Method of distillation

FIELD: food products; alcoholic beverages.

SUBSTANCE: according to the method, initial flow is supplied to the first distillation steam-stripping column while its distillate is passed to the second distillation rectifying column. Initial flow is refined using first membrane separation method. Obtained concentrate is passed to the first distillation column and derived permeate is supplied to the second distillation column. Distillate from the second distillation column is refined using second membrane separation method.

EFFECT: increasing pureness of obtained ethanol.

16 cl, 2 dwg, 2 tbl

 

The invention relates to a method of distillation, especially distillation of ethanol from the mash.

Distillation and dehydration of the ethanol from the beer mash, which after fermentation contains about 10% ethanol, 85% water and 5% solids, in the usual way congestion in a heated state fed to the first distillation column. In the first distillation column congestion evaporated, receiving CBM product contained in the mash solids that can be removed from the column with water. Usually part of this cubic product after heating again returned to distillation column (boiler).

First vaporous distillate, which still contains water, ethanol and fusel oil, served, not necessarily through the collector-mixer, the second distillation column, made in the form of a distillation column. In this distillation column is further division, which fusel oil discharged in the form of a side stream. A small portion formed in the second distillation columns in the form of the cubic product water after heating again returned to distillation column (boiler), and the rest are also removed, fully bringing it from the process. Obtained in the second distillation column distillate, which still contains water and ethanol, can again partially, not necessarily through already cited UTY above collection, to return to the first and second distillation columns.

The overwhelming amount of forming the second distillate water-ethanol mixture containing 95% ethanol and 5% water, is subjected to last for dehydration of ethanol with the highest possible degree of purity of the order 99-99,8%. In this last phase dehydration using molecular sieves, in which the crystalline zeolite type sponge adsorb molecules of H2O.

However, zeolites molecular sieves quickly saturated with water. For continuous dehydration of water-saturated zeolites must be regenerated. For this reason, molecular sieves are usually used in pairs. In this case, from the first, active molecular sieve is possible to obtain high-purity ethanol, which can also be used for regeneration of the second, inactive molecular sieves. When regenerating inactive molecular sieves used for this purpose, the ethanol can be returned into the distillation column of the reverse flow, which may account for about 30% of pure ethanol, obtained on the active molecular sieve. This constant change of the current at the molecular sieves load, due to their periodic loading pressure and removing the current pressure on them, leads to abrasion of such filler to the m are molecular sieves, and the formation of dust. Such pulverulent products abrasion molecular sieves contaminate the subsequent stages of the installation, which for this reason have to periodically replace. This increases capital costs and operating costs.

Dehydration of ethanol is an energy-intensive process. Thus, in particular, evaporation of congestion in the first distillation column, as well as the need to return to her large quantities of distillate, associated with significant operating costs and capital costs. In addition, and water-ethanol mixture before processing molecular sieves must have a high degree of purity, in which the concentration of ethanol should be about 90-95%, for which the mixture of substances must undergo extremely difficult from the viewpoint of equipment design and exceptional expensive from the point of view of operating costs of rectification as close to the azeotropic point. For this reason, in a distillation column is required to provide many degrees of separation and return to it a large number of phlegmy.

Based on the above-described prior art, the present invention was used to develop the method of distillation, which would significantly increase the efficiency of the process especially when de is gratzii ethanol from mash.

In regard to the method of distillation, especially ethanol from the mash, in the exercise of which the source stream is fed to the first distillation column, also frequently referred to as a Stripping column, and select from it the distillate served in the second distillation column, also frequently referred to as a distillation column, the above task is solved by the fact that the original thread is subjected to cleaning the first membrane separation method of obtaining a concentrate, which is fed to the first distillation column, and a permeate, which is fed to the second distillation column, and/or distillate taken from the second distillation column, purified second membrane separation method.

Membrane separation processes, a great variety of which are known in the prior art have proven themselves in practice. The advantage of the majority of membrane separation processes is that in the process of separating the processed product undergoes no phase transformations and therefore does not highlight or no absorption amounts of stored energy. In addition, the membrane is inert to the components of the partial mixture of substances, eliminating the possibility of additional contamination of the product with impurities, the source of which are excipients, ispolzuemyi separation. Thereby eliminated and the need for further purification of the product from such contaminating its auxiliary substances used in the process of separation. Such separation devices do not require their regeneration.

