RU2394806C1 - Method of producing tertiary butanol - Google Patents

Abstract

FIELD: chemistry. ^ SUBSTANCE: invention relates to a method of producing tertiary butanol which is used as a solvent and a semi-finished product in organic synthesis. The method involves hydration of isobutylene at high temperature and pressure by bringing a hydrocarbon phase containing isobutylene into contact with an aqueous phase mainly containing water with dispersion of one phase into the other in flow-type and extraction-reaction type reactors filled with heterogeneous acid catalysts while feeding water for hydration into both reactors and an initial stream of hydrocarbons which contains isobutylene into the flow-type reactor, and output of a stream of hydrocarbons from the flow-type reactor which contains tertiary butanol, division of the said stream of hydrocarbons through fractionation into a stream which contains a concentrated solution of tertiary butanol and a stream which mainly contains unreacted hydrocarbons, and feeding the latter into the extraction-reaction type reactor opposite a stream which mainly contains water. A large amount of isobutylene taken for hydration is converted to tertiary butanol in a flow-type reactor and the process in this reactor is carried out while dispersing the aqueous phase in a solid stream of the hydrocarbon phase and temperature of the aqueous stream fed to the input of the flow-type reactor is 5-50C lower than temperature of the aqueous stream fed into the extraction-reaction reactor. ^ EFFECT: conditions for realising the method enable to increase degree of conversion of isobutylene and also reduce excessive use of water and, as a result, reduce power and material consumption on producing the end product. ^ 2 dwg, 4 ex

Description

The invention relates to the production of tertiary butanol (TB), which is used as solvents and intermediates for organic synthesis, in particular, to obtain pure isobutylene and isoprene.

A known method for producing TB by the interaction of an isobutylene-containing fraction of hydrocarbons with water in the presence of a heterogeneous cation exchange catalyst at a temperature of 70-130 ° C and a pressure of 10-50 atm, in which water is supplied to the top of the hydration reactor as a continuous phase, and the isobutylene-containing fraction of hydrocarbons in the form the dispersed phase is fed through a switchgear to the bottom of the hydrator reactor. The speed of movement of droplets of hydrocarbons through the continuous phase is maintained in the range of 0.10-0.17 m / s. The main amount of TB produced is displayed as a diluted water stream. The degree of conversion of isobutylene 96.2-98.5% is achieved with a volume ratio of water: hydrocarbons of 5.3 ÷ 8.1: 1 (SU 588729).

The main disadvantage of this method is the low degree of conversion of isobutylene, high water consumption and, as a result, high energy costs for the allocation of TB from dilute aqueous solutions.

A known method for producing TB by hydration of isobutylene at elevated temperature and pressure in a vertical column reactor filled with a molded acid-type ion-type catalyst, by countercurrent contact of an isobutylene-containing fraction of C ₄ hydrocarbons and water, withdrawing spent C ₄ fraction from the upper part of the reactor and from the lower part of the TB reactor in the form of an aqueous solution in which C ₄ hydrocarbons containing 5-50% aqueous solution of TB are removed from the reaction zone, followed by isolation of aqueous TB from this stream and recycling of C ₄ -ug hydrocarbons containing unreacted isobutylene to the reactor (SU 859343).

The disadvantage of this method is the use of a large 6-7-fold volume excess of water relative to the C ₄ -fraction of hydrocarbons to achieve 99.5-99.7% conversion, low productivity (up to 170 g of isobutylene per 1 liter of catalyst per hour) and, as a result, high energy costs for the allocation of alcohol from a dilute aqueous solution.

Known methods for producing TB by hydration of isobutylene at elevated temperature and pressure in a column-type reactor assembly filled with an ion-type molded acid-type catalyst, with countercurrent movement of the organic phase — isobutylene-containing C ₄ -fraction of hydrocarbons and the aqueous phase, when the organic phase is dispersed in the aqueous phase, with removal from the upper part of the reactor unit of the spent C ₄ fraction, from the lower part of the reactor unit of the aqueous solution of TB and from the reaction zone of the stream containing hydrocarbons and TB, followed by by separating hydrocarbons from a given stream and recycling them to a reactor unit, in which the process is carried out in a reactor unit containing at least two column type reactors and / or two catalyst layers and having at least one catalyst-free zone between the layers from which divert the stream containing hydrocarbons and TB, while recirculating in the reactor node flows are fed at a certain temperature (RU 2304137, RU 2304138, RU 2307823).

