WO2011029110A1 - Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen - Google Patents
Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen Download PDFInfo
- Publication number
- WO2011029110A1 WO2011029110A1 PCT/AT2010/000320 AT2010000320W WO2011029110A1 WO 2011029110 A1 WO2011029110 A1 WO 2011029110A1 AT 2010000320 W AT2010000320 W AT 2010000320W WO 2011029110 A1 WO2011029110 A1 WO 2011029110A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- separation
- membrane
- stage
- permeate
- module
- Prior art date
Links
Classifications
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
- A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
- A23L2/08—Concentrating or drying of juices
- A23L2/082—Concentrating or drying of juices by membrane processes
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/16—Purification of sugar juices by physical means, e.g. osmosis or filtration
- C13B20/165—Purification of sugar juices by physical means, e.g. osmosis or filtration using membranes, e.g. osmosis, ultrafiltration
Definitions
- the present invention relates to a method and an apparatus for the concentration of valuable solutions by means of pressure-operated membrane processes.
- the desired products are obtained in the form of more or less highly dilute solutions, from which the respective recyclable material must be separated by means of complex separation processes.
- Representative examples include the sugar, fruit juice, pharmaceutical and chemical industries.
- US-A-3,617,550 it is known to concentrate solutions by passing two reverse osmosis separation stages with membranes of different permeability, wherein sometimes permeate from the second stage is recycled into the feed of the first stage. Dilute sugar solution and fruit juices are mentioned as examples of the solution, and the inventors calculate the required operating pressure for each of the two separation stages from the retention ratio of the membrane separation.
- US-A-5,096,590 discloses a similar system having a plurality of separation stages (up to twelve) in which the last permeate is in turn recycled to the feed of the first separation stage.
- This object is achieved in a first aspect by providing a method in which the concentration of a recyclable solution using at least two consecutive membrane separation stages for each separation of the valuable solution in a retentate and a permeate, wherein the cut-off in the Separation stages used membranes is in each case higher than that of the membrane used in the previous stage, the retentate is fed to each separation stage with the exception of the last stage as the feed of the next separation stage and the permeate from at least one separation stage recycled to a previous separation stage and in the feed wherein the method is characterized in that the recirculated permeate has a concentration or viscosity which substantially corresponds to the concentration or viscosity of the feed of the preceding separation stage into which it is introduced.
- the viscosity of the process streams depends, in addition to their temperature, above all on the concentration of the substances dissolved therein, in particular of course the valuable material to be separated off in each case.
- a viscosity "substantially equal to one another" means a difference in viscosities of from 10% to a maximum of 15%, since, especially when aqueous sugar solutions are used, the viscosity is at Increasing the concentration by 1% by weight at lower concentrations (ie at about 15 to 20% solutions) by about 3.5% and at higher concentrations (ie at about 35 to 40% solutions) by about 5 % changes. In those cases where the processed solution of valuable material undergoes no change in temperature in the process, it goes without saying that the control of the concentration goes hand in hand with that of the viscosity.
- the invention provides in preferred embodiments that the difference in the concentrations of recirculated permeate and feed of the preceding membrane separation step not more than 3 wt .-%, more preferably not more than 2 wt .-%, in particular not more than 1% by weight is, whereby the above-described advantages are particularly pronounced.
- the number of separation stages provided in the process according to the invention is not particularly limited.
- the permeate of each separation stage be from the second in initiated the feed of the immediately preceding separation stage, which further increases the efficiency of the process.
- a membrane is used with such a permeability that the difference in osmotic pressure between the retentate and permeate is less than the respective feed side operating pressure.
- a membrane with a cut-off is preferably used in the first separation stage, which is smaller than the size of the recyclable material molecules to be separated, so that practically no valuable substance is lost in the first separation stage. Therefore, in the first membrane separation stage, either reverse osmosis or nanofiltration with a cut-off which is lower than the molecular mass of the valuable substance is carried out as the preferred separation process, whereby valuable solutions which essentially consist only of solvent and valuable substance can be processed. In the second and optionally each further membrane separation stage, however, preferably nanofiltration or ultrafiltration is carried out in order to allow a portion of the valuable material to pass through the membrane and thus to adjust the suitable concentration or viscosity in the respective permeate stream.
- the selection of the recyclable solution to be separated in the process according to the invention is not particularly limited.
- sugar solution or fruit juice but also solutions of lactic acid or a salt thereof, amino acid solutions or other aqueous, non-aqueous or mixed aqueous-nonaqueous solutions can be used, as for example in the fields of the chemical industry, pharmaceutical chemistry, biotechnology etc. incurred.
- a sugar solution is particularly preferably processed in the process according to the invention, in which case a hot raffinate sugar solution is used in particular.