As membrane separation methods, it is preferable to use a so-called membrane technology, and from them, primarily for processing the original thread, mainly beer mash upon receipt of ethanol, filtered through the membrane. As a result of such filtering through a membrane, for example, congestion in the quality of the permeate receive only liquid mixture of ethanol, water and fusel oils. The remaining concentrate with a high content of mash pulp serves in the usual way, preferably after preheating in the first distillation column.

As indicated above, the permeate obtained by membrane separation process the original thread, serves to bypass the first distillation column directly to the second distillation column. Upon receipt of ethanol, in particular from the beer mash, the permeate obtained by membrane separation process has basically the same structure as that of the distillate obtained in the first distillation column. Therefore, the permeate is no need to send to the processing in the first distillation column, and can be directly submitted in in which which distillation column. Thanks to this already provides significant energy savings, as supplied directly to the second distillation column permeate is no longer required, unlike traditional methods, to completely evaporate in the first distillation column. Said especially true in the case when the mass ratio of concentrate to permeate resulting from the first membrane separation process, the original thread is from 1 to 8.

In the preferred embodiment, it is possible to use dynamic filtering through a membrane with a cross-flow movement. This filtering technology is based on the use of disk membranes mounted on hollow shafts, while the disk membrane, mounted on different shafts, mutually overlap. The flow of the partial product runs onto the disk membrane on the outside and permeate, penetrate through the disk membrane inside her, is discharged through the hollow shaft. Bringing the disk membranes in rotation at high speed relative to the partial product, as well as the occurrence of significant turbulence in areas of mutual overlap of disk membranes significantly reduce the possibility of contamination of the membranes or driving. As a result of increased specific productivity of the permeate and reduced energy consumption per unit amount of permeate. SIP the mo of this cleaning cycles membranes if this lasts much longer than other membrane technologies, resulting in higher availability and lower operating costs. Technology dynamic filtration through a membrane with cross-traffic flow is known, for example, from international publication WO 98/23724.

From a technological point of view it is preferable to further apply the permeate resulting from the first membrane separation process the original thread, in the form of a mixture with the first distillate, i.e. the distillate taken from the first distillation column into a second distillation column. In this case, is provided by the uniform regulation of the amount fed to the second distillation column material and smoothing fluctuations in performance of the first distillation column and membrane separation process. In another embodiment, the permeate resulting from the first membrane separation process of the source stream and the distillate taken from the first distillation column can be fed to the second distillation column separately from each other.

Depending on the particular variant proposed in the invention method supplied in the form of mixtures with each other or separately from each other in the second distillation column permeate and/or distillate taken from the first distillation column support in liquid status and in a relatively hot condition, for example, a temperature of 120C, but preferably practically in the form of a liquid phase in contrast to the prior art, according to which these materials serves the second distillation column in vapor form at a temperature close to the dew point. In other words, the permeate and/or distillate, individually or in a mixture of support in a liquid state at a temperature close to the boiling point.

From the second distillation column, the water is taken from her cube in the liquid phase. Therefore, another advantage of the proposed invention the method also lies in the fact that the water component of the permeate resulting from the first membrane separation process, the original thread remains or is present in the second distillation column in a liquid phase. For this reason, in the second distillation column from received it the mixture should evaporate only the ethanol component. Unlike traditional methods proposed in the invention method allows you to save the energy that would be spent on evaporation of the water component, since water is supplied to the second distillation column as a liquid phase, and not in a vaporous form and remains in this column in the liquid phase.

Depending on the selected membrane method of separation supplied to the first distillation column number of liquids and is reduced in comparison with the known from the prior art method by 15-50%. Accordingly, on evaporation filed in the first distillation column the amount of fluid required and less energy.

Thanks to the above measures in the first distillation column is fed product with already high concentration in the mash slurry containing solids. Despite receipt of the first distillation column a smaller amount of fluid that is supplied to it in the original thread, the concentration of the cubic product, as well as the composition of the distillate conform to the normal ways, however, the concentration in the distillation column above.

The content of ethanol in the distillate taken from the second distillation column is from 75 to 95 wt.%. The advantage of the invention method is that even at relatively high water content in the distillate in comparison with conventional methods, the implementation of which the content of ethanol in the distillate before the final stage of dehydration should be about 90-95 wt.%, for the final dehydration can use another membrane separation process, primarily well as membrane technology, and in this case, preferably the evaporation through the membrane. This makes it possible to reduce the manufacturing cost of the second distillation column and the cost of its operation.

