EP0226605A1 - Procede et dispositif pour le traitement a phase multiple des liquides aqueux - Google Patents

Procede et dispositif pour le traitement a phase multiple des liquides aqueux

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Publication number
EP0226605A1
EP0226605A1 EP86903339A EP86903339A EP0226605A1 EP 0226605 A1 EP0226605 A1 EP 0226605A1 EP 86903339 A EP86903339 A EP 86903339A EP 86903339 A EP86903339 A EP 86903339A EP 0226605 A1 EP0226605 A1 EP 0226605A1
Authority
EP
European Patent Office
Prior art keywords
ice
steam
liquid
pulp
evaporator
Prior art date
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.)
Withdrawn
Application number
EP86903339A
Other languages
German (de)
English (en)
Inventor
Chahpar Mostofizadeh
Michael Thomas Koschowitz
Collin Livanos
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Fried Krupp AG
Original Assignee
Fried Krupp AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Fried Krupp AG filed Critical Fried Krupp AG
Publication of EP0226605A1 publication Critical patent/EP0226605A1/fr
Withdrawn legal-status Critical Current

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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
    • A23L2/12—Concentrating or drying of juices by freezing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/02—Crystallisation from solutions
    • B01D9/04—Crystallisation from solutions concentrating solutions by removing frozen solvent therefrom
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/22—Treatment of water, waste water, or sewage by freezing

Definitions

  • the present invention relates to a method and a device for the multi-phase treatment of an aqueous liquid and in particular to a method for converting an aqueous liquid into an egg pulp and subsequent treatment of the ice slurry.
  • the invention relates to a method and a device for the concentration and / or crystallization of aqueous solutions, in particular of those that occur in food technology and chemistry. Examples of this are the concentration of fruit juices, organic and inorganic acids as well as the crisis from waste water from various industrial branches.
  • the invention relates to the production of an egg pulp and various uses thereof, in particular the conversion into an ice pulp pumpable consistency and its use for artificial purposes, or the conversion of the ice pulp into solid ice blocks or pellets.
  • the invention entails a concentration build-up in the liquid phase of the ice pulp, but not the solids present in the original aqueous liquid.
  • the invention is efficient on a method and a device for extracting water vapor of low density and temperature with a pressure transformer and subsequent compression with a mechanical compressor to achieve a comparatively high overall efficiency.
  • Such systems have the disadvantage that they work at high temperatures (eg 70 to 100 ° C) and thus favor the formation of dirt and incrustations on system parts. Soiling occurs primarily with temperature-sensitive products, e.g. through biological reactions.
  • a method and a device for the desalination, in particular of sea water are known, in the literature known as vacuum evaporation vaporization processes, of which a large-scale version is known as a "hydroconverter” (KS Spiegier, Principles of Desalination, page 310 ff., (1966) Academic Press, New York and London).
  • KS Spiegier Principles of Desalination, page 310 ff., (1966) Academic Press, New York and London.
  • this technology was not known for any purposes other than seawater desalination, where the product consists of pure water, melted ice and condensed steam condensates, but not for other applications where ice or ice cream was used as a product, or for Application in crystallization and Concentration processes, such as those used in the fruit juice and chemical industries.
  • the industrially preferred method in the hydroconverter uses a kind of falling film evaporation, whereby the sea water runs down as a thin film on the walls of the freezer chamber.
  • the sump in which the ice pulp collects in the freezer chamber is flat and the vacuum space above the ice pulp, where the evaporation takes place and from which the steam is extracted, is also relatively low.
  • the brine tends to be carried along with the vapors and sucked out of the vacuum chamber.
  • a pre-separation of the ice pulp in ice and liquid phase in the flat sump part of the device does not take place, and the ice pulp is withdrawn as a whole from the sump.
  • compressors When compressing steam with saturation temperatures between 60 and 100 oC, compressors achieve overall efficiencies of 75 to 80%. However, if the saturation temperatures are between 0 and 5oC, only efficiencies of 50% are achieved. This enormous difference results from the fact that the diameter of the impeller for compressing the same mass flow at 0oC is 5.7 times as large as at 61oC, and the mechanical losses are considerably greater, not to mention the high cost of such a large device.
  • a task of the invention is to achieve a gentle concentration or effective crystallization at low temperatures and low energy consumption by creating a method and a device.
