of 8 m and an inner diameter of 200 mm, load 230 l catalyst obtained by extrusion of a mixture consisting of 70 wt.h. powdered sulfonated copolymer of styrene with divinylbenzene and 30 wt.h. polypropylene, and 22 l of the nozzle in the form of Raschig rings size 15x15 11 l above and below the catalyst bed. The catalyst has a static exchange capacity

3,0

C4-hydrocarbon fraction containing 38% of isobutylene in number according to the table. 1, 2, and serves on the bottom of the bottom of the extraction zone.

Water in an amount according to the table. 1, 2 serves up the top of extraction the x2">

The temperature in the reaction and extraction zones is 85-90aboutWith the pressure of 18-20 ATM.

The resulting tert. -butanol is removed from the reaction zone at the level of 1/3 of the layer with the hydrocarbon fraction in number according to the table. 1, 2 and with the aqueous phase in amounts according to table. 1, 2 from a bottom of the reaction zone.

A hydrocarbon stream containing tert.-butanol is sent to a distillation column with number plates 15. Rectification lead with a reflux ratio of 0.5. After separation of tert.-butanol hydrocarbon fraction return to the same area.

Water stream coming from the bottom of the reaction zone is divided into two streams in the ratio according to table. 1, the first of which in number according to the table. 1, 2 is removed from Hydrator and sent to concentration in the distillation column with the number of plates 40. Rectification lead with a reflux ratio of 0.4-1, the second thread in number according to the table. 1 enters the bottom of the extraction zone. The water coming from the bottom of the column is directed to the top of the reaction zone.

Purified from isobutylene fraction in number according to the table. 1, 2 and containing isobutene in a quantity according to table. 1. 2 deduce from the top of the column. For comparison in the table. 1, 2 shows the use of the in gidratatini, represents a column of steel 18CR10NITI, the height of 7.3 m with an inner diameter of 200 mm was charged To the reactor 230 l of catalyst as in examples 1-4.

WITH4-hydrocarbon fraction containing 38% of isobutylene, in number according to the table. 1, 2 and serves on the bottom of Hydrator.

Water in an amount according to the table. 1, 2 served at the top of Hydrator. The volumetric ratio of water supplied and4-hydrocarbon fraction are presented in table. 1. The temperature of hydration 85-90aboutWith the pressure of 18-20 ATM.

The resulting tert. -butanol is removed from the reaction zone at the level of 1/3 of the catalyst with the hydrocarbon fraction in number according to the table. 1, 2 and with the aqueous phase in amounts according to table. 1, 2 with the bottom of the tower.

An aqueous solution of tert.-butanol from the bottom of the column serves on the concentration in the distillation column as in examples 1-4.

The hydrocarbon fraction is subjected to rectification in the column with the number of plates 15 and reflux ratio of 0.5, and return in Hydrator at the same level.

The share of tert.-butanol, extracted with a hydrocarbon fraction, in comparison with tert.-butanol derived with the aqueous phase from the bottom of the column shown in the table. 1.

P R I m e R 5. In Hydrator, pry the catalyst offretite, representing granules of cylindrical shape with a diameter of 1.5 mm, a length of 3-10 mm in the number 0,880 L.

Top and bottom layer of catalyst placed the nozzle in the form of ceramic rings size 5x6 mm in a volume of 0.16 l

WITH4-hydrocarbon fraction containing 46% of isobutylene, in the amount of 32,8 g/h, serves on the bottom of the bottom of the extraction zone, and water in an amount 95,1 g/h in the top of the top of the extraction zone.

The volumetric ratio of water supplied and4-hydrocarbon fraction is 1:1.

The temperature in the reaction and extraction zones 115-120aboutWith the pressure of 29 bar.

Hydrocarbon fraction, passing the bottom of the extraction zone and 1/2 of the catalyst layer with the amount of catalyst 0.4 l, contains 16.8 percent of isobutylene and 34.4% of tert. -butanol and displayed in a distillation column for separation of tert.-butanol in the form of the cubic product. The distillate FROM4-hydrocarbon fraction from the top of the column is directed into the reaction zone at the level of the sampling fractions with tert.-butanol and passes the rest of the catalyst layer and the upper otryvnuju zone. From the top of Hydrator displayed WITH4-hydrocarbon fraction in the number 32,8 g/h containing 3% of isobutylene.

Water is AdRotator and sent to distillation column at a concentration, second in number 107,04 g/h enters the bottom of the extraction zone and passing it, recycle to the top of the reaction zone.

The amount of tert.-butanol, extracted with hydrocarbon and water streams, respectively 68,4 and 31.6% of the total number of generated alcohol.