The main disadvantage of these methods is the complex design of the reactor unit, as well as low specific productivity.

The closest analogue of the claimed method is a method for producing TB by hydration of isobutylene at elevated temperature and pressure by contacting the hydrocarbon phase containing isobutylene with an aqueous phase containing mainly water in flow reactors (prereactor) and reaction-extraction type filled with heterogeneous acid catalysts, including the supply of water for hydration to both reactors and the initial hydrocarbon stream containing isobutylene to a flow-type reactor, output from a flow reactor and with the hydrocarbon stream, the main amount of TB obtained in the flow reactor, followed by rectification of the hydrocarbon stream into a stream containing a concentrated TB solution, and a stream containing mainly unreacted hydrocarbons, and supplying the last stream to the reaction-extraction type reactor counter-flow to the stream, containing mainly water, while the process is carried out by dispersing the hydrocarbon phase in the aqueous phase, the amount of water supplied to the flow reactor does not exceed It accounts for 25% of the total amount of water supplied for hydration, and the maximum degree of conversion of isobutylene in a flow reactor does not exceed 70% (RU 2089536).

The disadvantage of this method is the low degree of conversion of isobutylene (the residual content of isobutylene in the exhausted C ₄ fractions of hydrocarbons is more than 0.5 wt%) even when using a sufficiently large volumetric excess of water supplied for hydration with respect to the volume of hydrocarbons (1.73- 4.35 volumes of water per 1 volume of feed hydrocarbons).

The technical task of the proposed method is to increase the degree of conversion of isobutylene, as well as reducing the excess of water used and, as a result, reducing energy and material costs for the production of TB.

This problem is solved by a method for producing TB by hydration of isobutylene at elevated temperature and pressure by contacting a hydrocarbon phase containing isobutylene with an aqueous phase containing mainly water, when one phase is dispersed in another, in flow and reaction-type reactors filled with heterogeneous acid catalysts, including the supply of water for hydration to both reactors and the initial hydrocarbon stream containing isobutylene to a flow-type reactor; withdrawal from a flow-type reactor a hydrocarbon stream containing TB by dividing a given hydrocarbon stream by rectification into a stream containing a concentrated TB solution and a stream containing mainly unreacted hydrocarbons, and feeding the latter stream to a reaction-extraction type reactor countercurrent to a stream containing mainly water, in which a larger amount of the total amount of isobutylene fed to hydration is converted to TB in a flow-type reactor, and the process in this reactor is carried out with dispersion AANII aqueous phase in the continuous stream of the hydrocarbon phase and the temperature of the aqueous stream supplied to the input of the flow reactor, at 5-50 ° C at the water flow temperature to the reactive extraction reactor.

As isobutylene-containing C ₄ -fraction of hydrocarbons, fractions with different isobutylene content can be used, in particular industrial butylene-isobutylene and isobutane-isobutylene fractions containing 10-65% of the mass. isobutylene.

As acidic heterogeneous catalysts can be used sulfocationite, in particular the molded catalyst KU-2FPP according to TU 2174-022-05842324-2001, the catalyst KU-2-23FPP according to TU 2174-050-48158319-2008, macroporous sulfocationionites in the H-form of various brands and manufacturers, etc.

The following examples illustrate the method.

Example 1

Schematic diagram of a pilot installation for obtaining TB is presented in figure 1.

The flow reactor P-1 is a stainless steel pipe with an inner diameter of 50 mm, equipped with a thermostatic jacket. The reactor is loaded with 3 l of water-swollen macroporous sulfonation K-2621 from Bayer, Germany.

The original butylene-isobutylene fraction (BIF) containing 52.5% of the mass. isobutylene (stream 1), is fed into the reactor P-1 under the catalyst layer in the form of a continuous phase in the amount of 6500 ml / hour (3398.9 g / hour). The temperature of the BIF at the inlet to the reactor is maintained in the range of 70 ± 5 ° C.

In the upper part of the reactor P-1 on the catalyst layer through a special distribution device in the form of a dispersed phase serves a mixture of streams 3 and 2:

stream 3 - 900 ml / hour (843.0 g / hour) of an aqueous solution of TB with an alcohol content of 13.5% of the mass. (recycling from the bottom of reactor P-1);

flow 2 - 580 ml / hour (577.0 g / hour) of fresh water.

These streams are pre-mixed and cooled in a T-1 heat exchanger to a temperature of 50 ± 5 ° C before being fed to the catalyst bed.