  • a method for converting an aqueous liquid into an egg pulp with subsequent subsequent treatment of the ice slurry, characterized in that the liquid is injected into an evaporator space which is expanded to a pressure. which is the saturation pressure at the corresponding vaporization temperature of the liquid in the Evaporation space at -5 to 10oC corresponds, so that the liquid partially evaporates due to a phase imbalance caused by a short residence time in the evaporation space and cools down to a low temperature and is then collected with a sufficiently long residence time, so that this occurs due to an Equilibrium forms an ice slurry, the ice slurry is drawn off and subjected to a separation of the liquid phase from the ice slurry, followed by one or more of the following process steps:
  • an aqueous solution for example a solution to be concentrated
  • a nozzle system to a low pressure which corresponds to the saturation pressure of the corresponding evaporation temperature of -5 to 10 ° C, such that the solution is adjusted by setting an imbalance partially evaporated, cooling to a low temperature.
  • the imbalance is achieved in that the nozzle system creates fine drops that have a very short residence time in the steam room.
  • the drops are then collected and then, with a sufficiently long dwell time in the swamp, form an ice pulp which is passed into a separator and freed of ice.
  • the product is drawn off from the separator, while after washing off the attached product, the ice is melted and used to pre-cool the fresh solution.
  • the steam created by imbalance is suctioned off with the aid of a compressor and fed to a condenser in which the washed-out egg is melted and then used to pre-cool the incoming solution.
  • the process just described has the following advantages:
  • the low temperature means that more volatile constituents (e.g. flavorings) are retained in the product.
  • the rate of corrosion is very low, and it. cheap materials can be used.
  • Biological and other chemical reactions are also strongly inhibited. This allows long periods of operation between cleaning periods.
  • the low energy consumption of the system is also of particular advantage.
  • the spraying into the evaporator chamber takes place reasonably close to the surface of the ice pulp collected in the room and at a short distance from the top of the evaporator chamber, where the vapors, after extensive separation of the droplets, and preferably after a passage through a defogger.
  • the selection of a liquid injection according to the invention offers the advantage of particularly effective presentation of the liquid surface in order to achieve rapid evaporation and under-cooling of the droplets. This also avoids the tendency towards ice accumulation in the name of the water inlet, as reported in the literature regarding the hydroconverter's falling film method, at the top of the vessel.
  • the supercooled droplets settle relatively evenly over the entire surface of the ice pulp that collects in the lower part of the evaporator chamber, and the relatively large height of the room above the injection points and the relatively low flow velocity of the vapors in the room ensure this , that a comparatively complete separation of the droplets from the vapors takes place before the vapors are suctioned off, preferably after a further defogging process by means of conventional droplet separating devices.
  • a method for converting low-pressure steam into steam of higher pressure by means of a pressure transformer stage in which the low-pressure steam is mixed in an absorber with absorbent and is absorbed by it, wherein the heat of absorption of coolant, in particular is dissipated by cooling water, and in which the resulting absorption medium, enriched with the liquid supplied by the steam, in particular water, after a pressure reduction by a pump is first heated by heat exchange, and then passed into an expander , in which a steam at higher pressure is generated by the supply of heat.
  • a steam absorption method can also be found in connection with sea water desalination in the above-mentioned literature (KS Spiegier), but without the vapors extracted from the steam expeller part of the absorber system being under pressure and being fed to a further mechanical compression, be it for Purpose of condensing the vapors, and optimizing energy efficiency or for other purposes. On the contrary, the vapors are suctioned off under vacuum.
  • the invention also relates to devices and systems for carrying out and using this method.
  • the invention provides that the steam generated in the expeller compresses higher pressure with the aid of a compressor and the boiler room of the expeller as a heating medium is fed in, which condenses after the condensation heat has been given off and then leaves the expeller.
  • the solution depleted in the expeller with regard to the absorbed steam, in particular water is used in a heat exchanger for heating the steam-enriched solution arriving from the absorber and then fed to the absorber via a throttle valve.
  • the inert gases released in the absorber are preferably collected and drawn off by a vacuum pump.
  • the invention teaches in the above-mentioned respect that between the place where the low-pressure steam is extracted and the mechanical compressor, a pressure transformer is switched, which effects a pre-compression of the steam to be extracted, whereby the specific volume is considerably reduced, and the mechanical compressor Compression of the same mass flow, built correspondingly smaller, and so can be operated with a higher overall efficiency.