- the pressure drop in the membrane modules decreases significantly due to the lower viscosity at higher temperature, without the solution needs to be heated additionally.
- the energy required for pumping the solution through the system, and the energy consumption for a downstream evaporation unit is significantly reduced, since the retentate from the last membrane separation stage already obtained at a higher temperature.
- the present invention relates to an apparatus for carrying out a preferred embodiment of the method according to the invention, namely a device for concentrating a recycling solution, comprising: a) at least two serially connected membrane separation modules each having a feed line, a retentate line and a permeate line in which the retentate line of each separation module, with the exception of the last one, at the same time constitutes or opens into the feed line of the respectively following separation module, wherein at least one permeate line opens into the feed line of a preceding separation module and wherein the cut-off of the membranes used in the separation modules is in each case higher than that the membrane used in the preceding separation module is; b) at least one pressure device for acting on at least the first separation module with pressure; and c) optionally one or more heating and / or cooling elements; wherein the device is characterized in that at least three membrane separation modules are provided and the permeate line of each separation module opens from the second into the feed line of a preceding separation module.
- the permeate line of each separation module preferably discharges from the second into the feed line of the immediately upstream separation module, as seen in the flow direction of the valuable solution, since the concentrations are thus easier to adjust accordingly, as described in the method according to the first aspect of the invention.
- permeate streams are basically depressurized
- further pressure devices are provided for the feed streams consisting of the retentate of the preceding and the permeate of a subsequent separation stage.
- a pressure device for acting on the separating module is provided with pressure for each separation module in the feed line opens a Permeattechnisch.
- the additional pressure devices ensure a high throughput of the device according to the invention and a more uniform flow therein, without the need to set an excessively high output for the first pressure device.
- the first separation module comprises a membrane with a cut-off which is smaller than the size of the valuable molecules to be separated, so that essentially no valuable substance is separated off in the first separation module.
- the first separation module is a reverse osmosis module, since particularly small cut-off values are possible, or a nanofiltration module with a cut-off, which is lower than the molecular weight of the recyclable, whereby valuable solutions are processed, which consists essentially only of solvent and Recyclable material.
- the second and optionally any further separation module is or are preferably (a) nanofiltration module (s) or ultrafiltration module (s) with higher cut-off values to allow a portion of the valuable material to pass through the membrane and thus the appropriate concentration or viscosity in the respective permeate stream.
- at least one membrane of at least one separation module is a temperature-stable membrane. If a high temperature of the reusable solution is to be maintained throughout the device, even more preferably, any membrane used therein is temperature stable.
- at least one membrane of at least one separation module is a ceramic membrane, since it is characterized by particularly high thermal and chemical stability and by very good cleaning capability.
- At least one membrane of at least one separation module is preferably a membrane with a particularly high permeability, ie a high-flux membrane. This either increases the throughput of the device, or it can be used at the same throughput smaller membrane areas. In addition, the membranes can thus have lower retention or higher cut-off values.
- the apparatus of the present invention may not only include one or more optional heating and / or cooling elements to cool or heat individual separation modules and / or associated inlets and outlets, but also others conventional components such as additional pumps, overpressure or check valves, bypass lines, pressure gauges, temperature sensors or the like may contain or contain.
- Figure 1 shows a flow chart of the method according to the invention in its simplest embodiment in a device according to the prior art
- Fig. 2 is a flow chart of a preferred embodiment of the method according to the invention in a device according to the present invention.
- a conventional apparatus for carrying out a two-stage membrane separation process is shown, as it is known for example from US-A-3,617,550.
- a recyclable solution e.g. a sugar solution is introduced via feed line 11 into a first membrane separation module 1, which is pressurized by means of a pressure device 4, usually a pump.
- the solution is separated into a retentate and a permeate, of which the first via retentate 12 and the latter via permeate 13 are discharged.
- the permeate obtained from 13 which normally has very low valuable substance concentrations, is therefore generally discarded, while the retentate obtained from 12 is introduced via feed line 21 into a second separation module 2 in order to be subjected to the second separation stage.
- the accumulating there retentate is removed via retentate 22 and represents the desired concentrated solution of recyclable material, while the second permeate, which usually has significantly higher concentrations of valuable material than the first, is recycled to the first separation module.
- such a separation process is optimized in that the concentration and / or the viscosity of the recirculated permeate is adjusted so that it corresponds substantially to the concentration of the feed solution, with which the permeate is mixed.
- concentration difference is not more than 3% by weight or the viscosity difference is not more than 15%, preferably not more than 2% by weight or not more than 10%, more preferably not more than 1% by weight. -% or not more than 5%.