P R I m e R 6. In Hydrator described in example 5, download the cation exchanger KU-23 representing macroporous sulfonation into balls the size of 0.3-1.2 mm in the number of 1,075 HP

From the bottom and from the top of the catalyst layer is placed the nozzle in the form of ceramic rings size 5x6 mm number 0,161 and 0,064 l, respectively.

WITH4-hydrocarbon fraction containing 46% of isobutylene, in the amount of 38,08 g/h serves on the bottom of the bottom of the extraction zone, and water in an amount 127,94 g/h in the top of the top of the extraction zone. The volumetric ratio of water supplied and4-hydrocarbon fraction is 2:1.

The temperature in the reaction and extraction zones supported 115-120aboutWith the pressure of 29 bar.

Hydrocarbon fraction, passing the bottom of the extraction zone and 1/3 part of the catalyst layer with the amount of catalyst 0,36 l and containing 15.9% of isobutylene and 33.9% tert.-butanol is displayed in the native fraction from the top of the column is directed into the reaction zone at the level of the sampling fraction and passes the rest of the catalyst layer and the upper otryvnuju zone. From the top of Hydrator output WITH4-hydrocarbon fraction in the amount of 20.7 g/h containing 0,76% of isobutylene.

The water stream leaves the bottom of the reaction zone and is divided into two streams: the first in the number of 129.6 g/h is removed from Hydrator and sent to rectification column on the concentration, the second in the amount of 135,7 g/h enters the bottom of the extraction zone and passing it, recycle to the top of the reaction zone.

The number of rubs. -butanol, extracted with hydrocarbon and water streams is 63,4 - and 36.6%, respectively, of the total generated amount of alcohol.

The proposed method resulting from the reaction of tertiary butyl alcohol is excreted in the hydrocarbon and water phases, the number of rubs. -butanol output from the hydrocarbon phase is increased by 10-35% and the amount of aqueous solution of tert.-butanol supplied for further processing, is reduced from 1.3 to 5.3 times. This allows to reduce the consumption of power and capital costs.

The METHOD of separation of ISOBUTYLENE FROM the CONTAINING HYDROCARBON MIXTURES by countercurrent liquid-phase contacting the mixture with water in the column in the presence of acid heterosuggestion, from the bottom of the reaction zone an aqueous solution of tertbutanol, then supplied to the decomposition of the isobutylene and water, with a selection from the middle part of the reaction zone a mixture of hydrocarbons and an aqueous solution of tertbutanol with subsequent separation from the mixture of hydrocarbons is returned to the reaction zone, characterized in that use column having top and bottom of the extraction zone, located respectively above and below the reaction zone and is equipped with an inert mass transfer elements or nozzle, and the original hydrocarbon mixture is fed to the lower part of the bottom of the extraction zone, the water in the upper part of the top of the extraction zone, an aqueous solution of tertbutanol, the output from the reaction zone is divided into two streams in a mass ratio of from 4: 1 to 1:4, one of whom serves on the decomposition, and the second serves in the upper part of the bottom of the extraction zone, and extending from the lower part of the column, the flow returns to the reaction zone.

 

Same patents:
The invention relates to the field of allocation of tertiary olefins from mixtures of hydrocarbons of varying degrees of saturation and can be used in the production of monomers for IC
The invention relates to the separation of tertiary olefins from mixtures of hydrocarbons of varying degrees of saturation and can be used in industry to obtain monomers for IC

The invention relates to a catalyst obtain isobutene by dehydroisomerization n-butane, the method of its production and method of use of this catalyst

The invention relates to a method of processing paraffin hydrocarbons, particularly to carbon dioxide conversion (dehydration) of isobutane to isobutylene and carbon monoxide, and can be used in chemical, oil and gas industry

FIELD: chemical industry; methods of production of the pure isobutene out of the isobutene-containing mixture.

SUBSTANCE: the invention is pertaining to the method of production of the pure isobutene out of the isobutene-containing mixture predominantly - out of hydrocarbon С4 with usage of the catalysis by the strong-acid cationite(s) including the liquid-phase interaction of the isobutene with the water at the temperature of from 60 up to 130°С in one or several sections at the stage of hydration, delamination of the being withdrawn from it stream(s), distillation of the unreacted hydrocarbons С4 from the hydrocarbon layer, decomposing of the tret-butanol in the section(s) at the stage of dehydration, separation of the formed isobutene from the water and its) purification and characterized by that isobutene and the total amount of the returned from the stage of dehydration fresh water is fed in the section of hydration in the total molar ratio from 1:0.4 up to 1:20, and it is preferential from 1:1 up to 1:5, in the straight-flow or bubbling mode in the absence of the emulsifier hydrate from 30 up to 97 % of isobutene. From the stage of the hydration in the stage of the dehydration at least one-third of the produced tret-butanol is fed in the stream, separated by the rectification from the layer of the unreacted hydrocarbons and containing from 5 up to 30 mass % of the water, and, possibly, the rest amount - in the stream of the water layer, at the total content of the different, than the isobutene, the hydrocarbons not exceeding their admissible quantity in the target isobutene, and from the stage of the dehydration the water at least partially is returned into the stage of the hydration. The presented method requires the low power input and the low metal input.

