DISTILLATION

Abstract: A method and an apparatus for distillation of a liquid near or above the critical point of the liquid, wherein the liquid is fed to a separation zone (32) in which a temperature profile rising from a liquid inlet to a vapour outlet is provided in a predominant part of the separation zone, said liquid assuming in said temperature profile a temperature near or above the critical temperature of the liquid, and residue (53) is withdrawn immediately below the liquid surface (45) in the separation zone (32). The method and the apparatus are useful for desalination of salt water and for purification/heat treatment of waste water from industry and agriculture.

Description: Distillation 1. BACKGROUND OF THE INVENTION Technical Field The present invention concerns a method and an apparatus for distillation of a liquid near or above the critical point of the liquid, particularly for use in desalination of salt water, purification and/or pressure-heat treatment of organically tainted waste water from industry and agriculture. Liquid such as saline drinking water can be purified of solid substances using distillation by retaining the non¬ volatile substances of the liquid as a residue in the distillation container and allowing the vapour, which evaporates from the liquid, to pass into the condensation part, in which it is condensed as a distillate possibly containing volatile substances and the components of the air dissolved therein. Evaporation of the vapour from the liquid comprises a phase shift from liquid to vapour, just as the conden¬ sation of the vapour from vapour to liquid comprises a phase shift from vapour to liquid, both of which being driven by forces which are caused by differences in pressure, temperature or concentration above a liquid- vapour interface. At pressures and temperatures below the critical point of the liquid, the liquid may be brought from liquid phase to vapour phase at a constant tempera¬ ture by addition of the necessary evaporation heat. However, at pressures and temperatures above the critical point this phase shift can take place without addition of heat, because the evaporation heat at these super critical pressure and temperature conditions is zero. As a case in point it may be mentioned that the evaporation heat is 2257 kJ for 1 kg of water at 1 atm and 100 °C, whereas it is 0 kJ at the critical point at 221,20 bars and 374.15 °C. "Distillation below the Critical Point" To obtain optimum energy utilization in distillation of a liquid below the critical point, it is known to heat the liquid using the energy, including the evaporation heat, available in the vapour. It is known from e.g. "Principles of Distillation", Part A and B, Editors K.S. Spiegler and A.D.K. Laird, Academic Press Inc., 1980, New York to perform distillation by thermal single- or multi-step evaporation processes, in which the energy available in the discharge currents of distillate and residue contributes to heating the feed stream. For such processes the driving force is provided for the heat transfer by a temperature difference between the discharge streams and the feed stream, which is sub¬ stantially established by lowering the vapour pressure of the liquid. It is moreover known. Ibid, to perform distillation of a liquid by evaporation processes in which a temperature difference between the discharge streams and the feed stream is established by condensing and cooling the vapour from a compressed state, thereby creating a higher vapour pressure for the liquid. A common drawback of these evaporation processes is that they all require addition of evaporation heat, and that reuse of the added energy requires difficult and cumbersome multi-step processes or vapour compression processes, the latter requiring compressors which, frequently with low efficiencies, are to be capable of compressing large volumes of vapour at relatively low pressures. Another drawback is that it is not certain that the distillate is sterile. Accordingly, there is a need for a liquid distillation technique wherein a lower energy consumption is achieved than by the heretofore known methods, while ensuring that the distillate is sterile. "Distillation above the Critical Point" It is known to separate solid, non-volatile substances from a solution in a liquid by evaporating and distilling the liquid at pressures and temperatures exceeding the critical pressure and the critical temperature of the liquid, wherein - a lower energy consumption is achieved than by heretofore known techniques, while ensuring that the distillate is sterile, - the necessity of recovering the evaporation heat is obviated, and - the necessity of compressing vapour or using multi step heat exchanging processes in order to reuse the energy available in the vapour is obviated. According to the prior art a liquid is distilled near or above the critical point of the liquid by a) feeding the liquid to a heat exchanger in which it is heated, and then b) conveying the heated liquid to a separator to which a pressure is applied so that the liquid is brought to a state near or above the critical point, whereby it undergoes a phase shift forming a vapour phase and a liquid residue which are separated by a liquid surface, and then c) the vapour under phase shift to liquid and the residue are discharged as a distillate and a residue, respectively, such that they release their heat to the liquid in the heat exchanger, thereby heating the liquid. Specifically it is known to use this technique in connection with crystalization of salt from an achieved saline residue. A drawback of