For Windows athelney dehydration it is expedient to provide the group parallel to the membrane apparatus, which serves, preferably through the superheater, the distillate taken from the second distillation column (rectifying column), and the exhaust from which the quality of the end product concentrate, in this case primarily ethanol, has a high degree of purity greater than 99%, and component mainly from 99 to 99.95%.

The efficiency of separation in the membrane apparatus can be increased, again giving a small part of which is the end product of the concentrate obtained in the membrane apparatus, in each of them as a flushing stream on the permeate side and again returning this concentrate after passing through the corresponding membrane apparatus together with the data points from the permeate to the second distillation column as a second feed stream.

The wash stream is selected from the obtained in membrane devices concentrate continuously returned to the membrane apparatus and lowers them on the permeate side partial pressure of water, which allows economical way to additionally increase the degree of purity of the concentrate to the value reaching at 99.95%.

To implement such a process of cleaning the membranes by washing, it is preferable to use a so-called internal flushing flow in the form of a partial flow of the concentrate or external flushing flow, for example p is a stream of nitrogen. A common feature of both these methods is physical (convective) the withdrawal or removal of permeate additional stream.

Since in the preferred embodiment, the diaphragm apparatus of the evaporation through the membrane, and which is the end product concentrate is in the gas phase, the wash stream without any problems also serve membrane apparatus in gaseous form. This is also due to the fact that the throttle creates a vacuum in the permeate and therefore significantly increases the volume flow of the leaching flux, thereby increasing the efficiency of convective entrainment permeate moving in a counter to it proryvnym stream.

The permeate obtained in the membrane apparatus, before filing the second distillation column, it is advisable to preheat the heat generated in it and taken from it the cubic product.

Similarly the heat of the final product and/or the cubic product formed in the second distillation column and select from it can be used to heat the concentrate from the first membrane separation process the original thread, which usually uses traditional heat exchangers.

For heat dissipation, summed up in the first distillation column to vaporize the liquid and the article is vsego after this redundant, in the supply line leading to the second distillation column, preferably directly in front of the entrance, it is advisable to install the heat exchanger, the first capacitor.

In the particular case of the proposed in the invention method, the second distillation column may be formed by two separated from one another distillation columns.

Below proposed in the invention method is described in more detail with reference to the accompanying drawings, which represent only the technological scheme and which, in particular, it is shown:

figure 1 is a diagram illustrating the first process,

figure 2 - diagram illustrating the second process.

In addition, in the accompanying drawings tables 1 and 2 only as an example presents the corresponding positions 1-10 and 31-40 specific values of common physical quantities, both technological process, which is illustrated in figures 1 and 2, differ basically only different by using eye-catching during the heat.

1 schematically shows an installation for the distillation, respectively dehydration of ethanol from the beer mash, employee source stream 1 submitted for processing.

The mash contains about 10 wt.% ethanol, 85% water and 5 wt.% solids and has temperature is round, for example, 20C. In step 11 membrane separation congestion divided into concentrate 2 containing mash mush in high concentrations and solids, and the permeate is 3, representing only the liquid phase consisting of a mixture of water, ethanol and fusel oils. Concentrate 2 with a high content of mash slurry and solids are heated in the heat exchanger 12, for example, at 10C to a temperature of 30C and fed to the first distillation column 13 or Stripping column.

Liquid permeate 3, taken from the stage 11 membrane separation original thread 1, is fed directly to the second distillation column 14, which represents a distillation column.

The presence of elevated concentrations of mash pulp in the concentrate 2 fed to the first distillation column 13, can effectively carry out the process in the first distillation column 13 and eliminates the need for complete evaporation of the permeate. Moreover, in this column from mash the pulp is separated ethanol-water mixture with a high content of ethanol, which in the end is only required to evaporate from it, while accumulating in the cube, water and solids removed from the process in the form of the cubic product 5 (Barda).

Part of the cubic product 5 after the heat exchanger 15 can in the usual way again serve peruyperuanos column 13.