The reactor coolant P-1 is supplied with a coolant from a thermostat with a temperature of 70 ± 2 ° C. An excess pressure of 1.3 MPa (13 kgf / cm ² ) is maintained in the P-1 reactor, which ensures that all components of the reaction mixture are in a liquid state.

6510 ml / hr (3975.9 g / hr) of the hydrocarbon phase (stream 4) of the composition,% by weight: isobutylene - 10.77; C ₄ inert hydrocarbons - 40.61; TB - 45.07; water - 3.55.

From the bottom of the reactor P-1 divert 1,500 ml / hour (1405.0 g / hour) of the aqueous phase (stream 3) containing 13.2% of the mass. TB, which is fully recycled to the top of the P-1 reactor on the catalyst bed.

The hydrocarbon phase taken from the upper part of the reactor P-1 (stream 4) is fed to a distillation packed column K _n -1. The nozzle loaded into this column provides separation efficiency corresponding to more than 20 theoretical plates.

From the bottom of the distillation column K _n -1, flow 6 is withdrawn in an amount of 2550 ml / hr (1933.1 g / hr at 60 ° C), which is a concentrated aqueous solution of TB containing 7.3% of the mass. water, and less than 0.1% of the mass. hydrocarbons With ₄ .

On top of the distillation column 3640 ml / hr (2042.8 g / hr) of butylene-isobutylene fraction (stream 5) containing 20.97% of the mass are taken. isobutylene and less than 0.1% of the mass. TB, which with a temperature of 40 ± 5 ° C is fully supplied under the catalyst bed to the P-2 type reaction-extraction reactor.

The P-2 reactor is a stainless steel pipe with an internal diameter of 34 mm, into which 5 l of water-swollen molded sulfocationic catalyst KU-2FPP (catalyst height 5.5 m) is loaded.

10065 ml / hr (9642.9 g / hr) of water at a temperature of 100 ± 5 ° C (sum of flows 7 and 11) is also fed into the P-2 reactor on the catalyst bed.

At the top of the P-2 reactor, a stream 8 is diverted in an amount of 3770 ml / h, containing mainly inert C ₄ hydrocarbons with impurities of isobutylene (0.1% wt.) And TB (less than 0.1% wt.).

An aqueous solution of TB (stream 9) containing 5.6% of the mass is withdrawn from the bottom of the P-2 reactor. TB and less than 0.05% of the mass. With ₄ hydrocarbons.

Stream 9 in an amount of 10,720 ml / hour (10,069.6 g / hour) is fed into a packed distillation column K _n -2, the efficiency of the nozzle in which corresponds to more than 20 theoretical plates.

880 ml / hr (661.1 g / hr) of an aqueous TB solution with an alcohol content of 85.3% of the mass is distilled off by the top of column K _n -2. (stream 10), 9820 ml / hour (9408.5 g / hour) of water (stream 11) containing less than 0.1% of the mass is withdrawn by the bottom of the column. TB, which at a temperature of 100 ± 5 ° C is fed to the catalyst bed in the P-2 reactor. An additional 245 ml / hr (234.4 g / hr) of fresh water (stream 7) is added to this stream at a temperature of 100 ± 5 ° C.

The volumetric ratio of water: source hydrocarbons With ₄ is 1.62: 1 (volumetric ratio of the sum of flows 7 and 11 to stream 1). The degree of conversion of isobutylene is 99.91%.

Example 2

A schematic flow diagram of a pilot plant for producing TB is shown in FIG. 1, but an adiabatic flow reactor (without a shirt) is used as the P-1 reactor. The reactor P-1 is loaded with 3 l of water-swollen molded sulfocationic catalyst KU-2-23FPP. The original butylene-isobutylene fraction (BIF) (stream 1) containing 52.5% of the mass. isobutylene, is fed as a continuous phase into the P-1 reactor under a catalyst bed in an amount of 5500 ml / h (3209.8 g / h). The temperature of the BIF at the inlet to the reactor is maintained at 25 ± 3 ° C.

In the upper part of the reactor P-1 on the catalyst layer through a special distribution device in the form of a dispersed phase serves a mixture of streams 3 and 2:

stream 3 - 12500 ml / hour (11715.0 g / hour) of an aqueous solution of TB with an alcohol content of 13.0% of the mass. (recycling from the bottom of reactor P-1);

flow 2 - 535 ml / h (532.9 g / h) of fresh water.