this prior art is that the distillation is unstable so that overflow of saline residue to the distillate may occur. Prior Art Patent Literature US Patent Specification 1204716 describes a method of evaporation and distillation of liquids at pressures and temperatures which correspond to. pr are near the critical point of the liquid. US Patent Specification 2520186 describes a process for separating solid non-volatile substances from a solution in a liquid at pressures and temperatures which exceed the critical pressure and the critical temperature of the liquid. US Patent Specification 3361647 describes a method and an apparatus for crystallizing salt from a brine by establishing a pressure and a temperature in the brine which are above the critical pressure and the critical temperature of pure water, and which are sufficient to cause phase separation between a salt-lean vapour phase and salt-rich liquid phase, from which a portion is passed on for separation of salt in crystallization chamber. US Patent Specification 3477918 describes a vapour compression distillation process for recovery of purified water from a solution of water and dissolved substances by vapour compression at 80-200 atm. A drawback of the prior art according to the above- mentioned patent specifications is that they are too unstable and ineffective for use in industrial processes. 2. DESCRIPTION OF THE INVENTION Object of the Invention An object of the present invention is to provide a method and an apparatus for distillation of a liquid near or above the critical point of the liquid which are more efficient and reliable in operation than the heretofore known techniques. Another object of the present invention is to provide such a method and such an apparatus for distillation, particu¬ larly for desalination of salt water and for heat-pressure treatment of the water, in particularly organically tainted waste water from industry and agriculture, which can be realized in a compact system having small physical dimensions. Solutions according to the Invention "Method of Super Critical Distillation" These objects are achieved according the invention by providing a method of distilling of a liquid near or above the critical point of the liquid, wherein a) the liquid is fed to a heating zone in which it is heated, and then b) the heated liquid is conveyed to a separation zone to which a pressure is applied such that the liquid is brought to a state near or above the critical point, whereby it undergoes a phase shift forming a vapour phase and a liquid residue which are separated by a liquid surface, and then c) the temperature of the vapour in the vapour phase is raised, and d) the vapour phase-shifted from vapour to liquid and the residue are discharged as a distillate and a residue, respectively, such that they release their heat to the liquid in the heating zone, thereby heating the liquid, said method being characterized by providing in a predominant part of the separation zone a temperature profile which increases from a liquid inlet to a vapour outlet and in which the liquid assumes a temperature near or above the critical temperature of the liquid, and withdrawing the residue immediately below the liquid surface in the separation zone. "Apparatus for Super Critical Distillation" These objects are moreover achieved by providing an apparatus for distillation of liquid near or above the critical point of the liquid, comprising a) a separator, b) a heat exchanger, c) means for feeding liquid to the heat exchanger, d) means for heating liquid and vapour in the separator, e) means for discharging the vapour and the residue, respectively, from the separator, and f) pumps for pumping-in the liquid and pumping out the vapour and the residue, respectively, said liquid feeding means and heating means being adapted to establish such a pressure and such a temperature in the separator that the liquid and the vapour in it are present near or above the critical point, and said vapour and residue discharging means discharging the vapour and the residue in the separator via the heat exchanger in which the vapour is converted to a distillate, said apparatus being characterized in that heating means are provided in connection with a predominant part of the separation section, said heating means being adapted to establish a rising temperature profile from a liquid inlet to a vapour outlet in the separation section, and that the outlet for the residue discharging means in the separation section is positioned immediately below the liquid surface between the vapour and the residue. Effects According to the Invention By proving in a predominant part of the separation zone a temperature profile which increases from a liquid inlet to a vapour outlet and in which the liquid assumes a temperature near or above the critical temperature of the liquid, it is achieved i) that the liquid in the separation zone is heated such that temperatures above the critical temperature exist from an area in the liquid along the increasing temperature profile, in which area the liquid is present in a super critical state and therefore undergoes a phase shift forming, without an increase in volume, a vapour phase which is not capable of carrying solid matter or is just capable of carrying little solid matter, ii) that a liquid surface is formed between the super critical vapour phase and the liquid, which is sub- critical, said liquid surface separating the solid- lean vapour phase from the solid-rich liquid phase, the residue, the position of said liquid surface depending upon the concentration of dissolved