GB2457187A - Installation for the distillation of drinking alcohol, especially whiskey - Google Patents

Installation for the distillation of drinking alcohol, especially whiskey Download PDF

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Publication number
GB2457187A
GB2457187A GB0908325A GB0908325A GB2457187A GB 2457187 A GB2457187 A GB 2457187A GB 0908325 A GB0908325 A GB 0908325A GB 0908325 A GB0908325 A GB 0908325A GB 2457187 A GB2457187 A GB 2457187A
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United Kingdom
Prior art keywords
alcohol
distillation column
steam
column
distillation
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
GB0908325A
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GB2457187B (en
GB0908325D0 (en
Inventor
Daniel Bethge
Paul Hildenbrand
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GEA Wiegand GmbH
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GEA Wiegand GmbH
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Publication of GB0908325D0 publication Critical patent/GB0908325D0/en
Publication of GB2457187A publication Critical patent/GB2457187A/en
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Publication of GB2457187B publication Critical patent/GB2457187B/en
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12H—PASTEURISATION, STERILISATION, PRESERVATION, PURIFICATION, CLARIFICATION OR AGEING OF ALCOHOLIC BEVERAGES; METHODS FOR ALTERING THE ALCOHOL CONTENT OF FERMENTED SOLUTIONS OR ALCOHOLIC BEVERAGES
    • C12H6/00—Methods for increasing the alcohol content of fermented solutions or alcoholic beverages
    • C12H6/02—Methods for increasing the alcohol content of fermented solutions or alcoholic beverages by distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
    • B01D3/003—Rectification of spirit
    • B01D3/004—Rectification of spirit by continuous methods
    • B01D3/005—Combined distillation and rectification
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/38—Steam distillation

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Food Science & Technology (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)

Abstract

The invention relates to an installation for the distillation of drinking alcohol, especially whiskey, comprising a distillation column (5) stripping the crude alcohol vapors from the fermented mash and a rectification column (17) increasing the alcohol content of the crude alcohol. At least a part of the crude alcohol vapors of the first distillation column (5) is condensed in an evaporator, especially a falling film evaporator (39), thereby producing low pressure water vapor from preheated fresh water or the distiller's wash or expansion vapors from the distiller's wash, the pressure and/or temperature thereof being increased in a mechanical condenser (49) and being fed to the distillation column (5) or another distillation column stripping the alcohol vapors from the fermented mash, to heat the same. The energy requirement of the distillation installation can therefore be reduced. Since the mechanical condenser does not condense alcoholic vapors but water vapor, the condenser (49) does not require an explosion-protected design.