  • Precompression is achieved by first mixing the low pressure steam in an absorber with an absorbent, from which the steam is absorbed. At the same time, the heat of absorption released is dissipated by cooling water. The solution enriched with steam (water-rich solution) is then sucked out of the absorber with a solvent pump and pumped to the evaporation pressure.
  • the rich solution is then heated in a heat exchanger and then flows into the steam expeller.
  • the low-pressure steam previously absorbed in the absorber evaporates at the selected higher pressure level.
  • the high pressure steam generated in this way is compressed with a mechanical compressor, its pressure and temperature increase.
  • the steam then penetrates into the expeller's boiler room, condenses there and thereby supplies the heat required for evaporation.
  • the heat contained in the condensate can continue to be used in the process.
  • the solution (poor solution) which is depleted of steam (water) in the expeller is fed into the previously heated heat exchanger, where it cools down and supplies the energy required to heat the rich solution.
  • the poor solution then flows through a throttle valve, undergoes relaxation to the lower absorber pressure, and enters the absorber, which closes the circuit.
  • LiBr, NaOH, Ca (OH) 2 , MgCl 2 , CH 2 NH 2 or CaCl 2 can be used as absorbents.
  • the invention also relates to a method and a device for concentrating or crystallizing aqueous solutions, in particular fruit juices, organic and inorganic acids and salts, as waste water, characterized in that the solution to be concentrated or crystallized is via a nozzle system Evaporation is supplied at which the solution is depressurized to a pressure corresponding to the evaporation temperature of -5 to + 10 ° C, which corresponds to the saturation pressure, so that the solution partially evaporates due to an imbalance caused by a short residence time, and thereby evaporates cools to a low temperature, and is then collected after a sufficiently long dwell time, so that it forms an ice pulp due to an established equilibrium with the other Characterize that the vapors formed under low pressure during evaporation are converted into high pressure vapor by means of a pressure transformer stage of the type described above.
  • the ice slurry is preferably skimmed mechanically from the top region in an enriched form.
  • Another important preferred characteristic is that the evaporation into the evaporator chamber is directed upwards from below the surface of the collecting ice slurry.
  • This characteristic is intended to counteract the tendency of the glands to freeze.
  • the invention also offers devices for Implementation of various aspects of the invention are suitable.
  • a device is characterized by an evaporator required for the production of ice slurry with a container which has a nozzle system in about half, contains a collecting container in the lower part, and is provided with demister in the upper part, and in has its lower part of an ice sludge extraction and conveyor, in particular a screw pump, and facilities for further treatment of the ice slurry are switched.
  • a special version provides a separating device, consisting of a container with an upper and lower tube sheet, into which a bundle of tubes is embedded, which consist of a pure material, such as membrane or mesh, and the lower tube sheet an inlet chamber with an inlet for Recording of the ice pulp and its forwarding is assigned to the Ronroündel, while there is a receiving chamber for the ice-enriched treated ice pulp above the upper tube sheet.
  • a separating device consisting of a container with an upper and lower tube sheet, into which a bundle of tubes is embedded, which consist of a pure material, such as membrane or mesh, and the lower tube sheet an inlet chamber with an inlet for Recording of the ice pulp and its forwarding is assigned to the Ronroündel, while there is a receiving chamber for the ice-enriched treated ice pulp above the upper tube sheet.
  • the freeze evaporator preferably has a device for removing the ice slurry in a region of the evaporator in the vicinity of the surface of the ice slurry in the evaporator.
  • the removal device preferably has a mechanical skimming or wiping device.
  • the hone of the removal device can preferably be adapted to the level of the ice slurry in the evaporator device.
  • the removal device can be set up to drive on the porridge surface. It is a preferred feature that the nozzle device has upwardly directed nozzles below the normal ice level.
  • a pressure transformer is attached, which pre-compresses the vapors drawn off, thereby reducing the specific volume of the vapors.
  • the device is of such a type that the pressure transformer has an absorber in which the low-pressure vapors are mixed with and absorbed by an absorbent, a heat exchanger device for dissipating the heat of absorption, a pump device for taking vapor-enriched absorbent solution from the absorber and forwarding it to a heat exchanger a higher pressure and in a steam expeller to expel the steam under higher pressure from the absorbent.
