WO2000024488A1 - Vakuumdestillationsanlage und verwendung derselben zur aufkonzentration von organisch-wässrigen lösungsmittelgemischen - Google Patents
Vakuumdestillationsanlage und verwendung derselben zur aufkonzentration von organisch-wässrigen lösungsmittelgemischen Download PDFInfo
- Publication number
- WO2000024488A1 WO2000024488A1 PCT/EP1999/007968 EP9907968W WO0024488A1 WO 2000024488 A1 WO2000024488 A1 WO 2000024488A1 EP 9907968 W EP9907968 W EP 9907968W WO 0024488 A1 WO0024488 A1 WO 0024488A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- vacuum distillation
- bottom product
- condensate
- evaporator
- distillation system
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/284—Special features relating to the compressed vapour
- B01D1/2856—The compressed vapour is used for heating a reboiler or a heat exchanger outside an 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
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/009—Collecting, removing and/or treatment of the condensate
Definitions
- the present invention relates to a vacuum distillation system and a method for concentrating organic-aqueous solvent mixtures, in particular spissum extracts, using this system.
- One way of producing plant-based medicinal products is to extract the plant material and further process the extracts and tinctures obtained into dry extracts.
- aqueous, alcoholic or mixed aqueous / alcoholic extracts are produced, whereby mostly ethanol is used as the alcoholic component.
- the extracts can also contain other organic solvents such as methanol, propanol, butanols and also ethers or ketones (in particular ethyl ether and acetone).
- the extracts or tinctures obtained in this way are either used as such or concentrated to give so-called spissum extracts. These can then be processed into dry extracts.
- Organic-aqueous solvent mixtures are normally concentrated by bubble or surface evaporation.
- the thickening or evaporation is usually carried out by means of conventional distillation.
- Conventional distillation to thicken or evaporate spissum extracts or more generally aqueous, alcoholic solutions has several disadvantages.
- a lot of energy is needed to vaporize strongly polar solutions like water or alcohol.
- about 1 kW of power is required to evaporate one kilo of water in conventional evaporator systems, which corresponds to 15 times the amount required for the distillation of apolar solvents such as toluene.
- apolar solvents such as toluene.
- On the apparatus side this in turn requires that the heat exchanger surfaces are particularly large and that heat must be supplied continuously. This means that processes without heat recovery are extremely uneconomical.
- distillation plants with heat recovery are known from other areas of technology.
- the open heat pump with mechanical compression has the best key figures. For example, 50 watts / kg are required for the distillation of water, which corresponds to an energy consumption that is 20 times less than with conventional distillation.
- the distillation plant known from the prior art works on the principle of the open heat pump with mechanical vapor compression (compression of the top product).
- the overhead products released in the evaporator under vacuum are volumetrically drawn off by the compressor, compressed, further heated and then deposited in a condenser.
- the condensation energy is fed directly to the evaporation. This creates an energetic cycle that is only kept going by the compressor output without heating and cooling. This allows the amount of heat required to be reduced considerably.
- the system can be operated with a bubble evaporator or a flash evaporator.
- the heat exchanger lies in the sump chamber of the medium to be distilled, while in the flash evaporator the sump product is passed through the heat exchanger with a circulation pump conveyed, warmed back into the evaporator and expanded there for distillation.
- These systems are used for the concentration of baths and rinsing water from degreasing, phosphating, chromating and electroplating, for cooling lubrication emulsions, vibratory grinding emulsions, compressor condensates or washing solutions from washing booths and high-pressure cleaners.
- the distillate can be fed to the conventional wastewater, while a highly concentrated concentrate is removed as a bottom product for disposal.
- this type of distillation still has the problem that the more volatile solvent is first distilled off and the ratio with the solvent to one another in the bottom product therefore shifts.
- a vacuum distillation system comprising a) a flash evaporator, b) a vapor compressor, and c) a multi-stage condenser connected downstream of the vapor compressor, preferably with an intermediate rectification, in which means for recycling at least part of the condensate from a condensation stage the evaporator are provided.