EFFECT: the invention ensures the low power input and the low metal input.

14 cl, 2 dwg, 4 ex

FIELD: petrochemical processes.

SUBSTANCE: invention is directed to processing of isobutene-containing hydrocarbon mixture preferably containing C4-hydrocarbons, which processing comprises interaction of isobutene contained therein with methanol in presence of acidic solid catalyst in one or several zones of synthesis of methyl tert-butyl ether followed by distilling off unreacted C4-hydrocarbons from reaction mixture, withdrawing, as more high-boiling residue, stream containing methyl tert-butyl ether, which is fully or partially supplied to ether decomposition zone, decomposing methyl tert-butyl ether in presence of high-acid solid catalyst, distilling off reaction products of stream preferably containing isobutene, methanol , and minor portion of non-decomposed methyl tert-butyl ether, withdrawing the rest of more high-boiling product containing predominantly methyl tert-butyl ether from the system or recycling it to ether decomposition zone, rectifying distilled-off stream predominantly containing isobutene, methanol, and minor portion of non-decomposed methyl tert-butyl ether, wherein stream mainly containing isobutene is distilled off and more highly boiling residue containing methanol and ether is subjected to additional rectification at lower pressure, recycling bottom residue containing mostly methanol to ether synthesis zone and distillate to distillation zone next after decomposition zone, recovering methanol by water extraction from mainly isobutene-containing stream, freeing washed isobutene stream from dimethyl ether by rectification, wherein stream containing dimethyl ether and isobutene is withdrawn as distillate and purified isobutene is recovered as more high-boiling bottom residue or, in case of heteroazeotropic drying of isobutene jointly with removal of dimethyl ether, stratifying resulting distillate and discharging water and hydrocarbon streams while recovering purified isobutene as more high-boiling bottom residue. Process is characterized by that decomposition of methyl tert-butyl ether is conducted at pressure assuring liquefied state of substances and temperature 60-120°C, stream obtained as distillate of rectification of washed out isobutene stream and containing dimethyl ether and isobutene or hydrocarbon stream containing dimethyl ether and obtained after stratification of distillate of heteroazeotropic drying of isobutene is recycled to methyl tert-butyl ether decomposition zone.

EFFECT: reduced formation of dimethyl ether and increased productivity of plant.

2 dwg, 9 tbl, 9 ex

FIELD: chemistry.

SUBSTANCE: invention pertains to the method of separating polymerisation pure isobutylene by liquid phase contacting with a hydrocarbon fraction, containing isobutylene, with water in a column type reaction system in the presence of an acidic heterogeneous catalyst, located in the reaction zone(s) of the reaction system. Unreacted hydrocarbons are extracted. The tert-butanol formed is separated and directed for disintegration with formation of isobutylene. The method is characterised by that, the hydrocarbon fraction before contacting with water is mixed with isobutylene, obtained by disintegration of methyl-tert-butyl ether, in mass ratios ranging from 10:1 to 1:1.5.

EFFECT: higher efficiency of the process.

3 cl, 1 tbl, 4 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention refers to method of isobutylene production by decomposition methyl-tertiary-butyl ether with heterogeneous catalyst at raised temperature and pressure, characterised that catalyst is multi-purpose synthetic zeolite NaX, while process is enables at atmospheric pressure with water vapour with observing the conditions as follows: temperature 200-250°C, volumetric MTBE feed rate 1.0-2.0 h-1. These conditions ensure minimal generation of MTBE decomposition by-products.

EFFECT: MTBE conversion per run is 96-99% with isobutylene selectivity at least 99%.

1 cl, 3 tbl, 9 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of extracting isobutylene from an isobutylene containing fraction through hydration of the isobutylene containing fraction, obtaining a tert-butanol containing fraction and its subsequent dehydration. The method is characterised by that, dehydration is done in two stages. At the first stage, temperature is kept at 90-120°C and pressure at 1-3 kgf/cm2 and concentrated isobutylene and an aqueous solution of tert-butyl and sec-butyl alcohol are extracted, from which concentrated sec-butyl alcohol and an isobutylene containing fraction, which is taken for hydration, are extracted at the second stage. Process at the second stage is carried out at temperature 100-130°C and pressure 2-6 kgf/cm2.