  • FIG. 1 shows a graphic representation of the principles according to the invention
  • FIG. 2 a process diagram for juice thickening
  • FIG. 4 a process diagram for the concentration of saline water
  • FIG. 5 a process diagram for the production of block and ice mash
  • FIG. 6 shows a process diagram of a pressure transformer, as can be used for example in the thickening of fruit juice or chemicals dissolved in water under triple point conditions, or for the production of ice or ice pulp, for example for cooling purposes.
  • FIG. 7 a process diagram for a complete plant for the production of an ice pulp for cooling purposes, including some of the characteristics described in connection with FIG. 5 and in combination with FIG. 6.
  • Figure 1 shows some of the principles of the invention in a graphical representation.
  • the ordinate P represents the pressure and the Abzissae SV the specific volume.
  • the curve a, b never represents the van der Waalsche status line, consisting of the settling line a of the aqueous liquid, which rises to a maximum, represented by the critical point e, beyond which it becomes the dew line b.
  • Another curve shows the states which are passed through by the aqueous liquid during the process, including point f, namely the state of the solution before entering the spray nozzles, from which the aqueous solution is injected into the evaporator, while part c of the curve shows the Represents the state of the droplets inside the evaporator.
  • the dashed horizontal line represents the triple point pressure.
  • FIGS. 2 and 3 show a diagram of the process principles for the thickening of juice in a process according to the invention.
  • 1 represents the evaporator, in the form of a cylindrical container under reduced pressure.
  • the injection system 2 which is supplied with the juice to be concentrated through a line 3 by means of the juice pump 4.
  • the fresh juice is cooled in a juice cooler 5 in countercurrent to the melted ice and vapor condensate in a manner to be described below, and pressed through the nozzle system 2 by the pump 4.
  • the nozzles 6 of the nozzle system 2 convert the juice into fine drops 7, which enter the evaporator at high speed.
  • a reduced pressure is set in the evaporator, which theoretically corresponds to the triple point pressure of the solution to be thickened. Due to the short residence time of the drops, however, the equilibrium state of the triple point in the liquid jets 7 is not reached. Rather, there is a lively evaporation of the drops with strong hypothermia, which initially does not result in ice formation. For the formation of the disease, critical illnesses are necessary, which cannot be achieved due to the short dwell time (a few hundredths of a second). The state change during the flight time of the droplets never takes place along the van der Waals state line without reaching equilibrium, as shown in FIG. 1.
  • the nozzle system 2 is located in a manner far below the top of the vessel 1, where the vapors are suctioned off, preferably at least 1.5 m below the droplet separator 29 and even better 1.8 to 3 m.
  • the nozzles are quite close to the surface of the ice pulp, e.g. not more than about 2 m, in order to nevertheless provide a sufficient residence time for the evaporation. This distance can be significantly reduced, e.g. to less than 1.5 m if the nozzles are designed in such a way that wide-angle spraying takes place.
  • the drops 7 are collected in the evaporator sump. There will be the strong one through a sufficient stay Hypothermia is reduced by the formation of ice.
  • the ice slurry produced in this way enters the separating apparatus 10 via a screw pump 9, which removes a bundle of perforated or porous tubes or plates 12.
  • the tubes can also consist of wound screen mesh or supported separation membranes.
  • the thickened product (juice) 13 migrates into the outer space of the separating apparatus 10, formed by a jacket 14, and is there at 15 deducted.
  • the ice content in the flow direction increases in the tubes, and then the ice reaches an equalization space 15, formed by a tube sheet 17 above the tubes 12, for the purpose of speed compensation.
  • the ice is then washed in a washing column, which works in a similar way to the separating apparatus 10, in countercurrent to the melt water formed by the melting of the ice in the upper part of the device.
  • the washing column has perforated or porous tubes 19, similar to the tubes 12 of the separating apparatus 10. This melt water serves as washing water and, with a low product content, passes through perforated tubes 19 of the washing column 18 into the outer space 20 of the washing column, filtered by the jacket 21, and wi rd then added through the outlet 22 and at the pipe connection 23 to the pre-cooled fresh juice before entering the pump 4.
  • the ice enters the impermeable tubes 24 of the melting condenser 25, which is located in the material flow with and on the washing column 18, and liquefies by absorbing heat from the steam 26, which previously came from the evaporator 1 via a droplet separator or Demi ster 29 with the help of a compressor 27 to reduce the pressure within the evaporator 1 and to compress the vapors 26 to a higher pressure of the evaporated steam 28, which in the Melting condenser 25 enters through the nozzle 30, has been compressed.