- the condenser preferably serves as a heat exchanger and is arranged in such a way that the bottom product serves as cooling liquid or heat transfer liquid for the condenser before being returned to the evaporator or before being injected into the flash evaporator. This happens in the as the bottom product before feeding into the evaporator Coolant is led past the condenser. The bottom product takes up the heat of condensation of the distillate in exchange and is brought back to the distillation temperature. When it is fed back into the flash evaporator, the bottom product relaxes, with some of the solvents evaporating and the remaining liquid cooling. This in turn occurs as a bottom product, which can again be used for cooling.
- the "cooling liquid” is guided according to the principle of heat exchange, whereby this is first brought into contact with the colder condensation stage for the most volatile components of the top product, which are followed by further condensation stages in order of the volatility of the precipitated distillate components up to the condensation stage for the most volatile components.
- water is the most volatile constituent of the top product and the alcohol (s) the more volatile constituent (s) thereof.
- the distillate condensates are removed separately from the condensation stages.
- Rectification is preferably provided between the condensation stages in order to achieve a better separation of the overhead product components from one another.
- the condensate is again fed to the bottom product of at least one stage by means of lines provided for this purpose before it is fed back to the evaporation.
- the more volatile constituent alcohol serves as an entrainer for the less volatile constituent water, which is entrained from the aqueous, alcoholic solvent mixture below the azeotropic point.
- the condensate is preferably returned to the evaporator above the liquid level of the bottom product.
- the condensate can also be fed to the bottom product, mixed with this and, if appropriate, further solution (spissum extract) and the mixture fed to the evaporator.
- the efficiency of the cooling process can be increased by providing means for the active passage of the bottom product or bottom from the evaporator through the condenser. This is preferably a circulation pump.
- the device according to the invention preferably has the features described in the claims.
- a process for the gentle concentration of aqueous, alcoholic solutions in which a) the solution is released under vacuum, b) the head product is volumetrically conveyed and compressed, c) the head product is condensed in several stages in order to convert it into its less volatile and separate more volatile constituents, and d) feeding at least part of the condensate back to the bottom product at least one stage before it is used again in step a) until the desired concentration is achieved.
- the bottom product is preferably used as a cooling liquid for the condensation stages, in that it is actively guided past the various condensation stages as described above.
- a method for the gentle concentration of binary aqueous, alcoholic (preferably ethanolic) solutions is preferably provided, in which two condensation steps take place in step c) and the condensate of the second stage, which is the more volatile alcohol, in particular ethanol the bottom product is fed again.
- the condensate is preferably returned in such an amount leads to the fact that the water / alcohol ratio (water / ethanol ratio) of the solution in the bottom product remains constant.
- Evaporation takes place with the help of flash evaporation.
- the flash evaporation allows working at low temperatures, while reducing the surface load of the product, reducing the residence time and homogeneous energy consumption. This avoids a thermal load on the medicinally active constituents of the plant extracts. In general, it is possible to narrow down solutions that contain heat-sensitive substances.
- the method is preferably used according to the invention for concentrating aqueous, ethanolic plant drug extracts with an ethanol content of at least 20% by volume, preferably 30 to 70% by volume. Most of the active pharmaceutical ingredients, in particular phenols and flavonoids of plant origin, are soluble in this area. Excessive feeding of the extract into the water phase can be avoided according to the invention, so that no separation of the spissum extract occurs.
- the system according to the invention can be used to carry out the method according to the invention.
- the present invention is based on the idea of using alcohol as entrainer for distilling out the water, which is per se less volatile, and which is obtained from the process without additional energy.
- the temperature in the heat exchanger is controlled by partial condensation so that a simultaneous condensation and separation of several different solvents (water and alcohol (s)) is possible at the same pressure.
