RU65779U1 - SYSTEM OF SUPPLY OF HEAT FLOWS WHEN RECEIVING A RECTIFIED ALCOHOL IN A BRAKE RECTIFICATION INSTALLATION (OPTIONS) - Google Patents

Abstract

The utility model relates to the alcohol industry, in particular, to plants for the production of rectified food alcohol and allows to increase the efficiency of the process of rectification by reducing energy costs. The heat flow supply system upon receipt of rectified alcohol in the distillation unit includes a source of hot steam, steam pipelines communicating with each other through heat exchangers-boilers (1), distillation (3), epure (5), fuselage (8) (option 1), methanol (10), ether (12) columns and a condensate collector (13) (option 2), while the source of hot steam, respectively, is connected via distillation (3) and (9) with distillation (3) and fusel (8) columns. The distillation column (3), respectively, through heat exchangers-boilers (2) and (6) is communicated with the brew (1) and epuration (5) columns. The fuselage column (8), respectively, through the heat exchanger-boiler (7) is in communication with the epilation column (5) (option 1). The recovery column (5) is in communication with the methanol column (10) through the heat exchanger-boiler (11), while the distillation (3) and fuselage (8) columns, respectively, are connected with the condensate collector through the heat exchangers-boilers (4) and (9) (13), which is in communication with the ether column (12) (option 2). The mash (1), methanol (10) and ether (12) columns are connected to the vacuum pump through the corresponding heat exchangers, while the epurenation (5) columns are connected to the vacuum pump or to the atmosphere through the corresponding heat exchangers. 2 n.p. f-ly, 2 z.p. f-ly, 2 ill.

Description

The utility model relates to the alcohol industry, in particular to installations for the production of rectified edible alcohol.

A known rectification unit (BRU) is used to implement a method for producing rectified alcohol, in which ethanol is digested from the mash in a mash-digestion column with the passage of ethyl alcohol and associated impurities to the distillate with steam from this column and liquid fractions from the condenser of the carbon dioxide and alcohol separator , the separation of impurities from the distillate in the distillation column with the supply of hot water to the middle zone of its concentration part and the selection of the side fraction from hydroselection, which, together with fractions of fusel oil and fusel alcohol from an alcohol column, is rectified in a fusel column (V.L. Yarovenko, B.A. Ustinnikov, B.P. Bogdanov, S.I. Gromov. Guide to the production of alcohol. Raw materials , technology and technochemical control. M.: Light and food industry, 1981, - p.138).

Closest to the proposed utility model is a heat supply system for producing rectified alcohol in a distillation unit, implemented in a method for producing rectified alcohol (RF Patent No. 2172202 B01D 3/14 publ. 2001.08.20.) By digesting alcohol from the mash in a brew column with the transfer of ethyl alcohol and related impurities to the mash distillate, purification of the mash distillate from head and intermediate impurities, including fusel oil components, in an epilation column using hydroselection and distillation of the epureate in an alcohol column with the selection of fractions of fusel oil, fusel alcohol and unpasteurized alcohol, distillation of the head and intermediate fractions

impurities. The process of rectification is carried out under reduced pressure in the epuration, alcohol (distillation), methanol and first booster columns (ether) and high pressure in the brew, boiled (epure) and second booster (fuselage) columns. The distribution of heat fluxes is carried out as follows: with hot steam, the brew, boiled (epure) and second booster columns (fuselage) are heated, the steam leaving the brew column is used to heat the distillation and methanol columns, the steam from the second booster column (fuser) is heated with the first accelerator column ( ethereal), and the steam from the boiled-out (epuration) column heats the alcohol (distillation) column and finally heats the original mash, which is preheated with steam from the alcohol (distillation) column and luther from the boiled-off (epuration) column, fraction from the capacitors of the carbon dioxide separator, the brew and epuretion columns, alcohol traps of dirty epaulettes together with fusel alcohol are sent to the nutrient plate of the first acceleration (ether) column, from which the head fraction concentrate is removed and the liquid from the cube together with the fusel oil fraction from the alcohol (distillation) column and the wash water from the sivuhopryvatel are sent to the second power plate (fusel) columns, fractions from methanol and alcohol (distillation) column condensers are fed to the upper nutrient plate of this column, the head fraction concentrate is removed from the condenser of the second booster (fusel) column, fusel oil is removed from the vapor phase of its 5-11th lower plates , the propyl alcohol concentrate is removed from the liquid phase of the lower plates of the strengthening part of the second booster (fusel) column, and the ethyl alcohol fraction is taken from its middle zone and returned to the mash.