  • the condensate 31 of this steam is withdrawn from the melting condenser 25 through a nozzle 32, and conveyed by a pump 33 and added to the melted ice in the mixing chamber or mixing chamber 34.
  • This mixing chamber 34 is constructed above and in the material flow of the melting condenser 25 and separates it from the juice artist above the mixing chamber 34.
  • the condensate is used in the juice cooler 5 to cool the fresh juice.
  • the washing device ie the washing column 18, is separated from the melting condenser 25 by a tube plate 35 common to the tubes 19 and 24.
  • the detail X in FIG. 2, which shows the relationship between the melting condenser and the washing column and the principle of action of the washing column, is shown in FIG. 3.
  • the melt water serving as washing liquid is schematically represented by the meandering lines and arrows 36.
  • the juice cooler 5 has a casing 37 with inlet and outlet ports 38 and 39 for the fresh juice delivered by the feed pump 40.
  • the cooler also has a bundle of vertical cooling tubes 41, through which the contents of the mixing chamber 34, which in the meantime have largely melted, migrate upward into a collecting chamber 42. This represents the top part of the device, of which the separator 10 forms the bottom part. Now that most of the cold has been released into the fresh juice, the water 43 is discharged through the water outlet 44.
  • the following example is intended to give you an impression of the size of the operator in the case of apple juice thickening.
  • FIG. 4 shows a performance example for the concentration S a l z h a l t i g e r W a w s e r w i e A w a w s e r a u s flue gas desulfurization plants, mine water or cooling tower blowdown water.
  • the same reference numbers are used to designate the same or essentially the same parts as those according to FIGS. 2 and 3.
  • the nozzle 38 becomes an inlet for raw water
  • the juice cooler 37 becomes a raw water cooler
  • the line 3 for fresh juice now conveys pre-cooled water.
  • the ice pulp 11 'in the present case differs from the ice pulp 11 which accumulates in the collecting space 8 of FIG. 2 in that it also contains salt crystals.
  • the ice pulp 11 "from the evaporator 1 is conveyed in the case of FIG. 4 by the screw pump 9 into a hydrocyclone 50. There, the precipitated solids are drawn off at 51 with the concentrate.
  • a centrifuge can advantageously be used, in particular The brine 15 'separated in the separating apparatus 10 is returned together with the washing water 36 into the area 8 of the evaporator 1. The other process steps remain as shown in FIG. 2 and described with reference to it.
  • FIG. 5 Another application is the production of ice pulp and block eggs for cooling or egg production.
  • the corresponding process scheme is shown in FIG. 5. Again, the same reference numerals apply to the designation of parts that are identical or essentially identical to those in FIGS. 2 and 3.
  • the raw water 38 ' is mixed with make-up water 38 "(see later) and passes through the nozzle system 2 into the evaporator 1, which works according to the same principle as shown in FIGS. 2 and 3. In this case, however, the steam produced can no longer be obtained from the egg
  • the steam 26 is drawn in and earned by a multi-stage compressor 27 'via the droplet separator (demister) 29.
  • cooling water 52 is injected into the steam stream, to reduce the specific volume and thereby to achieve a lower workload.
  • a part 28 'of the compressed steam 28 is re-condensed in the condenser 53 and after softening at 54 is used again as injection water 52.
  • the larger part 28 "of the steam is experienced by a Steam jet pump 55, driven by working steam 56, and is injected at 57 into a spray condenser 58 .
  • the final pressure is selected so that the steam in the subsequent spray condenser 58 can condense on cooling water 59, which is supplied by a cooling tower 60.
  • the inert gases 61 leave the condenser 58 via a vacuum pump 62, which is followed by a smaller condenser 63 for the condensation of the residual steam.
  • the ice pulp 11 removed from the evaporator 1 via the screw pump 9 is freed of the brine 15 ′′ in the separating apparatus 10 and produces the egg pulp for the eventuality
  • the brine 15 "from the separating apparatus is partly sent back to the evaporator 1 at 64 and partly used for cooling the condensers 53, 63 for generating injection water 52 and residual steam condensation from the inert gases 61.
  • the residual water, (press water) 69 is used in this case for the cooling of the condensers 53, 63 for injection water and inert gases (dashed line) Brine 15 "emerging from the separator is then entirely returned to the evaporator 1 at 64.