These flows before being fed to the catalyst bed are pre-mixed and cooled in a T-1 heat exchanger to a temperature of 70 ± 5 ° C.

An excess pressure of 1.4 MPa (14 kgf / cm ² ) is maintained in the P-1 reactor to maintain all components of the reaction mixture in a liquid state.

On top of the P-1 reactor, 6160 ml / hr (3,742.7 g / hr) of the hydrocarbon phase (stream 4) of the following composition was selected, wt%: isobutylene - 12.16; C ₄ inert hydrocarbons - 40.74; TB - 43.43; water - 3.67.

From the bottom of the reactor P-1 divert the aqueous phase (stream 3) containing 13.3% of the mass. TB, which is fully recycled to the top of the P-1 reactor on the catalyst bed.

The hydrocarbon phase taken from the upper part of the reactor P-1 (stream 4) is fed to a distillation packed column K _n -1. The nozzle loaded into this column provides separation efficiency corresponding to more than 20 theoretical plates.

From the bottom of the distillation column K _n -1, stream 6 is discharged in an amount of 2320 ml / hr (1763.0 g / hr at 60 ° C), which is a concentrated aqueous solution of TB containing 7.8% of the mass. water and less than 0.1% of the mass. hydrocarbons With ₄ .

3530 ml / hr (1979.7 g / hr) of the butylene-isobutylene fraction (stream 5) containing 23.0% of the mass was selected on top of the distillation column. isobutylene and less than 0.1% of the mass. TB This stream 5 is fully supplied to the reactor of the reaction-extraction type R-2 under the catalyst bed with a temperature of 40 ± 5 ° C.

The P-2 reactor is a stainless steel pipe with an internal diameter of 34 mm, into which 5 l of water-swollen molded sulfocationic catalyst KU-2FPP (layer height 5.5 m) is loaded.

In the reactor P-2, 10200 ml / hr (9844.7 g / hr) of water (the sum of flows 7 and 11) with a temperature of 90 ± 5 ° C is supplied as a continuous phase to the catalyst bed.

On top of the R-2 reactor, stream 8 is diverted in an amount of 3150 ml / h (1527.8 g / h), containing mainly inert C ₄ hydrocarbons with impurities of isobutylene (0.2% by weight) and TB (less than 0.1 % mass.).

An aqueous TB solution (stream 9) containing 5.8% of the mass is withdrawn from the bottom of the P-2 reactor. alcohol and less than 0.05% of the mass. With ₄ hydrocarbons, which in the amount of 10,880 ml / hour (10296.6 g / hour) is fed into a packed distillation column K _n -2. The efficiency of the column nozzle K _n -2 corresponds to more than 20 theoretical plates.

On top of the column, 930 ml / hour (700.1 g / hour) of an aqueous TB solution with an alcohol content of 85.3% by weight is distilled off. (stream 10), 10020 ml / h (9596.5 g / h) of water containing less than 0.1% of the mass are withdrawn by cube. TB (stream 11), which, after cooling to 90 ± 5 ° C, is fed to the catalyst bed in the P-2 reactor. An additional 257 ml / hr (248.2 g / hr) of fresh water is added to this stream at a temperature of 90 ± 5 ° C (stream 7).

The volumetric ratio of water: source hydrocarbons C ₄ is 1.95: 1. The degree of conversion of isobutylene is 99.82%.

Example 3

Schematic diagram of a pilot installation for obtaining TB is presented in figure 2.

The flow reactor P-1 is a stainless steel pipe with an inner diameter of 50 mm, equipped with a thermostatic jacket. The reactor loaded with 3 l of water-swollen macroporous sulfocationic amberlist-15.

The original isobutane-isobutylene fraction (IIF) containing 46.5% of the mass. isobutylene (stream 1), is fed as a continuous phase into the upper part of the P-1 reactor onto the catalyst bed in an amount of 7500 ml / hour (3666.6 g / hour). The temperature of the IIF at the inlet to the reactor is maintained in the range of 80 ± 5 ° C.

The following flows are dosed onto the catalyst layer through a special distribution device in the form of a dispersed phase:

stream 4 - 1100 ml / h (1023.2 g / h) of an aqueous solution of TB (13.0% by weight of alcohol) from the separator C-1 installed after the reactor P-1;

flow 2 - 545 ml / hour (542.1 g / hour) of fresh water.

These streams are pre-mixed and then heated in a T-1 heat exchanger to 80 ± 5 ° C.