Description

Plant for the distillation of potable alcohol, in particular whisky
Description
The invention relates to a plant for the distillation of potable alcohol, in particular whisky from fermented mash.
Conventional distillation plants for potable alcohol, in particular whisky, drive the alcohol out of fermented and therefore alcohol-containing mash by means of a distillation column, also referred to as a mash column.
The preheated, liquid mash is fed to the distillation column in an upper region. The heat energy required for the distillation is fed to the distillation column in the bottom region, for example by directly blowing in fresh steam or indirectly via a reboiler heated by vapour of a further stage of the distillation plant, i.e. a heat exchanger, through which the spent mash collecting in the bottom region of the distillation column is subjected to a forced circulation. Usually, the reboiler of the distillation column is heated by top vapour of a rectification column increasing the alcohol content of the crude alcohol taken off in the distillation column.
The rectification column is usually operated at slightly superatmospheric pressure and at a higher top temperature than the distillation column operated at reduced pressure, so that the heat energy of the top vapour of the rectification column is as a rule sufficient for heating the distillation column. Here, the rectification column is heated by fresh steam.
Conventional distillation plants for potable alcohol require a comparatively large amount of external energy for the distillation process. In addition, the energy balance for the distillation plant must be carefully tailored if sensory changes of the potable alcohol are to be avoided. A change in the taste of the potable alcohol may occur, for example, on local overheating of the alcohol product stream. Thus, the top of the distillation column contains, for influencing the sensory properties of whisky, components made from copper which react chemically with the alcohol vapour and the reaction properties of which change in a temperature-or pressure-dependent manner. Depending on the column temperature, there is a possibility of crack reactions, through which constituents, for example of the spent mash, are converted into readily volatile substances which can enter the crude alcohol.
It is an object of the invention to provide a plant for the distillation of potable alcohol, in particular whisky, which operates in an energy-efficient manner without influencing the sensory properties of the potable alcohol.
The invention starts from a plant for the distillation of potable alcohol, in particular whisky, from fermented mash, comprising: * at least one distillation column taking off alcohol vapour from the fermented mash, * a condenser arrangement condensing at least a part of the alcohol vapour and * a rectification column which increases the alcohol concentration and the top vapour of which heats a reboiler of the distillation column.
The above object is achieved, according to the invention, in that the condenser arrangement comprises an evaporator utilizing the heat of condensation of at least a part of the alcohol vapour of the distillation column for producing steam, and in that the steam can be fed via a mechanical compressor increasing the pressure and/or the temperature of the steam to the distillation column, for heating said column.
In such a distillation plant, not only the heat content of the top vapour of the rectification column but also the heat content of the top vapour taken off from the distillation column and containing the crude alcohol is utilized for heating this distillation column or, in the case of multi-stage plants, for heating a further distillation column. In particular, the compressed steam can also be fed to a further distillation column taking of f alcohol vapour from the fermented mash, for heating said column. The mechanical compressor increases the energy content or the condensation temperature of the alcohol vapour, which otherwise cannot be sufficiently utilized for heating the distillation column. What is important is that the energy required for this purpose can be provided simply and economically not in the form of fresh steam which is expensive to provide but in the form of electrical energy for the motor drive of the mechanical compressor. What is furthermore important is that the mechanical compressor does not compress the alcohol vapour directly but compresses steam which is produced indirectly by means of the evaporator. The compressor therefore need not be designed to be explosion-proof, which simplifies the design of the distillation plant.
The evaporator may be a forced-circulation evaporator.
However, a downf low evaporator is preferred since such an evaporator can be operated with a relatively small temperature difference of, for example, about 5° between the heating circulation temperature and the evaporator exit temperature, which increases the efficiency and the specific heat transfer.
The evaporator is expediently arranged in a forced circulation in which a liquid supplying the steam circulates. The liquid may be spent mash from the bottom region of the distillation column or flash vapour produced from the spent mash. Since the spent mash is taken off hot from the bottom region of the distillation column, the steam can be produced in an energy-efficient manner. In order to ensure that substances forming through denaturing reactions do not enter the alcohol vapour of the distillation column, in a preferred variant for producing the steam exclusively preheated fresh water is used. The circulation loop preferably contains a separator which separates off the steam, for example in the form of a gravity separator, in order to keep solids of spent mash or other suspended substances out of the steam. The separator can also be used for producing flash vapour from spent mash.
This steam is preferably low-pressure steam having a pressure of 200 to about 250 mbar. The pressure of the steam is therefore about 60 to 80 mbar lower than the top pressure in the distillation column. The compressor increases the pressure of the steam to a value greater than the value of the top pressure, for example to 500 to 600 mbar. The compressor may be a customary compressor.
However, rotary vane compressors, such as fans for example, are also particularly suitable. Of course, the mechanical compressor may also comprise a plurality of mechanical compressor stages connected in series with one another.
The mechanical compressor increases not only the pressure of the steam but also the temperature thereof. In order to avoid overheating of the compressed steam to above the temperature required in the distillation column, cooling water may be mixed with the steam prior to compression.
The compressed steam is expediently blown directly into the bottom region of the distillation column.
The distillation plant expediently comprises only a single distillation column which is heated by means of the reboiler and additionally by means of the compressed steam of the mechanical compressor. This has the advantage that the total amount of alcohol is transported at the same pressure and same temperature through the distillation column or the copper components thereof.
Particularly in the case of whisky, good sensory properties can be achieved in this manner, in particular if the top temperature of the distillation column is not more than 85°C. Advantageous values of the top temperature are between 55 and 70°C, while the temperature of the compressed steam is kept at 70 to 90°C.
The top temperature of the rectification column is expediently above 85°C, for example between 85 and 110°C, at a superatmospheric pressure between 1 and 3 bar. In order to reduce the energy requirement of the rectification column, the latter expediently has more than 50 trays, although the rectified potable alcohol is taken off here not via the top of the rectification column but in an upper region of the column located therebelow, in order to avoid enrichment with low-boiling constituents.