  • the additional water 38 is required for the case if the raw water 38 'absorbs salts in upstream systems.
  • the energy requirement of the system according to FIG. 5 was calculated to be about 60 kJ / kg, ie only 25% of the value of conventional systems for ice cream production lung.
  • the ice pulp is intended as a final product for cooling purposes, in order to be pumpable, such a pulp must have an ice to liquid phase content of more than 50:50, in particular between 50:50 and 80:20, preferably about 70: Own 30.
  • the slurry enriched in this way can be pumped to where cooling is required, e.g. for environmental cooling in underground mining.
  • this method offers the advantage that the volume of the ice cream concentrate that has to be pumped in to a given location for a required cooling capacity corresponds to only a small fraction of the volume of cooling water that one can use for the same Purpose should have pumped.
  • Figure 6 shows the principle of the use of a pressure transformer according to the invention for converting low-pressure steam into steam at higher pressure, in particular for the purpose of reducing the size and thus improving the energy efficiency of compressor systems 27, 27 'as used in the examples in FIGS. 1 to 5.
  • the vapor space 101 of a triple point evaporator (for example an evaporator as described with reference to FIGS. 1 to 5) and which serves as a freezing system 102 is connected to the absorption space 104 via a pipeline 103.
  • This is a falling film absorber in a tube bundle design.
  • the poor absorbent solution (with low water content) flows, delivered via a line 121 through distribution caps, not shown, which ensure uniform wetting, on the inside of the tubes 106 of the absorber (104 to 108) down.
  • the resulting large surface area at high flow velocity absorbs the steam inside the absorber, so that a negative pressure is created and additional steam is thereby sucked out of the freezer 101.
  • the heat released during absorption is removed by cooling water which flows through the jacket space of the absorber 104 (arrows 107).
  • The, water-rich, absorbent solution flows from the lower opening of the tubes 106 into the sump 108 and is sucked off there by a pump 109. If there are inert gases that are not absorbed by the absorbent, they can be sucked off by a vacuum pump 110.
  • Solution pump 109 sucked rich solution is pumped to the desired evaporation pressure and then heated in a tube bundle heat exchanger 111. It then flows into the steam expeller 112, which is designed as a film evaporator in a tube bundle design with tubes 113.
  • the rich solution flows downwards on the inside of the tubes 113 in a falling film, as a result of which water from the medium water enriched on the inside of the Ronre 113 Absorbent solution partially evaporated and this water is withdrawn at 114 as steam of higher pressure.
  • This vapor of higher pressure is passed through a vapor compressor 115 and is fed at 116 to the top of the casing space around the ring 113 so that the previously vaporized and compressed vapors condense on the outside of the tubes 113. Due to this construction and operating mode, it is possible to work with very low temperature differences and high heat transfer coefficients.
  • the condensate of the compressed steam collects on the lower tube plate 117 in the jacket space and is drawn off at 118. His remaining energy can be used elsewhere in the process.
  • area I on the left side of the dash-dotted line A represents the pressure transformer stage according to the invention.
  • Area II on the right side of line A represents the part of the system with the mechanical compressor 15, the size of which to improve the overall thermal efficiency of the process intended for area II.
  • the area II includes a precaution, since the switch to the triple point evaporator 102, e.g. the evaporator 1 in Figure 5, which is supplied by a Ronwasserpump 123 with raw water via a line 124. If necessary, this Ronwasser can be supplemented with additional water (not shown).
  • the water is injected through nozzles of a spray system 125 into the interior of the evaporator 102, which is kept under low pressure by the negative pressure formed in the region I, as a result of which partial evaporation of the droplets formed in the spray system 125 occurs.
  • the low pressure nozzles formed represent the vapors which are withdrawn from the vapor space 101 through the line 103.
  • the evaporation causes hypothermia of the droplets below the freezing aperture, and partial freezing takes place in the sump 126 of the evaporator 102.
  • This ice slurry in the aqueous concentrate is drawn off at 127 for further use and processing, e.g. in a further detail for FIGS. 1 to 5 described.
  • water for the production of an ice pulp for cooling purposes is withdrawn from a water reservoir 150 and first pumped through a pre-cooling tower 151 and pressed from there by means of a pump 152 and via a down pipe 153 into the spray system 2, which has spray nozzles 6 directed upwards, to avoid pressure losses which are attached just below the top of the ice slurry 11 contained in the sump of the freeze evaporator 1. Since the pump 152 is designed to supply the pipe water 38 'with a constant delivery rate, which often exceeds the supply consumption of the spray system 2, a bypass pipe 154 is also provided, whereby the menranfall of water is returned to the reservoir 150.