EFFECT: use of the given method allows for extracting isobutylene without butene or butadiene impurities, and reduction of tert-butyl alcohol loss.

1 cl, 1 tbl, 8 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing isobutylene and butadiene-1,3 through catalytic dehydrogenation of corresponding paraffin hydrocarbons on a chromia-alumina catalyst at high temperature, separation of dehydrogenation products through absorption-desorption and extractive rectification, obtaining commercial-grade isobutylene and butadiene-1,3 of C4 olefin hydrocarbons, unconverted paraffins and combustible wastes: "light" and "heavy" unabsorbed gases and butadiene-acetylene concentrate, where the mixture of "heavy" unabsorbed gases with butadiene-acetylene concentrate and part of "light" unabsorbed gases is passed through a binary hydrogenation bed, one of which is nickel-chrome and the other aluminium-palladium, and a propane fraction is obtained at the output.

EFFECT: use of the given method increases utilisation of combustible wastes, obtaining a commercial-grade propane fraction through catalytic hydrogenation and longer service life of the catalyst.

1 cl, 1 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for synthesis of isobutene, isoprene and possibly tertbutanol from isobutene-containing C4-fraction(s), involving hydration of isobutene in C4-fraction(s), distillation of unreacted C4-hydrocarbons from tert-butanol, dehydration of tert-butanol, bringing isobutene-containing C4-fractions and possibly tert-butanol into contact with aqueous solution(s) of formaldehyde and acid, distillation of at least the remaining C4-hydrocarbons and decomposition of intermediate products at high temperature with formation and subsequent extraction of isoprene and isobutene, characterised by that the initial isobutene-containing fraction(s) is at least partially hydrated on a sulfo-cation catalyst in a hydration unit with moderate supply of water in an amount which compensates for its consumption in the reaction with isobutene and output as part of an organic layer which mainly contains a mixture of unreacted C4-hydrocarbons and tert-butanol formed during isobutene conversion ranging from 40 to 80%, a distillation stream mainly containing tert-butanol is extracted from at least part of the said organic layer, as well as a stream of unreacted C4-hydrocarbons containing from 10 to 40% isobutene, which is brought into contact with aqueous solution(s) of formaldehyde and acid and intermediate products formed after distillation of at least the remaining C4-hydrocarbons are subjected to liquid-phase or gas-phase catalytic decomposition at high temperature with formation of isoprene, isobutene and by-products, and the said stream which mainly contains tert-butanol is at least partially fed into the intermediate product decomposition zone directly and/or after coming into contact with at least aqueous solution(s) of formaldehyde and acid in an additional reaction zone, and the remaining part of the said stream which mainly contains tert-butanol is dehydrated to obtain isobutene.

EFFECT: use of the method reduces supply of water and associated power consumption.

8 cl, 1 dwg, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing isobutylene through decomposition of methyl-tert-butyl ether on a heterogeneous catalyst at high temperature, characterised by that the catalyst used is a calcium-boro-phosphate catalyst and the process is carried out at atmospheric pressure in the presence of water vapour with the following conditions: temperature 200-250°C, volume rate of feeding methyl-tert-butyl ether 1.0-2.0 h-1.

EFFECT: use of the method increases conversion of methyl-tert-butyl ether in per pass.

1 cl, 3 tbl, 8 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of decomposing high-boiling by-products of production of isoprene from isobutylene and formaldehyde by mixing high-boiling by-products with superheated water vapour and contact with a catalyst in one or two deck-type reactors while heating to obtain isoprene, formaldehyde and isobutylene, characterised by that liquid high-boiling by-products are first evaporated and superheated to temperature 300-350°C together with water vapour in ratio 1:1.0-1.2 in the convection part of a vapour-superheating furnace in a system of straight pipes fitted with a self-contained collector, and then mixed in a mixer with superheated water vapour to weight ratio 1:3.0-4.0, and then fed at 400-450°C into a reactor, in the over-catalyst zone of which there is a clearing-distribution grid with common clear area of 15%, having 20 mm holes and caps with diameter of 100 mm and height of 80 mm.

EFFECT: use of the present method enables to loser specific consumption of water vapour when splitting high-boiling by-products with simultaneous increase in output of desired products.

2 cl, 3 ex, 1 dwg

FIELD: blasting.