The temperature in the P-1 reactor is maintained in the range of 70-80 ° C by supplying a coolant with a temperature of 70-80 ° C and an overpressure of 1.6 MPa (16 kgf / cm ² ) into the jacket of the P-1 reactor.

From the bottom of the reactor P-1, the reaction mass is sent to a separator C-1, where the separation of the aqueous and hydrocarbon phases occurs.

The aqueous phase is fully recycled to the reactor P-1 (stream 4), and the hydrocarbon phase (stream 3) is sent to a packed distillation column K _n -1 in the amount of 7260 ml / hour (4208.7 g / hour) of the following composition,% mass .: isobutylene - 10.13; isobutane - 46.61; TB - 40.15; water - 3.11.

Loaded into the column K _n -1 nozzle provides separation efficiency corresponding to 20 theoretical plates.

The cubic distillation column K _n -1 divert concentrated aqueous solution of TB (stream 6) containing 7.2% of the mass. water and less than 0.1% of the mass. hydrocarbons C ₄ in an amount of 2400 ml / hour (1820.9 g / hour at 60 ° C).

4550 ml / hr (2387.8 g / hr) of the isobutane-isobutylene fraction (stream 5) containing 17.85% of the mass was collected at the top of the distillation column K _n -1. isobutylene and less than 0.1% of the mass. TB This stream 5 in the form of a dispersed phase through a special switchgear and a temperature of 50 ± 5 ° C is fed into the reactor P-2 under the catalyst bed.

The P-2 reactor is a stainless steel pipe with an inner diameter of 34 mm, into which 5 l of water-swollen molded sulfocationic catalyst KU-2-23FPP (catalyst layer height 5.5 m) is loaded.

10090 ml / hr (9768.5 g / hr) of water (streams 7 and 11) with a temperature of 85 ± 5 ° C is fed into the P-2 reactor on the catalyst layer as a continuous phase.

4250 ml / hr (1963.6 g / hr) of isobutane containing 0.1% of the mass is discharged on top of the P-2 reactor. isobutylene and less than 0.1% of the mass. TB (stream 8).

An aqueous TB solution (stream 9) containing 5.5% by weight is withdrawn from the bottom of the P-2 reactor. alcohol and less than 0.05% of the mass. C ₄ hydrocarbons, which in an amount of 10,770 ml / hour (10,192.7 g / hour) are fed into a packed distillation column K _n -2, the packing efficiency of which corresponds to more than 20 theoretical plates.

870 ml / hr (657.1 g / hr) of an aqueous TB solution with an alcohol content of 85.3% by weight is taken from the column K _n -2. (stream 10).

9950 ml / hr (9535.5 g / hr) of water (stream 11) containing less than 0.1% of the mass is withdrawn from the cube of column K _n -2. TB, which, after cooling to 85 ± 5 ° C, is fed to the catalyst bed in the P-2 reactor. An additional 240 ml / hr (233.0 g / hr) of fresh water is added to this stream at a temperature of 85 ± 5 ° C (stream 7).

The volumetric ratio of water: starting hydrocarbons C ₄ is 1.41: 1. The degree of conversion of isobutylene is 99.89%.

Example 4

Schematic diagram of a pilot installation for obtaining TB is presented in figure 2.

The flow reactor P-1 is a stainless steel pipe with an inner diameter of 50 mm, equipped with a thermostatic jacket. 3 l of water-swollen molded sulfocationic catalyst KU-2-23FPP was loaded into the reactor.

The original isobutane-isobutylene fraction (IIF) containing 46.5% of the mass. isobutylene (stream 1), is fed as a continuous phase into the top of the P-1 reactor onto a catalyst bed in an amount of 7000 ml / h (3354.4 g / h). The temperature of the IIF at the inlet to the reactor is maintained in the range of 85 ± 5 ° C.

The following flows are dosed onto the catalyst layer through a special distribution device in the form of a dispersed phase:

stream 4 - 500 ml / h (468.6 g / h) of an aqueous solution of TB (13.0% by weight of alcohol) from a separator C-1 installed after the reactor P-1;

stream 2 - 471 ml / hour (470.6 g / hour) of fresh water.

These flows are pre-mixed and then heated in a T-1 heat exchanger to 85 ± 5 ° C.

The temperature in the P-1 reactor is maintained in the range of 70-85 ° C by supplying a coolant with a temperature of 70-80 ° C and an overpressure of 1.6 MPa (16 kgf / cm ² ) into the jacket of the P-1 reactor.