- Such an adjustment of the concentration or viscosity according to the invention is carried out by suitable design of the entire plant, with particular attention being paid to the separation membranes, the respective pressure conditions and optionally the temperatures of the individual streams.
- the present invention does not only relate to a two-stage separation process.
- the number of separation stages is subject to no restriction, and in preferred embodiments of the process according to the invention, at least three separation stages are used, as shown in FIG.
- This figure therefore simultaneously represents a flow chart of a preferred embodiment of the method of the invention and schematically an apparatus according to the second aspect of the invention for carrying out this preferred embodiment of the method according to the invention.
- the device from FIG. 2 is expanded by a third separation module 3, into which the permeate originating from the retentate line 22 of the second separation module is introduced via the associated feed line 31.
- This feed is again separated, in which case the solution withdrawn via retentate 32 represents the desired concentrated solution of valuable material.
- the concentration of the concentrated recyclable solution can be further increased, which means, for example, in the case of a raffinate sugar solution as the starting feed of the process an even greater energy saving in the subsequent evaporation process.
- the following embodiments simulate two- and three-stage separation processes using the example of a refined sugar solution, i. an aqueous solution of sucrose at a temperature of 40 ° C, assuming that there is no significant change in temperature in the system, which in practice means high throughputs of the individual separation modules and optionally additional heating of the modules and / or lines is achievable.
- a refined sugar solution i. an aqueous solution of sucrose at a temperature of 40 ° C
- the two-stage example 1 is exclusively an exemplary embodiment of the method according to the invention, while examples 2 and 3 illustrate both the method and the apparatus of the invention.
- the following membranes were used for the simulations:
- TFC-SR3 from Koch Membrane Systems, a polyamide-based plastic nanofiltration membrane with a cut-off of 200-300 Da;
- SeIRo MPF-36 from Koch Membrane Systems, a plastic nano-filtration membrane unspecified by the manufacturer for the material, with a cut-off of 1000 Da;
- Example 3 shows that although the expansion of the plant by the additional third separation stage, no stronger concentration effect, but a significantly increased flow through the device could be achieved.
- Example 3 an increased concentration of the valuable solution is achieved compared to Example 1, so that in the subsequent evaporation process smaller amounts of energy are required than in the prior art.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Nutrition Science (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Biochemistry (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/394,859 US20120238777A1 (en) | 2009-09-11 | 2010-09-08 | Method and device for concentrating material solutions |
BRBR112012008378-3A BR112012008378A2 (pt) | 2009-09-11 | 2010-09-08 | Processo e dispositivo para a concentração de soluções de materiais. |
EP10768853A EP2475269A1 (de) | 2009-09-11 | 2010-09-08 | Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ATA1446/2009 | 2009-09-11 | ||
AT0144609A AT508549B1 (de) | 2009-09-11 | 2009-09-11 | Verfahren und eine vorrichtung zur aufkonzentrierung von wertstofflösungen |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2011029110A1 true WO2011029110A1 (de) | 2011-03-17 |
Family
ID=43064683
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/AT2010/000320 WO2011029110A1 (de) | 2009-09-11 | 2010-09-08 | Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen |
Country Status (6)
Country | Link |
---|---|
US (1) | US20120238777A1 (de) |
EP (1) | EP2475269A1 (de) |
AT (1) | AT508549B1 (de) |
BR (1) | BR112012008378A2 (de) |
CU (1) | CU20120043A7 (de) |
WO (1) | WO2011029110A1 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105603130A (zh) * | 2015-10-28 | 2016-05-25 | 中国科学院过程工程研究所 | 一种甘蔗制糖过程中残糖的回收装置及方法 |