The 4 distillate obtained in the first distillation column 13 and containing, for example, 30% ethanol, assign another one heat exchanger 16 and then mixed with the permeate 3. The resulting mixture serves 6, preferably at a constant volumetric rate, the second distillation column 14. The content of ethanol in the mixture 6 is, for example, 20 wt.%, as the water content is 80 wt.% at a temperature of 120C (see data tables). The mixture preferably 6 must remain in the liquid phase at a temperature close to the temperature of its boiling point.

The distillate 7, taken from the second distillation column 14 at a temperature of, for example, 125C still contains 85 wt.% ethanol and 15 wt.% water. The distillate 7, taken from the second distillation column 14, when the content of ethanol is about 80 wt.% unlike conventional methods, the implementation of which its content in the distillate should be 90-95 wt.%, it is possible according to the proposed invention method to expose the final dehydration of the membrane separation method.

To this end, the distillate 7, taken from the second distillation column 14, serves in group 17 of the few, and in this example of three parallel membrane devices 18, 19, 20. Concentrate 9 obtained by filtration through a membrane filter, primarily evaporation through the membrane, isone of the final product, namely, high-purity ethanol containing only 0.2 wt.% or less up to 0.05 wt.% water. The final product is finally taken after cooling in the heat exchanger 12, through which it is passed to heating them fed into the first distillation column 13 concentrate 2.

The process in membrane devices 18-20 can be carried out in mode with the cleaning of the membranes, for which some amount of concentrate 9, representing the final product, again return in each of the membrane filter apparatus 18-20, passed through them as the flushing stream, after which, together with the obtained them in the permeate in the form of a mixture 10 containing, for example, to 57.2 wt.% ethanol and 42.8 wt.% water, condensed in the heat exchanger 21 under vacuum and serves not shown in the drawing the pump, not necessarily through the collection, back to the second distillation column 14 for enrichment. In the heat exchanger 21 in this case we use the waste heat water, which is the only kubovy product 8, which is formed in the second distillation column 14, and which leaves the heat exchanger cooled, for example, to 30C.

In the process carried out is shown in figure 2 installing, distillation, respectively, subjected to dehydration of the ethanol from the beer mash, which is the source stream 31, which serves for processing the composition of which corresponds to the composition of the original beer mash in the above first example embodiment of the invention.

In step 41 membrane separation congestion and in this embodiment is divided into concentrate 32 and permeate 33. Concentrate 32 is passed through two heat exchanger 42, 43 and/or the head condenser of the first distillation column 44 by heating to approximately 115C., and fed to the first distillation column 44.

Part condensed in the first distillation column 44 of the beer mash, taken from her as the cubic product 35, return through the heat exchanger 45 back to the first distillation column 44, which thus can operate in the optimal way (boiler). Excess VAT product 35 is removed from the process.

Permeate 33, and the distillate 34, taken from the first distillation column 44, served together in the form of their mixture 36 to the second distillation column 46.

Part taken from the cube of the second distillation column 46 of purified water after evaporation in the heat exchanger 53 again return directly to the second distillation column 46 (boiler), and excess water 38, taken from the second distillation column 46, delete, previously passing through the heat exchanger 42. Another partial stream 55 of purified water is evaporated in the heat exchanger 52 and then use as an auxiliary material in the second distillation column 46. The heat exchanger 52 is used for this boiler, in which the partial evaporation of sweat is ka 55 purified water. This distillate 34, taken from the first distillation column 44, condensed.

A mixture of 36, which consists of distillate 34, taken from the first distillation column 44, and permeate 33 obtained in step 41 membrane separation original thread 31, and which is heated to a high temperature, lying near the boiling point, but still remains in the liquid phase, served in the second distillation column 46 through located directly in front of the entrance 56 it the heat exchanger 54, the first capacitor. Via a heat exchanger 54 excess heat emitted from the evaporation of the liquid in the first distillation column 44, it is possible to withdraw from the process and use them in the future for various purposes.

Part of the distillate taken from the second distillation column 46, in the form of a partial stream 57 again return to it (phlegm), while the main thread 37 of the distillate is passed through a superheater 51 in group 47 of membrane units 48-50.

The process in membrane devices 48 and 50 in this embodiment can be carried out in mode with the cleaning of the membranes, for which a portion of the concentrate stream 39, which is the end product, return back to each of the membrane filter apparatus 48-50, passed through them similar to the above example and return in the form of a mixture with 40 received in the membrane apparatus 48-50 VT is the atom in the second distillation column 46.