  • ice scooping device 156 which floats on the surface of the ice pulp, and the hone of which is thus in a fixed ratio to the ice brewing level in the device, this level being monitored by a control device 157.
  • Ice pulp 11 which accumulates in the bottom part of the evaporator, is subject during its dwell time to a partial separation of gravity into ice particles which float upwards and the liquid phase which sinks under gravity and which, together with suspended and precipitated solids, accumulates in the liquid phase in the downpipe 158, the bottom End has a drain valve 159 through which solid precipitates can be removed as sludge at intervals.
  • Concentrated egg pulp is skimmed off by mechanical stripping devices as part of the skimming device 156 from the surface of the egg pulp into the hopper of the skimming device 156 and arrives from there through a flexible line 160 and the tube 161 into the centrifugal ice concentrator 50 'from where a concentrated ice slurry is drawn off through line 122 to the screw pump 9 and is conveyed from there in the direction of arrow 163 to any location where cooling is to be carried out, for example in the sam mena ng mit t u terta ge be r gba u. D ieim
  • Centrifugal ice separator liquid phase is withdrawn through a pipe 164 by means of a pump 165 and fed to a further nozzle system 2 ', which is also equipped with upwardly directed spray nozzles below the surface of the ice slurry in the evaporator.
  • the nozzles of the spray systems 2 and 2 'thus spray an upward sprinkling of water and brine into the evaporator chamber 1.
  • the nozzles are about 10 to 100 mm below the surface.
  • the arrangement of the nozzles below the surface of the ice slurry counteracts the tendency of the nozzles to freeze, and the upward spraying also somewhat extends the floating time of the droplets in the vacuum space.
  • the falling, cooled droplets have a lower solute content than that of the liquid pnase in the ice pulp and thus partially prewash the ice concentrate.
  • Redirection devices 167 serve to bypass the cyclone or the centrifuge in the start-up phase of the system before ice has formed, or to redirect the liquid phase into the bottom of the evaporator without being passed through the spray system 2 '.
  • Coolant lines 107 which lead from a condenser tower 107 'and back again, are used to cool the pipes 106 of the absorber.
  • the water-enriched absorption medium solution is fed by a pump 109 to a first heat exchanger 111 ', where it is heated by hot, low-water absorption medium solution, which is extracted from the sump 119 of the steam expeller 112 via a line 110. It absorbs further heat in a second heat exchanger 111 ′′, supplied by the compressed vapors and the condensate, which are passed through the jacket surrounding the steam discharge pipes 113. This condensate, with a low content of total dissolved solids, is added partial release of its heat content in the heat exchanger 111 "through the line 121 'is returned to the water reservoir 150 for reuse in the process.
  • the steam chamber 108 'of the sump 108 of the absorber at 171 removed water vapor passes into a cold trap 110', which is evacuated via a venting element 110 "by a liquid vacuum pump 110.
  • the heat exchange tubes of the cold trap 110 are cooled by cold liquid phase which was withdrawn from the downpipe 153 of the evaporator via the pump 172 and a line 173 and, after passing through the cooling trap at 174, enters a heat exchanger 175 and from there through line 176 of a conductivity tsmess réelle 178 and a signal transmitter 179 monitored three-way control elements 177.
  • the liquid is returned to the bottom of the evaporator via a nozzle 180 directed downwards a mixture in the egg pulp and washes solid Precipitation from the inclined sump wall down and down into the downpipe 158, where it is finally drawn off through the valve 159.
  • a signal emitted by the device 178, 179 causes the liquid to be discharged via the three-way valve 177 via a waste water line 181 for disposal.
  • the wastewater volume derived at 181 represents only a very small percentage of the total amount used of the aqueous liquid extracted from the reservoir 150.
  • Cooling liquid for the pump 110 is circulated by a pump 182.
  • the vapors expelled by heating from the absorbent solution in the runners 113 collect in the steam space 119 'above the liquid level kept constant in the sump 119 by means of the circulation line 120' and the monitoring devices 120 ", which level is thereby maintained is that, as required, liquid is returned from line 120, which draws water-free absorbent solution from sump 119 via pump 183 and passes back through heat exchanger 111 "via line 121 into the absorber.