Of course, the condensation arrangement may comprise a heat exchanger downstream of the evaporator in the product stream of the alcohol vapour and intended for preheating the fermented mash to be fed to the distillation column, in order to be able to further utilize the heat content of the alcohol vapour of the distillation column which heats the evaporator. The alcohol product stream from the condensation arrangement can be fed to the distillation column and optionally to the rectification column as top ref lux.
Below, an example of embodiment of the invention is explained in more detail with reference to a drawing. Here:
Fig. 1 shows a diagram of a distillation plant set up according to the invention and intended for potable alcohol, in particular whisky.
Fig. 1 shows a distillation plant for potable alcohol, in particular whisky, to which fermented, i.e. ethyl alcohol-containing, mash is fed from a previous stage 1 of the alcohol production process. The mash is heated in a preheater 3 to the distillation temperature of a distillation column 5 and fed via a pipe 7 of the distillation column 5, at a middle level but below catalytic copper components 9, to the distillation column 5. The top region of the distillation column 5, often also referred to as a mash column, is indicated at 11.
The crude alcohol taken off as alcohol vapour from the top region 11 of the distillation column 5 is condensed in a multistage condenser arrangement 13 and passed as feed in liquid form by a conveying pump 15 to a rectification column 17 via a preheater 19 heating the crude alcohol to the rectification temperature of the rectification column 17. The rectification column 17 increases the alcohol content of the crude alcohol of the distillation column S to values between about 93 and 96% by volume. Stages for separating off the fractions undesired in the potable alcohol (fusel oils) are present but not shown. The rectification column 17 discharges the potable alcohol end product at 21 from a column position below its top region 23.
Top vapour taken of f from the top region 23 of the rectification column 17 via a pipe 25 is fed to a reboiler 27 of the distillation column 5, which reboiler takes off spent mash occurring in the bottom region 33 of the distillation column 5 via a forced circulation 31 provided with a pump 29 and via a bottom region connection 35 and, after heating in the reboiler 27, recycles said spent mash to the bottom region 33 of the distillation column 5 for heating said column. The reboiler 27 at the same time forms the top condenser of the rectification column 17 and delivers reflux condensed from the top vapour via a pipe 37 to the top region 23 of the rectification column 17.
The distillation column 5 is operated at a slightly reduced pressure of about 300 to 500 nthar at a top vapour temperature between 55 and 70°C. The rectification column 17 operates at a slightly superatmospheric pressure of not more than 3 bar absolute and a top vapour temperature between 85 and 110°C. In general, in the case of mash raw materials having a relatively high protein content, such as for example rye, wheat, barley, etc., the temperature of the distillation column should not exceed 85°C. Under the operating conditions mentioned, the energy content of the top vapour of the rectification column 17 expediently heated by means of fresh steam is not sufficient for heating the distillation column 5 exclusively via the reboiler 27. The first stage of the condenser arrangement 13 is therefore formed as a falling-film evaporator 39 which vaporizes fresh water circulating in a forced circulation 43 provided with a pump 41. The fresh water is fed in at 45 in preheated form and leaves the falling- film evaporator 39 via a gravity separator 47 as low-pressure steam, which is blown directly into the bottom region 33 of the distillation column 5 via a mechanical compressor 49 with a pressure increased compared with the low-pressure steam and an increased temperature. The low-pressure steam has a pressure of about 200 to 250 mbar on the entrance side of the compressor 49, which is raised by the compressor 49 to an exit pressure between 500 and 600 mbar at a temperature between 70 and 90°C.
In the illustrated example of embodiment, the mechanical compressor 49 comprises three mechanical compressor stages 51 increasing the pressure serially. In principle, however, a single compressor stage is sufficient provided that it meets the requirements with regard to the pressure increase and temperature increase. In order to avoid overheating of the compressed steam, additional water is optionally injected at the entrance of each compressor stage 51 from a source 53. The compressor 49 or its compressor stages 51 may be conventional compressors. Rotary vane compressors or fans are particularly suitable.
In principle, it is also possible to use other evaporator types instead of the falling-film evaporator 39. However, an advantage of the falling-film evaporator is its small temperature difference of, for example, 5°C between the entrance temperature of the top vapour of the distillation column 5 which is to be at least partly condensed and the exit temperature of the low-pressure steam. The energy content of the top vapour can be better utilized in this manner. The electrical energy required for the motor drive of the mechanical compressor 49 can be reduced in this manner. In principle, the mechanical compressor 49 could also be in the form of a steam jet compressor, which, however, would increase the effort involved in providing fresh steam, whereas the provision of electrical energy presents no problems.
Since the top vapour of the distillation column S is not completely condensed in the falling-film evaporator 39, the uncondensed vapour fraction is fed at 55 to the preheater 3 forming the second stage of the condensation arrangement 13, for preheating the mash. The exit vapour of the preheater 3 is finally fed to a main condenser 57 which forms the third stage of the condensation arrangement 13 and discharges the crude alcohol as liquid condensate for passing on to the rectification column 17.
The main condenser 57 is cooled by cooling water which is fed in at 59. The alcohol condensate of the main condenser 57 is combined with the alcohol condensate of the falling-film evaporator 39, taken off at 61, and the alcohol condensate of the preheater 3, taken off at 63.
The pressure in the distillation plant is adjusted by means of a vacuum pump 65 connected to the main condenser 57. It should also be stated that the crude alcohol condensate produced in the condensation arrangement 13 is also fed via a pipe 67 as ref lux to the distillation column 5, in particular before it has passed through the preheater 19. The spent mash obtained in the distillation column 5 is discharged from the circulation loop 31 of the reboiler 27 and, at 69, fed for further use, for example in a drying process for use as animal feed or the like. The separator 47 separates entrained liquid and droplets from the vapour, in order to ensure trouble-free operation of the compressor 49. The production of a slurry at 71 prevents lime deposits and the like in the downf low evaporator 39.
In the example of embodiment of fig. 1, the falling-film evaporator producing the low-pressure steam is fed by preheated fresh water. However, the low-pressure steam can also be produced from spent mash flash vapour which is obtained for example in a flash separator located in the forced circulation 43. The spent mash obtained is taken off from the flash separator and can be fed for further use, for example once again to a drying process.
Since the spent mash already preheated to the distillation temperature, or the vapour thereof, is used for producing the low-pressure steam, the energy requirement of the distillation plant is further reduced.