However, this method leads to an increased neoplasm of esters and aldehydes in the mash column, a lower specific total heat consumption for the epuration and methanol columns, which limits the possibility of improving the quality of alcohol. In addition, this method requires increased energy consumption for fracking.

The technical result, the achievement of which is proposed by the proposed utility model, is to increase the efficiency of the process of rectification, by reducing energy consumption.

The technical result is achieved by the fact that in the heat flow supply system upon receipt of rectified alcohol in a distillation rectifier (option 1), which includes a source of hot steam and steam pipelines, communicating with each other, respectively, through heat exchangers, boilers, distillation, distillation, epuration and fusel towers, this source of sharp steam communicated with fusel column, new is that the source of sharp steam, in addition, is connected with a distillation column, which is in communication with mash column, communicates connected through heat exchangers with a vacuum pump, the fusel column is in communication with a scrub column, which is connected through heat exchangers with a vacuum pump or atmosphere.

In the heat flow supply system upon receipt of rectified alcohol in a distillation rectifier (option 2), which includes a source of hot steam and steam pipelines communicating with each other through heat exchangers-boilers, mash, distillation, epure, fuselage, methanol and ether columns, while the source of hot steam is communicated with a fusel column, and the methanol and ether columns are in communication with a vacuum pump, it is new that the source of sharp steam, in addition, is connected with a distillation column, which is connected with by the mash column communicated through heat exchangers with a vacuum pump, the fuselage column is in communication with the epilation

the column, which is in communication with the methanol column, while the distillation and fusel columns are in communication with the condensate collector, which is in communication with the ether column, in addition, the epilation column is connected through the heat exchangers to the atmosphere or to a vacuum pump.

In the heat flux supply system according to option 1 and 2, the distillation column is in communication with the epilation column for its additional heating.

The essence of the utility model is presented in figures 1 and 2.

Figure 1 - diagram of the supply of heat flux according to option 1.

Figure 2 - diagram of the supply of heat flux according to option 2.

Here: 1 - beer column; 2 - boiler-heat exchanger of the tow column; 3 - distillation column; 4 - boiler-heat exchanger distillation column; 5 - epilation column; 6 and 7 - boilers-heat exchangers of the epilation column; 8 - fusel column; 9 - boiler-heat exchanger fuselage columns; 10 - methanol column; 11 - a boiler-heat exchanger of a methanol column; 12 - ether column; 13 - condensate collector.

The rectification plant (BRU) includes a source of hot steam, a brewing column 1 with a boiler-heat exchanger 2, a distillation 3 with a boiler-heat exchanger 4, a distillation 5 with boiler-heat exchangers 6 and 7, a fuselage 8 with a boiler-heat exchanger 9, a methanol 10 with a boiler- heat exchanger 11 and ether 12 columns, condensate collector 13. The source of hot steam, respectively, through heat exchangers-boilers 4 and 9 by steam lines is connected with distillation 3 and fuselage 8 columns. The distillation column 3, respectively, through the heat exchangers-boilers 2 and 6 by steam pipelines is connected to the brew 1 and the recovery 5 columns and through the heat exchanger-boiler 4 with a condensate collector 13. Fusel tower 8,

accordingly, through the heat exchangers-boilers 7 and 9, the steam lines are connected to the epilation column 5 and to the condensate collector 13. The epilation column 5 is connected to the methanol column 10 through the heat exchanger-boiler 11 and the ether column 12 is connected to the condensate collector 13. Bruzhnaya 1, methanol 10 and ether 12 columns, through the corresponding heat exchangers (not shown in the diagram) are connected by steam lines to the vacuum pump, and the epilation column also through the corresponding heat exchangers (not shown) is connected to vacuum pump or atmosphere.

The distribution of pressure and temperature between the BRU columns provides the reuse of the energy of the steam heating the distillation 3 and fuselage 8 columns to heat the mash 1, epure 5 (option 1) and methanol 10 and ether 12 (option 2).