  • the vapors in the space 119 'of the sump 119 enter the suction side 184 of a multi-stage compressor 115 through a defogger element 119 ".
  • Cooling water which is removed from the sump of the cold trap 110" via a condensate pump 185, is controlled to a controlled extent by means of the spray devices 52 the stages of the multi-stage compressor injected.
  • the extent of the injection can optionally be controlled by a control element 186 controlled by a guide plate, and excess cooling water is returned via line 187 to cold trap 110 '.
  • Part of the cooling water is injected at 188 for injection into the labyrinth seal on the top of the compressor, below the gear 189 to improve the seal.

Abstract

Un procédé et dispositif pour le traitement à phase multiple d'un liquide aqueux, dans lequel un liquide aqueux (38') pré-refroide (151) est transformé en fraisil dans des conditions en trois points, pour injection dans une chambre de condensation (1) soumise à un vide partiel; les gouttelettes (7) sont surrefroidies par évaporation partielle et sont recueillies sous forme de fraisil dans le collecteur (8) de la chambre. Le fraisil est traité selon l'application prévue, notamment concentration de jus de fruits ou de produits chimiques, traitement des eaux usées ou conversion du fraisil en blocs de glace ou en un fraisil concentré, pouvant être pompé. (163), contenant environ 70% de glace pour le refroidissement, notamment dans des mines souterraines. L'efficacité thermique est également améliorée par le fait que la vapeur basse pression (26, 103), après extraction, de la chambre de condensation (1), est transformée en vapeur haute pression (119') dans une phase de conversion de la pression par absorption (104-108) suivie de désorption (112) par chauffage à haute pression, et de compression mécanique (115) ainsi que de condensation (113, 111').
EP86903339A 1985-05-20 1986-05-17 Procede et dispositif pour le traitement a phase multiple des liquides aqueux Withdrawn EP0226605A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
ZA853772 1985-05-20
ZA853772 1985-05-20
ZA86192 1986-01-10
ZA860192 1986-01-10

Publications (1)

Publication Number Publication Date
EP0226605A1 true EP0226605A1 (fr) 1987-07-01

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Application Number Title Priority Date Filing Date
EP86903339A Withdrawn EP0226605A1 (fr) 1985-05-20 1986-05-17 Procede et dispositif pour le traitement a phase multiple des liquides aqueux

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EP (1) EP0226605A1 (fr)
WO (1) WO1986006977A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4654064A (en) * 1986-01-31 1987-03-31 Cheng Chen Yen Primary refrigerant eutectic freezing process [PREUF Process]
DE3739839A1 (de) * 1987-11-24 1989-06-08 Gea Wiegand Gmbh Verfahren zur herstellung von blockeis
FR2649620B1 (fr) * 1989-07-17 1991-10-25 Richelmy Xavier Installation et procede mixte de production d'un solute et de refroidissement d'une enceinte a partir d'un fluide principal compose d'un solvant et d'un solute

Family Cites Families (9)

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Publication number Priority date Publication date Assignee Title
FR1215936A (fr) * 1955-06-28 1960-04-21 Carrier Corp Procédé et dispositif rendant potable l'eau salée
US3121626A (en) * 1955-10-18 1964-02-18 Zarchin Alexander Apparatus for sweetening water
US3049889A (en) * 1958-01-02 1962-08-21 Carrier Corp Method and apparatus for rendering brine solution potable
US3070969A (en) * 1960-07-11 1963-01-01 Carrier Corp Separation systems
GB1024573A (en) * 1961-04-14 1966-03-30 Desalination Plants Methods and systems for separating a solvent from a solution
US3443393A (en) * 1967-01-17 1969-05-13 Moise Levy Goldberg Triple point desalination system utilizing a single low pressure vessel and a gravity sea water feed
US3664145A (en) * 1969-10-13 1972-05-23 Wallace E Johnson Vacuum-freezing, ejector absorption solution separation systems and methods
US4236382A (en) * 1979-02-26 1980-12-02 Cheng Chen Yen Separation of an aqueous solution by the improved vacuum freezing high pressure ice melting process
US4314455A (en) * 1980-06-16 1982-02-09 Chicago Bridge & Iron Company Freeze concentration apparatus and process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO8606977A1 *

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