Table 1
12345678910
Volumetric flow rate, kg/h12,0008,9553,0452,9556,0006,0001,8424,7981,202640
Ethanol, wt.%109,810,53002085099,857,2
Water, wt.%85to 83.5to 89.5709080 151000,242,8
Congestion, wt.%56,7001000000
Absolute pressure, bar1,0132,52,52,52,52,52,51,0131,0130,1
Temperature, C2030301201201201253025120

Table 2
3132 3334353637383940
Volumetric flow rate, kg/h12,0008,9553,0452,9556,0006,0001,8424,7981,202640
Ethanol, wt.%109,810,53002085099,857,2
Water, wt.%85to 83.5to 89.5709080151000,242,8
Congestion, wt.%5001000000
Absolute pressure, bar1,0133331,013331,0131,0130,1
Temperature, C2011530120301201255030120

1. The method of distillation primarily of ethanol from the mash, in the exercise of which the source stream is fed to the first distillation column (Stripping column), and taken from her distillate served in the second distillation column (rectifying column), characterized in that original thread (1) is subjected to cleaning the first membrane separation method to obtain concentrate (2), served in the lane the second distillation column (13), and permeate (3), which is fed to the second distillation column (14), and/or distillate (7), taken from the second distillation column (14), purified second membrane separation method.

2. The method according to claim 1, characterized in that the membrane separation methods using membrane technology.

3. The method according to claim 2, characterized in that the membrane technology is a dynamic filtration through a membrane with cross-traffic flow.

4. The method according to claim 1, characterized in that the permeate (3)resulting from the first membrane separation process, the original thread (1)is fed to the second distillation column (14) in the form of a mixture (6) distillate (4), taken from the first distillation column (13).

5. The method according to claim 1, characterized in that the permeate (3)resulting from the first membrane separation process of the source stream and the distillate taken from the first distillation column, served in the second distillation column separately from each other.

6. The method according to claim 4 or 5, characterized in that supplied in the form of mixtures with each other or separately from each other in the second distillation column permeate and/or distillate taken from the first distillation column support in a liquid state at a temperature close to the boiling point.

7. The method according to claim 1, characterized in that the mass ratio of Koh is entrata (3) to the permeate (2), from the first membrane separation process, the original thread (1)is from 1 to 8.

8. The method according to claim 1, characterized in that the water component of the permeate (3). the resulting membrane separation process, the original thread (1)is or is present in the second distillation column (14) in the liquid phase.

9. The method according to claim 1, characterized in that the content of ethanol component in the distillate (7), taken from the second distillation column (14)is from 75 to 95 wt.%.

10. The method according to claim 1, characterized in that the distillate (7), taken from the second distillation column (14), served in a group (17) parallel to the membrane apparatus (18-20).

11. The method according to claim 1, characterized in that the distillate (7), taken from the second distillation column (46), served in the membrane apparatus (48-50) through the superheater (51).

12. The method according to claim 10, characterized in that the part which is the end product concentrate (9)obtained in membrane devices (18-20), again served in each of them as a flushing stream on the permeate side and after passing through the corresponding membrane apparatus again return together with the data points from the permeate to the second distillation column (14) as a feed stream (10).

13. The method according to claim 10, characterized in that the permeate (10)obtained in membrane devices (18-20), Bodog ewout warmth of the cubic product (8), formed in the second distillation column (14) and taken from her.

14. The method according to item 12, characterized in that the heat of the final product (9) and/or the cubic product (38)formed in the second distillation column (46), is used to heat the concentrate (2, 32), from the first membrane separation process, the original thread (respectively 1,31).

15. The method according to claim 1, characterized in that the supply line (56), leading to the second distillation column (46), a heat exchanger.

16. The method according to claim 1, characterized in that the second distillation column is formed by two separated from one another distillation columns.

17. The method according to item 15, wherein the distillate taken from the second distillation column (46)is fed through the superheater (51) group (47) membrane devices.



 

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6 cl, 1 dwg, 1 tbl

FIELD: alcohol production.

SUBSTANCE: method comprises direct distillation of concentrate of top ethyl alcohol impurities or rectification of intermediate ethyl alcohol fraction in presence of an alkali agent selected from sodium and potassium oxide, carbonate, and bicarbonate hydrates, and aqueous ammonia in case of top ethyl alcohol impurities processing and selected from sodium and potassium oxide, carbonate, and bicarbonate hydrates, calcium oxide, and aqueous ammonia in case of intermediate ethyl alcohol fraction rectification at alkali agent concentration 0.01 to 3.0 wt % and vat temperature 80-86°C. Desired processing product is commonly used as a binary mixture component and vat residue obtained in distillation and rectification operation is commonly used as additional component of fuel oil.