- volumetric steam delivery In the case of volumetric steam delivery, the molecules of the gas phase are compressed by a (vapor) compressor in accordance with the composition or the partial pressures of the constituents in the reaction vacuumed room. If, as provided according to the invention, a compressor or a volumetrically promoting system such as a Roots blower is connected between the evaporation process and the condenser, a defined mixture is created behind the compressor, which mixture can be broken down by partial condensation.
- rectification according to the invention is not used on the evaporator side, where the return required for depletion is formed by external heat removal and thus energy loss, but on the condensate side after compression.
- the condensation (and rectification) is used according to the invention in such a way that not only is the hydraulic energy used to separate the vapor pressures, but the heat of condensation of the condensed fractions can be used in a system-internal manner in order to return the bottom product to the working temperature.
- a constant alcohol reflux can be used as an entrainer without having to use energy beyond the compression work.
- part of the condensate is returned to the evaporator or the bottom product, so that the heat contained therein is in turn used to heat the bottom product cooled by the expansion in the flash evaporator has a favorable effect on the energy balance.
- the recycling of the condensate thus not only permits the use of the more volatile solvent component as an entrainer for higher-boiling components, but also contributes to reducing the energy requirement of the overall process.
- the supply of heat via the recirculation of part of the condensate reduces the interfacial load on the bottom product, since heat does not have to be supplied from outside via the interface between the container and the bottom product, but is instead fed in with a liquid. This contributes to the gentle processing or narrowing. By maintaining the alcohol concentration in the bottom product, segregation is also prevented.
- the inventive separation of the top product into its individual components allows them to be recycled separately.
- the top product is broken down into partial condensation steps in several condensation steps.
- rectification can be interposed between the individual condensation steps.
- this is placed between two heat exchangers in the device according to the invention, so that it forms the necessary vapor weight to allow the higher-boiling components (water) to condense out separately from the lower-boiling components (alcohol).
- This effect can preferably be increased by using a backing pump in addition to the compressor. This can be, for example, a liquid ring pump operated with oil.
- the individual condensates can be removed in a relatively pure form, provided that they are not recycled according to the invention.
- a distillation plant according to the invention first comprises an evaporator unit 1 from an evaporator sump 2 and thus the area in which the liquid to be evaporated circulates, a liquid separator 3 in which the product entrained in the evaporation is separated and via a Siphon 4 can run back into the liquid phase, as well as an aerosol separator 5, in which the pre-cleaned vapors or top products in the evaporator head are cleaned again with a tangential separator in order to also separate out the aerosols contained here.
- a probe sits in the middle of the evaporator from below and can be used to measure the filling level in the evaporator. That cooled down by the evaporation Bottom product runs through a drain pipe 6 in the evaporator bottom of the pump 7.
- the drain pipe is extended by a pipe bend, so that the evaporator cannot run completely empty via this line. For complete emptying, an additional line is therefore installed at the deepest point of the evaporator base, which ensures the remaining drain into the pump.
- the bottom product is heated up and returned via a circulation line 9 back to the tangential injection 10 in the evaporator.
- Another solution (feed) can also be fed via the same line.
- the supply takes place via a filling valve 11 through the heat exchanger into the circulation line, the introduction of the feed into the circulation line preferably being designed so that it simultaneously represents the throttle via which the circulating product relaxes, and thus the feed with the circulating bottom product mixed in the line to the evaporator.
- the vapors or overhead products released during the evaporation are drawn off by the vapor compressor 12, preferably a Roots pump or a Roots blower, compressed and simultaneously pressed into the heat exchanger 8a.
- a connecting line 13 goes from the heat exchanger 8a in the bottom area to the rectification 14, so that the vapors not deposited in the heat exchanger rise through the rectification and are then fed into the second heat exchanger 8b via a connecting line 15 of the rectification. The remaining solution is deposited there.
- the condensate of the heat exchangers is drawn off in each case, preferably via diaphragm pumps 16a, b and conveyed out. Depending on the flow control, the condensate of the second heat exchanger is injected again into the head region of the evaporator by means of a valve in order to ensure the reflux ratio here.