The purpose of the mash column 1 is to isolate alcohol from the mash. Volatile impurities are released along with alcohol.

The purpose of the epilation column 5 is to isolate the head and partially intermediate impurities from the mixture of alcohol and its accompanying volatile impurities, concentrate them and remove them from the installation.

The purpose of distillation column 3 is to isolate alcohol from the epuret, to concentrate it, freeing from tail, intermediate, end and the remainder of the head impurities.

The purpose of the methanol column 10 is to isolate residues of head and end impurities (such as methanol) from rectified alcohol.

In fusel tower 8, further focussing of fusel oil and other intermediate impurities started in distillation column 3 is carried out.

In the ether column 12, further concentration of the head intermediate impurities coming from the condensation condenser 5 and the crude 1 column is carried out.

The distribution of heat fluxes is as follows.

Hot steam enters the heat exchanger-boiler 4 for heating the distillation column 3. Part of the vapors leaving the top of the distillation column 3 enters the heat exchanger-boiler 2 of the distillation column 1 for heating it. Another part of the vapor from the top of the distillation column 3 enters the heat exchanger-boiler 6 of the epilation column 5 for additional heating. To create the necessary temperature difference in the heat exchanger-boiler 2 of the tower column 1 and the heat exchanger-boiler 6 of the emulsion column 5, the distillation column 3 operates under overpressure, the metal 1 under vacuum, and the emulsion 5 under atmospheric pressure or vacuum. Due to the work of the brewing column 1 under rarefaction, a significant neoplasm of esters and aldehydes can be avoided. Vapors leaving the top of the mash column 1 enter the heat exchanger (not shown in the diagram) for preheating the mash. Vapors that are not condensed in the heat exchanger to heat the mash, enter the next heat exchanger (not shown in the diagram) for condensation. Vapors not condensed in the previous heat exchanger enter an additional heat exchanger (not shown in the diagram) for condensation. Vapors that are not condensed in the heat exchanger-boiler 2 and in the heat exchanger-boiler 6 enter the heat exchanger (not shown in the diagram) of the distillation column 3 for final condensation.

Hot steam enters the heat exchanger-boiler 9 for heating the fusel tower 8. The vapors leaving the top of the fusel tower 8 enter the heat exchanger-boiler 7 of the emulsion column 5 for its main heating. Thus, the main heating

the columns 5 are carried out through the heat exchanger-boiler 7 in pairs leaving the fuselage column 8, and additional heating through the heat exchanger-boiler 6 in pairs leaving the distillation column 3. Vapors not condensed in the heat exchanger-boiler 7 of the emulsion column 5 enter the heat exchanger (on scheme not shown) fuselage column 8 for their final condensation. To create the necessary temperature difference in the heat exchanger-boiler 7 of the emulsion column 5, the fuselage column 8 operates under excessive pressure, and the emulsion column 5 operates under atmospheric pressure or vacuum.

According to the first embodiment, the vapor from the top of the epilation column 5 enters the heat exchanger, then to the additional heat exchanger (not shown in the diagram) of the epilation column 5 for condensation.

According to the second option, the vapors leaving the top of the epilation column 5 enter the heat exchanger-boiler 11 of the methanol column 10 for heating it. To create the necessary temperature difference in the heat exchanger-boiler 11 of the methanol column 10, it also operates under vacuum, for which an additional heat exchanger (not shown) of the methanol column 10 is connected to a vacuum ring pump (not shown). Vapors leaving the top of the methanol column 10 enter a heat exchanger, and then into an additional heat exchanger (not shown in the diagram) to condense them. Vapors that are not condensed in the heat exchanger-boiler 11 enter the additional heat exchanger (not shown in the diagram) of the epilation column 5 for condensation.

Steam condensate from the heat exchangers-boilers 4 and 9, respectively, distillation 3 and fusel towers 8 enters the condensate collector 13. The condensate collector 13 is connected to the ether column 12, in which the vacuum is maintained. Due to the fact that a vacuum also occurs in the condensate collector 13, a secondary

evaporation of the steam condensate, and the resulting vapors enter the cube of the ether column 12 to heat it. This allows you not to spend steam on heating the ether column 12. Vapors leaving the top of the ether column 12 enter the heat exchanger and then into the additional heat exchanger (not shown in the diagram) for condensation.