EFFECT: achieved wasteless processing of alcohol production wastes and utilization of all processing products.

6 cl

FIELD: method for production of alcohol-containing solvents based on waste from ethanol production from food-grade raw materials.

SUBSTANCE: claimed method includes reprocessing of etheraldehyde fraction of concentrate containing ethanol main admixtures from starch- and/or sugar-containing raw materials. Process is carried out in rectifier at vapor phase temperature in still of 60-90°C. Nitrosolvent is obtained by mixture sampling at 60-70°C. Degreasing solvent is obtained by mixture sampling at starting temperature in column top of 73°C or more when ethers are detected in distillate. Claimed nitrosolvent (degreasing solvent) contain (mass %): acetate-type ethers 10-30 (0.8-2.9); aliphatic alcohols 51-74 (87-89); acetaldehyde 5-9 (0.2-1.5), and water 8-10 (8-10).

EFFECT: simplified and economy method for reprocessing of waste from ethanol production; enhanced assortment of alcohol-containing solvents.

3 cl, 1 dwg, 3 ex, 3 tbl

FIELD: distillery industry; production of a dehydrated ethyl alcohol.

SUBSTANCE: the invention is pertaining to the field of distillery industry, in particular, to the methods of production of a dehydrated ethyl alcohol. The method provides for concentration of the water-alcohol solution purified from impurities by a rectification, its dehydration by adsorption through the molecular sieves and its regeneration by a desorption. Concentration of the water-alcohol solution and its dehydration by adsorption are conducted at the pressure of 105-350 kPa. A part of the formed during the concentration vapors is once more heated up to the temperature of 96-150°C and feed to the stage of desorption, which is realized at the pressure of 5-60 kPa. The rest part of the vapor from the stage of adsorption and a desorption is subjected to condensation and the water-alcohol liquid is fed to the stage of the alcohol concentration with withdrawal of the water from the process. The invention allows to intensify the process of dehydration and to reduce consumption of the heat-power input.

EFFECT: the invention allows to intensify the process of dehydration and to reduce the heat and power inputs.

1 tbl

The invention relates to a method of continuous hydration of ethylene, propylene or mixtures thereof with water in the vapor phase to the corresponding alcohols in the presence of salts heteroalicyclic as a catalyst at a molar ratio of water to olefin passing through the reactor, in the range of 0.1 to 3.0, an average hourly rate of gas supply water/olefin through the catalytic system 0,010 - 0.25 g/min/cm3concentrations of heteroalicyclic 5 to 60 wt.% from the total mass of the catalytic system, at a temperature of 150 - 350oC and a pressure ranging from 1000 to 25000 kPa

The invention relates to a method of dehydration of aliphatic alcohols C1-C3
The invention relates to the alcohol industry, in particular to a method of purification of ethanol from impurities

The invention relates to an improved process for the preparation and purification of synthetic ethanol produced by the direct hydration of ethylene
The invention relates to methods of producing ethanol and acetic acid or mixtures thereof, which can be used in many sectors of the economy

FIELD: distillery industry; production of a dehydrated ethyl alcohol.

SUBSTANCE: the invention is pertaining to the field of distillery industry, in particular, to the methods of production of a dehydrated ethyl alcohol. The method provides for concentration of the water-alcohol solution purified from impurities by a rectification, its dehydration by adsorption through the molecular sieves and its regeneration by a desorption. Concentration of the water-alcohol solution and its dehydration by adsorption are conducted at the pressure of 105-350 kPa. A part of the formed during the concentration vapors is once more heated up to the temperature of 96-150°C and feed to the stage of desorption, which is realized at the pressure of 5-60 kPa. The rest part of the vapor from the stage of adsorption and a desorption is subjected to condensation and the water-alcohol liquid is fed to the stage of the alcohol concentration with withdrawal of the water from the process. The invention allows to intensify the process of dehydration and to reduce consumption of the heat-power input.

EFFECT: the invention allows to intensify the process of dehydration and to reduce the heat and power inputs.

1 tbl

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