- the spissum extract to be concentrated is fed into the evaporator, expanded, and the resulting gases are removed via the compressor. pulled.
- the distillation residue or the bottom product falls into the bottom space and is conducted past the heat exchangers as cooling liquid. Since new extract is constantly fed in via the line and concentrated extract can be removed from the bottom line, the process can be carried out continuously.
- a batch process can optionally also be provided. In both cases, the alcohol content of the bottom product can be regulated continuously, specifically via the amount of the recycled alcohol.
- the working temperature of the process is between 35 and 45 ° C. preferably 38 and 42 ° C.
- the vacuum to be applied is between 80 mbar and 150 mbar, preferably 110 mbar and 130 mbar. Condensate that has not been recycled can be removed and used again for extraction or disposed of as a slightly contaminated product.
- an evaporation ratio of 1:10 can be achieved with the method according to the invention.
- the absolute amount of active pharmaceutical ingredients contained in the extract is not reduced, precipitations or foaming do not occur or only to an extremely small extent.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/806,423 US7291250B1 (en) | 1999-10-20 | 1999-10-20 | Vacuum distillation system and use thereof for concentrating organic-aqueous solvent mixtures |
AU63416/99A AU6341699A (en) | 1998-10-23 | 1999-10-20 | Vacuum distillation system and use thereof for concentrating organic-aqueous solvent mixtures |
JP2000578087A JP3577461B2 (ja) | 1998-10-23 | 1999-10-20 | 真空蒸留装置及び有機水性溶剤混合物の濃縮のためのその使用 |
CA002342982A CA2342982C (en) | 1998-10-23 | 1999-10-20 | Vacuum distillation system and use thereof for concentrating organic-aqueous solvent mixtures |
HK02103902.9A HK1043069B (zh) | 1998-10-23 | 2002-05-24 | 真空蒸餾設備及其濃縮有機含水的溶劑混合物的應用 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19849010.0 | 1998-10-23 | ||
DE19849010 | 1998-10-23 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000024488A1 true WO2000024488A1 (de) | 2000-05-04 |
Family
ID=7885473
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1999/007968 WO2000024488A1 (de) | 1998-10-23 | 1999-10-20 | Vakuumdestillationsanlage und verwendung derselben zur aufkonzentration von organisch-wässrigen lösungsmittelgemischen |
Country Status (7)
Country | Link |
---|---|
JP (1) | JP3577461B2 (de) |
CN (1) | CN1211145C (de) |
AU (1) | AU6341699A (de) |
CA (1) | CA2342982C (de) |
DE (1) | DE19905323C2 (de) |
HK (1) | HK1043069B (de) |
WO (1) | WO2000024488A1 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106582050A (zh) * | 2016-11-03 | 2017-04-26 | 江苏海雷德蒙新能源有限公司 | 一种降膜式蒸发器供液控制系统 |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2016188176A (ja) * | 2013-08-30 | 2016-11-04 | 住友ベークライト株式会社 | フェノールの分離、濃縮、及び/又は回収方法、並びにそのシステム |
JP6199192B2 (ja) * | 2014-01-14 | 2017-09-20 | 日本化学機械製造株式会社 | 蒸発装置における熱回収システム |
JP6850000B2 (ja) * | 2017-05-18 | 2021-03-31 | 株式会社ササクラ | ルーツブロワの防食方法 |
AT17768U3 (de) * | 2022-09-27 | 2023-03-15 | Gig Karasek Gmbh | Anlage und Verfahren zur Aufkonzentrierung von substanzhaltigen Flüssigkeiten durch mehrstufiges Eindampfen |