Vapors that are not condensed in additional heat exchangers (not shown in the diagram) of the bath 1, epure 5, methanol 10 and ether 12 columns are supplied to a vacuum liquid ring pump (not shown in the diagram) for final condensation and to create the necessary vacuum in these columns. Vapors that are not condensed in a vacuum ring-type pump enter a trap (not shown in the diagram) for final condensation, and then are released to the atmosphere.

The heat exchangers of the beer 1, methanol 10 and the ether 12 columns, as well as additional heat exchangers of the beer 1, epurection 5, distillation 3, methanol 10, fuselage 8 and ether 12 columns (not shown in the diagram) are cooled by water.

The rectification unit (BRU) is equipped with a vacuum ring-type pump (not shown in the diagram) to create the necessary vacuum in columns 1, 5, 10, and 12.

The proposed system of heat flux supply, in which distillation 3 and fuselage 8 columns are heated with hot steam, and in which they create increased pressure, while rectification processes are carried out under reduced pressure in mash 1, methanol 10 and ether 12 columns, and in epuration 5, under reduced pressure, and at atmospheric pressure, it allows to increase the evaporation rates of methanol, esters, aldehydes and other head impurities, to ensure a more complete extraction of these impurities from alcohol, to reduce their neoplasm and improve the quality of the final product. Heated 1, epurative 5, methanol 10 and ether 12 columns (option 2) are heated by reuse of heat

steam energy from distillation 3, fuselage 8 columns, as well as steam self-evaporation of steam condensate in the condensate collector 13, which reduces the energy consumption for obtaining the final product.

The proposed heat supply system allows to obtain rectified alcohol of better quality and with lower energy consumption.

In the proposed utility model, the processes of distillation purification of alcohol from methanol, esters, aldehydes, fusel and other impurities are carried out in mash 1, under reduced pressure, in epuration 5 under reduced or atmospheric pressure, and in distillation 3 and fusel 8 under increased pressure (option one). For additional purification of the final product (option 2), the distillation purification processes are carried out in brezhka 1, methanol 10 and ether 12 columns under reduced pressure, emulsion 5, and in distillation 3 and fuselage 8 under elevated pressure, which increases the evaporation rates of methanol, esters, aldehydes and other head impurities, provides a more complete extraction of these impurities from alcohol, reduces their neoplasm and improves the quality of the final product.

In the proposed system for supplying heat fluxes, heating of brew 1, epuretion 5, methanol 10 and ethereal 12 columns is carried out by reusing the thermal energy of steam from distillation 3, fuselage columns 8, as well as steam self-evaporation of steam condensate, which reduces energy costs for obtaining the final product by compared with the known method.

Claims (4)

1. The heat flow supply system upon receipt of rectified alcohol in the distillation rectifier, including a source of hot steam and steam pipelines communicating with each other, respectively, through heat exchangers, boilers, distillation, distillation and fuselage columns, while the source of sharp steam is in communication with fusel tower, characterized in that the source of hot steam, in addition, is connected with a distillation column, which is in communication with the mash column, communicated through heat exchangers with a vacuum pump, fuser Single column communicates with Epuration column, through the heat exchangers which communicates with the atmosphere or a vacuum pump. 2. The heat flow supply system according to claim 1, characterized in that the distillation column is additionally communicated with the epilation column. 3. The heat flow supply system upon receipt of rectified alcohol in the distillation rectifier, including a source of hot steam and steam pipelines communicating with each other through heat exchangers-boilers, mash, distillation, epuration, fusel, methanol and ether columns, while the source of hot steam is in communication with fusel tower and methanol and ether columns are communicated through heat exchangers with a vacuum pump, characterized in that the source of sharp steam, in addition, is communicated with a distillation column, which communicated with the brew column communicated through heat exchangers with a vacuum pump, the fusel column is communicated with an epilation column that communicates with a methanol column, while the distillation and fusel columns are communicated with a condensate collector, which is in communication with the ether column, while the epilation column is communicated through heat exchangers with atmosphere or vacuum pump. 4. The heat flow supply system according to claim 3, characterized in that the distillation column is additionally communicated with the epilation column.