CN110559875A (zh) * | 2019-09-22 | 2019-12-13 | 张俊杰 | 用于处理医疗废物的无害净化设备 |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2978755B1 (fr) * | 2011-08-02 | 2014-11-21 | Veolia Water Solutions & Tech | Installation de traitement d'eau par osmose inverse comprenant une premiere passe ayant plusieurs etages |
EP3925689A1 (de) * | 2020-06-16 | 2021-12-22 | Prayon | Verfahren zur reinigung einer phosphat enthaltenden sauren lösung, die verunreinigungen enthält, und vorrichtung zu deren anwendung |
CN113088324B (zh) * | 2021-04-14 | 2023-04-07 | 山东英可利新材料技术有限公司 | 一种从废润滑油、重质油或沥青中提取碳纳米材料的方法 |
US11534719B1 (en) * | 2021-07-02 | 2022-12-27 | Gradiant Corporation | Membranes with controlled porosity for serial filtration |
CN114307362A (zh) * | 2021-12-30 | 2022-04-12 | 无锡东恒新能源科技有限公司 | 一种碳纳米管浆料过滤装置 |
DE102023107305A1 (de) | 2023-03-23 | 2024-09-26 | Kärcher Futuretech GmbH | Mobile wasseraufbereitungsanlage zum erzeugen von trinkwasser in einem katastrophengebiet |
CN117180992A (zh) * | 2023-11-07 | 2023-12-08 | 山东赛特智能装备股份有限公司 | 一种桦树汁浓缩设备及其方法 |
Citations (2)
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US3617550A (en) | 1969-04-04 | 1971-11-02 | Hydronautics | Method and apparatus for the concentration of solutions |
US5096590A (en) | 1989-06-19 | 1992-03-17 | Director Of National Food Research Institute, Ministry Of Agriculture, Forestry And Fisheries | Concentration of solution by the reverse osmosis process |
Family Cites Families (8)
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US3836457A (en) * | 1973-03-19 | 1974-09-17 | Westinghouse Electric Corp | System for concentrating solutions by low pressure recycling |
US4000065A (en) * | 1974-11-18 | 1976-12-28 | Basf Wyandotte Corporation | Method and apparatus for purifying aqueous streams contaminated with organic materials |
US5238574A (en) * | 1990-06-25 | 1993-08-24 | Kawasaki Jukogyo Kabushiki Kaisha | Method and apparatus having reverse osmosis membrane for concentrating solution |
US7976710B2 (en) * | 2003-02-18 | 2011-07-12 | Exxonmobil Research And Engineering Company | Membrane and process for the recovery of acid |
DK2007506T3 (da) * | 2006-03-31 | 2014-06-16 | Danisco Us Inc | Tangentialstrømningsfiltreringsapparater, -systemer og -fremgangsmådertil separering af forbindelser |
CA2669279C (en) * | 2006-10-27 | 2017-01-03 | Cms Technologies Holdings, Inc. | Removal of water and methanol from fluids |
CN101269298B (zh) * | 2007-03-23 | 2011-06-01 | 中国科学院过程工程研究所 | 利用浓差极化浓缩生物大分子的膜过滤方法及其装置 |
JP2008307487A (ja) * | 2007-06-15 | 2008-12-25 | Mitsubishi Heavy Ind Ltd | 脱塩装置 |
-
2009
- 2009-09-11 AT AT0144609A patent/AT508549B1/de active
-
2010
- 2010-09-08 US US13/394,859 patent/US20120238777A1/en not_active Abandoned
- 2010-09-08 WO PCT/AT2010/000320 patent/WO2011029110A1/de active Application Filing
- 2010-09-08 BR BRBR112012008378-3A patent/BR112012008378A2/pt not_active Application Discontinuation
- 2010-09-08 EP EP10768853A patent/EP2475269A1/de not_active Withdrawn
-
2012
- 2012-03-12 CU CU20120043A patent/CU20120043A7/es unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3617550A (en) | 1969-04-04 | 1971-11-02 | Hydronautics | Method and apparatus for the concentration of solutions |
IT1065411B (it) * | 1969-04-04 | 1985-02-25 | Hydronautics | Metodo ed apparecchio per la concentrazione di soluzioni mediante osmosi inversa |
US5096590A (en) | 1989-06-19 | 1992-03-17 | Director Of National Food Research Institute, Ministry Of Agriculture, Forestry And Fisheries | Concentration of solution by the reverse osmosis process |
Non-Patent Citations (1)
Title |
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DATABASE WPI Week 197115, Derwent World Patents Index; AN 1971-26459S, XP002610058 * |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105603130A (zh) * | 2015-10-28 | 2016-05-25 | 中国科学院过程工程研究所 | 一种甘蔗制糖过程中残糖的回收装置及方法 |
WO2017071585A1 (zh) * | 2015-10-28 | 2017-05-04 | 中国科学院过程工程研究所 | 一种甘蔗制糖过程中残糖的回收装置及方法 |
CN105603130B (zh) * | 2015-10-28 | 2019-07-19 | 中国科学院过程工程研究所 | 一种甘蔗制糖过程中残糖的回收装置及方法 |
CN110559875A (zh) * | 2019-09-22 | 2019-12-13 | 张俊杰 | 用于处理医疗废物的无害净化设备 |
Also Published As
Publication number | Publication date |
---|---|
EP2475269A1 (de) | 2012-07-18 |
US20120238777A1 (en) | 2012-09-20 |
AT508549B1 (de) | 2011-02-15 |
CU20120043A7 (es) | 2012-07-31 |
AT508549A4 (de) | 2011-02-15 |
BR112012008378A2 (pt) | 2015-08-25 |
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