SUBSTANCE: invention relates to a method for joint production of isobutene and butadiene by dehydration of C4-hydrocarbons on a chromia-alumina catalyst at higher temperature with further separation of finished products of dehydration by methods of absorption-desorption and extractive rectification and release of commercial isobutene and butadiene -1,3. At the same time the method is characterized by the fact that C4-hydrocarbons are a mixture of hydrocarbons of the following composition, wt %: isobutane 15÷45, n-butane 15÷60, n-butenes 20÷45.

EFFECT: using this method makes it possible to produce isobutene and butadiene in one reactor with high yields.

1 cl, 1 tbl, 4 ex

FIELD: petrochemical industry; methods of hydrocarbon mixtures refining.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to refining of the hydrocarbon mixtures. The invention provides for refining of a hydrocarbon mixture containing iso- and normal butanes and, probably, the butanes containing as a minimum two stages of the contacting with the solid high-acidic catalyst(s). The mixture first is exposed to refining at the stage(-s) mainly of the primary transformation of isobutene: from the product(-s) distil off a mixture of the non-reacted hydrocarbons C4, which then is exposed to a liquid-phase refining at the stage(-s) of the primary transformation of n-butanes and from the product distil off the non-reacted hydrocarbons containing predominary butanes. At the stage(-s) of the primary transformation of isobutene the contacting is carried out at the presence of water and-or alcoholC1-C2 in a quantity sufficient for transformation of the majority of isobytene into tret-butanol and-or into alkyl-tret-butyl ether. At the stage of primary transformation of n-butenes feed the mixture of the non-reacted hydrocarbons containing no more than 8 % of isobutene and admixture of water and-or alcohol from a previousa stage (-s) and the majority of n-butenes transform into dimers and codimers of n-butenes at the temperature of as a minimum by 15°C higher, than at the stage(-s) of the primary transformation of isobutene. The technical effect: transformation of the tret-alkenes into the oxygen-containing products having the high octane numbers.

EFFECT: the invention ensures transformation of the tret-alkenes into the oxygen-containing products having the high octane numbers.

11 cl, 2 tbl, 4 ex

FIELD: petrochemical processes.

SUBSTANCE: alcohols such as tert-pentanol or tert-butanol are obtained via liquid-phase hydration of alkenes contained in hydrocarbon feedstock in presence of solid high-acidity catalyst at elevated temperature in two consecutive stages followed by separation of unreacted hydrocarbons from reaction mixture withdrawn, preferably via rectification, from the second stage and containing synthesized alcohols. In the first reaction stage carried out at higher temperature, reaction zone(s) comprises two liquid phases, of which phase containing basically water, is in essential weight excess and phase mainly containing hydrocarbon(s) is in dispersed state. Withdrawn is only or mostly (i) liquid stream containing mainly hydrocarbon(s), synthesized alcohol(s), and dissolved water and optionally (ii) liquid stream containing basically water and alcohol(s). The latter, in the second stage, is fed through distribution device(s) into one or several in series arranged reaction zones, water being introduced into one or several reaction zones separately, and liquid in the second-step reaction zones, operated at lower temperature, is maintained in homogenous or heterogeneous state wherein one phase containing basically water and alcohol(s) is in dispersed state and its weight does not exceed 25% of the weight of phase basically containing hydrocarbons and alcohol(s).

EFFECT: increased conversion of feedstock and accelerated reaction.

12 cl, 1 dwg, 3 tbl, 6 ex

FIELD: industrial organic synthesis.

SUBSTANCE: objective of invention is production of tert-butanol suitable as solvent and organic synthesis intermediate, in particular as raw material in production of pure isobutylene. Process comprises hydration of isobutylene at elevated temperature and pressure in a column-type reactor unit filled with molded ionite catalyst in H-form. Isobutylene-containing C-4-hydrocarbon fraction is brought into countercurrent contact with water. Exhausted C-4-fraction is removed from the top portion of reactor unit. Aqueous solution of tertiary butyl alcohol is withdrawn from the bottom portion of reactor unit. From the reaction zone is tapped stream containing hydrocarbons and tertiary butyl alcohol, which stream is then separated to remove and return hydrocarbons into reactor unit. Reactor unit comprises at least two catalyst beds and at least one catalyst-free zone between catalyst beds, out of which stream containing hydrocarbons and tertiary butyl alcohol is taken off. Fresh and recycled hydrocarbons are supplied to reactor unit at temperature by 20 to 120°C below temperature of water supplied to reactor unit.

EFFECT: reduced consumption of water employed for hydration at the same high degree of isobutylene conversion and high productivity, and also reduced consumption of power.

4 dwg, 5 ex

Up!