CN115888141A (zh) * | 2022-11-04 | 2023-04-04 | 石家庄博欧金属制品有限公司 | 精密铸造用蜡液回收处理装置 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2435521A1 (fr) * | 1978-09-11 | 1980-04-04 | Tournaire Sa | Dispositif pour extraire les huiles essentielles par hydrodistillation. |
US4305790A (en) * | 1980-01-31 | 1981-12-15 | Kramer Sr Edward F | Multiple effect distillation method and apparatus |
DE4129076A1 (de) * | 1991-09-02 | 1993-03-04 | Leuna Werke Ag | Verfahren zur reinigung von caprolactam |
WO1993024198A1 (de) * | 1992-06-04 | 1993-12-09 | Transferon Wäschereimaschinen Gmbh | Verfahren zur aufbereitung verunreinigter höhersiedender lösemittel sowie vorrichtung zur durchführung des verfahrens |
EP0600203A1 (de) * | 1992-11-30 | 1994-06-08 | Buss Ag | Verfahren zum Weiterverarbeiten des Vakuumrückstandes in einer Rohölraffinerie |
DE29504345U1 (de) * | 1995-03-01 | 1995-05-18 | ESA Tech Dr. Baumann GmbH, 99817 Eisenach | Vorrichtung zur Wiederaufbereitung eines verunreinigten Lösemittels |
WO1997020606A1 (en) * | 1995-12-06 | 1997-06-12 | C.I.T. S.R.L. | A method and a device for purifying water |
-
1999
- 1999-02-09 DE DE19905323A patent/DE19905323C2/de not_active Expired - Fee Related
- 1999-10-20 CN CNB998123927A patent/CN1211145C/zh not_active Expired - Fee Related
- 1999-10-20 WO PCT/EP1999/007968 patent/WO2000024488A1/de active Application Filing
- 1999-10-20 JP JP2000578087A patent/JP3577461B2/ja not_active Expired - Fee Related
- 1999-10-20 CA CA002342982A patent/CA2342982C/en not_active Expired - Fee Related
- 1999-10-20 AU AU63416/99A patent/AU6341699A/en not_active Abandoned
-
2002
- 2002-05-24 HK HK02103902.9A patent/HK1043069B/zh not_active IP Right Cessation
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2435521A1 (fr) * | 1978-09-11 | 1980-04-04 | Tournaire Sa | Dispositif pour extraire les huiles essentielles par hydrodistillation. |
US4305790A (en) * | 1980-01-31 | 1981-12-15 | Kramer Sr Edward F | Multiple effect distillation method and apparatus |
DE4129076A1 (de) * | 1991-09-02 | 1993-03-04 | Leuna Werke Ag | Verfahren zur reinigung von caprolactam |
WO1993024198A1 (de) * | 1992-06-04 | 1993-12-09 | Transferon Wäschereimaschinen Gmbh | Verfahren zur aufbereitung verunreinigter höhersiedender lösemittel sowie vorrichtung zur durchführung des verfahrens |
EP0600203A1 (de) * | 1992-11-30 | 1994-06-08 | Buss Ag | Verfahren zum Weiterverarbeiten des Vakuumrückstandes in einer Rohölraffinerie |
DE29504345U1 (de) * | 1995-03-01 | 1995-05-18 | ESA Tech Dr. Baumann GmbH, 99817 Eisenach | Vorrichtung zur Wiederaufbereitung eines verunreinigten Lösemittels |
WO1997020606A1 (en) * | 1995-12-06 | 1997-06-12 | C.I.T. S.R.L. | A method and a device for purifying water |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106582050A (zh) * | 2016-11-03 | 2017-04-26 | 江苏海雷德蒙新能源有限公司 | 一种降膜式蒸发器供液控制系统 |
Also Published As
Publication number | Publication date |
---|---|
HK1043069A1 (en) | 2002-09-06 |
DE19905323A1 (de) | 2000-04-27 |
CN1211145C (zh) | 2005-07-20 |
DE19905323C2 (de) | 2000-09-14 |
CN1324261A (zh) | 2001-11-28 |
AU6341699A (en) | 2000-05-15 |
HK1043069B (zh) | 2006-03-03 |
JP3577461B2 (ja) | 2004-10-13 |
CA2342982C (en) | 2005-01-04 |
JP2002528244A (ja) | 2002-09-03 |
CA2342982A1 (en) | 2000-05-04 |
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