From the bottom of the reactor P-1, the reaction mass is sent to a separator C-1, where the separation of the aqueous and hydrocarbon phases occurs.

The aqueous phase is fully recycled to the reactor P-1 (stream 4), and the hydrocarbon phase (stream 3) is sent to a packed distillation column K _n -1 in the amount of 6630 ml / hour (3825.0 g / hour) of the following composition,% mass .: isobutylene - 11.01; isobutane - 46.92; TB - 39.34; water - 2.73.

Loaded into the column K _n -1 nozzle provides separation efficiency corresponding to more than 20 theoretical plates.

Concentrated column TB solution (stream 6) containing 6.5% of the mass is withdrawn by the bottom of the distillation column K _n -1. water and less than 0.1% of the mass. hydrocarbons C ₄ , in an amount of 2120 ml / hour (1609.3 g / hour at 60 ° C).

On top of the distillation column To _n -1 take 4110 ml / hour (2215.7 g / hour) isobutane-isobutylene fraction (stream 5) containing 19.0% of the mass. isobutylene and less than 0.1% of the mass. TB This stream 5 in the form of a dispersed phase through a special switchgear and a temperature of 40 ± 5 ° C is fed into the reactor P-2 under the catalyst bed.

The P-2 reactor is a stainless steel pipe with an internal diameter of 34 mm, into which 5 l of water-swollen molded sulfocationic catalyst KU-2FPP (catalyst height 5.5 m) is loaded.

9890 ml / hr (9475.3 g / hr) of water (streams 7 and 11) with a temperature of 100 ± 5 ° C is supplied to the P-2 reactor on the catalyst layer as a continuous phase.

At the top of the P-2 reactor, 4200 ml / hr (1796.4 g / hr) of isobutane containing 0.1% of the mass is discharged. isobutylene and less than 0.1% of the mass. TB (stream 8).

From the bottom of the reactor divert the aqueous solution of TB (stream 9) containing 5.6% of the mass. alcohol and less than 0.05% of the mass. C ₄ hydrocarbons, which in the amount of 10540 ml / hour (9894.6 g / hour) are fed into a packed distillation column K _n -2, the efficiency of the nozzle in which corresponds to more than 20 theoretical plates.

860 ml / hr (649.6 g / hr) of an aqueous TB solution with an alcohol content of 85.3% by weight is taken from the column K _n -2. (stream 10).

9650 ml / hour (9245.0 g / hour) of water (stream 11) containing less than 0.1% of the mass is withdrawn from the cube of column K _n -2. TB, which at a temperature of 100 ± 5 ° C is fed to the catalyst bed in the P-2 reactor. An additional 240 ml / hr (230.3 g / hr) of fresh water (stream 7) with a temperature of 100 ± 5 ° C is added to this stream.

The volumetric ratio of water: starting hydrocarbons C ₄ is 1.48: 1. The degree of conversion of isobutylene is 99.88%.

Thus, the process by the proposed method allows to increase the degree of conversion of isobutylene from 99.5 to 99.82-99.91 using a smaller volume excess of water (1.4-1.9) relative to the hydrocarbons fed to hydration, while maintaining high productivity (195 -224 kg of isobutylene / m ³ catalyst · hour) and thereby reduce energy and material costs.

Claims (1)

A method of producing tertiary butanol by hydration of isobutylene at elevated temperature and pressure by contacting a hydrocarbon phase containing isobutylene with an aqueous phase containing mainly water, when one phase is dispersed in another, in flow and reaction-type extraction reactors filled with heterogeneous acid catalysts including the supply of water for hydration to both reactors and the initial hydrocarbon stream containing isobutylene to a flow-type reactor, withdrawal from a flow-type reactor of a stream hydrocarbons containing tertiary butanol, by separating this hydrocarbon stream by distillation into a stream containing a concentrated solution of tertiary butanol, and a stream containing mainly unreacted hydrocarbons, and supplying the latter stream to a reaction-extraction type reactor countercurrent to a stream containing mainly water, characterized in that a greater amount of the total amount of isobutylene fed to hydration is converted to tertiary butanol in a flow-type reactor, and p The process in this reactor is carried out when the aqueous phase is dispersed in a continuous stream of the hydrocarbon phase and the temperature of the water stream supplied to the inlet of the flow reactor is 5-50 ° C lower than the temperature of the water stream supplied to the reaction-extraction reactor.

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