Claims (11)

  1. Claims 1. Plant for distilling potable alcohol, in particular whisky from fermented mash, comprising at least one distillation column (5) taking off alcohol vapour from the fermented mash, a condenser arrangement (13) condensing at least a part of the alcohol vapour and a rectification column (17) which increases the alcohol concentration and the top vapour of which heats a reboiler (27) of the distillation column (5) p characterized in that the condenser arrangement (13) comprises an evaporator (39) utilizing the heat of condensation of at least a part of the alcohol vapour of the distillation column (5) for producing steam, and in that the steam can be fed via a mechanical compressor (49) increasing the pressure and/or the temperature of the steam to the distillation column (5), for heating said column.
  2. 2. Plant according to Claim 1, characterized in that the evaporator (39) is in the form of a falling-film evaporator.
  3. 3. Plant according to Claim 1 or 2, characterized in that fresh water, in particular preheated fresh water, or spent mash or spent mash flash vapour can be fed to the evaporator (39) for producing the steam.
  4. 4. Plant according to Claim 3, characterized in that the mechanical compressor (49) is connected via a separator (47) separating of f the steam to a circulation (43) passed through the evaporator (39) and intended for fresh water or spent mash or spent mash flash vapour. 1].
  5. 5. Plant according to any of Claims 1 to 4, characterized in that the mechanical compressor (49) comprises a plurality of mechanical compressor stages (51) connected in series.
  6. 6. Plant according to any of Claims 1 to 5, characterized in that the steam compressed by the mechanical compressor (49) is fed directly to the distillation column (5)
  7. 7. Plant according to any of Claims 1 to 6, characterized in that the distillation column (5) is heated by means of the reboiler (27) and additionally by means of the compressed steam of the mechanical compressor (49), preferably to a distillation temperature of not more than 85°C.
  8. 8. Plant according to any of Claims 1 to 7, characterized in that the rectification temperature of the rectification column (17) is higher than 85°C and the alcohol production stream can be fed to the rectification column (17) via a preheating heat exchanger (19).
  9. 9. Plant according to any of Claims 1 to 8, characterized in that the rectification column has more than 50 trays.
  10. 10. Plant according to any of Claims 1 to 9, characterized in that the condenser arrangement (13) comprises a heat exchanger (3) downstream of the evaporator (39) in the product stream of the alcohol vapour and intended for preheating the fermented mash to be fed to the distillation column.
  11. 11. Plant according to any of Claims 1 to 10, characterized in that a part of the alcohol product stream can be fed as ref lux to the condensation arrangement (13) of the distillation column (5).
GB0908325A 2006-10-18 2007-10-18 Installation for the distillation of drinking alcohol, especially whiskey Active GB2457187B (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006049175A DE102006049175A1 (en) 2006-10-18 2006-10-18 Plant for distilling drinking alcohol, in particular whiskey
PCT/EP2007/009060 WO2008046633A1 (en) 2006-10-18 2007-10-18 Installation for the distillation of drinking alcohol, especially whiskey

Publications (3)

Publication Number Publication Date
GB0908325D0 GB0908325D0 (en) 2009-06-24
GB2457187A true GB2457187A (en) 2009-08-12
GB2457187B GB2457187B (en) 2011-05-04

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GB0908324A Active GB2457186B (en) 2006-10-18 2007-10-18 Installation for the distillation of drinking alcohol,especially whiskey
GB0908325A Active GB2457187B (en) 2006-10-18 2007-10-18 Installation for the distillation of drinking alcohol, especially whiskey

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GB0908324A Active GB2457186B (en) 2006-10-18 2007-10-18 Installation for the distillation of drinking alcohol,especially whiskey

Country Status (8)

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EP (1) EP2079538B1 (en)
JP (1) JP4773563B2 (en)
BR (1) BRPI0718474B1 (en)
DE (2) DE102006049175A1 (en)
GB (2) GB2457186B (en)
PL (1) PL2079538T3 (en)
RU (1) RU2440410C2 (en)
WO (2) WO2008046633A1 (en)

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PL2079538T3 (en) 2019-11-29
GB0908325D0 (en) 2009-06-24

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