matter in addition to pressure and temperature. Furthermore, by withdrawing the residue immediately below the liquid surface in the separation zone it is achieved iii) that the liquid surface does not move, thereby ensuring that the distillation can be performed in a stable manner without residue being entrained in the distillate. This effect can be illustrated by the following non- limiting explanation as an increase of the critical point of the residue which is analogous with the boiling point increase of e.g. salt solutions. If it is imagined that the outlet of the residue is positioned too far down in the liquid below the liquid surface, this entails that a sufficient amount of solid is not discharged with the residue to keep the solid concentration below the liquid surface at its equilibrium concentration at the pressure and temperature concerned. The solid concentration would be too great for the available liquid to be able to carry the additional solid. To reduce the solid concentration to its equilibrium concentration the liquid therefore does not release so much vapour to the vapour phase, which results in a rising liquid surface. It has thus been found by tests that when the residue outlet is positioned too far down in the liquid below the liquid surface, the liquid surface can rise so much that the residue flows out through the distillate pipe. Conversely, when the residue outlet is positioned too high in the vapour phase with respect to the liquid surface, this rises until this is just above the pipe. Thus, according to the invention it is ensured that the separation of the distillate and residue is stable without overflow of residue into the distillate, thereby ensuring a reliable function in operation. Moreover, when the residue is withdrawn in accordance with invention, the residue is discharged with the greatest possible concentration of solid, thereby providing an efficient distillation process. Preferred Embodiments of the Method To achieve additional advantages it is preferred that the distillation process according to the invention is performed according to the following preferred embodiments. In a preferred embodiment of the method the temperature of the vapour in the vapour phase is raised by adding heat in an area of the separation zone which is situated at a relatively great distance from the area of the separation zone in which the residue is withdrawn, thereby ensuring that the liquid surface is above the residue outlet and not completely or partly in the vapour phase. In another preferred embodiment the temperature of the vapour in the vapour phase is raised by either - heating the vapour by addition of heat to it within the separation zone, - heating the vapour by addition of heat to it outside and into the separation zone, or - withdrawing the vapour from the separation zone and heating the withdrawn vapour, thereby ensuring that the heat consumed by the distillation is just to be added at one location, viz. at the location where the vapour in the vapour phase is heated, and that the heat here is added through the vapour such that liquid drops are not carried over in the vapour phase. It is moreover ensured that possible liquid drops with a great content of solid are dried, so that these are forced to fall back on the liquid surface because of gravitation or a centrifugal force. In yet another preferred embodiment the last part of the separation zone is a cyclone zone in which the liquid surface assumes a parabolic-like shape, thereby making it possible to provide a great centrifugal force enabling a compact system with small physical dimensions to be realized. In yet another preferred embodiment the last part of the separation zone is a separatory funnel zone. In a preferred embodiment, particularly in the embodiment in which the last of the separation zone is a cyclone zone or a separatory funnel zone, the temperature of the vapour in the vapour phase is raised by heating the vapour by addition of heat to it inside a helical course of the predominant part of the separation zone, thereby achieving that both the formed vapour, possible drops and the liquid are effected by a centrifugal force which separates the vapour and the liquid from each other and ensures that residue-containing drops, if any, are preferably forced into the liquid phase. In a preferred embodiment the liquid is fed in the bottom of the separation zone, thereby making it possible to realize a simple method utilizing gravitation to separate the vapour phase and the residue phase. For a great part of the added thermal energy to be reused, in particular for heating the added liquid, the distillate and the residue, respectively, are preferably discharged such that they release their heat to the liquid in the heating zone, individually or both at the same time. The heat from the vapour and the residue may optionally be used for other purposes than heating the liquid, e.g. in connection with heating in other process steps, where this is expedient. Preferred Embodiment of the Apparatus In a preferred embodiment the apparatus comprises reci- procating pumps with displacement means, such as pistons or diaphragms for liquid, residue and distillate, respectively, which are characterized in that each of the pumping-out cylinders associated with the residue dis¬ placement means and the distillate displacement means communicates with an outlet valve and a slide valve, which are controlled by the piston movement such that the slide valve shuts off discharge of liquid to a discharge conduit when the piston has reached a position before its top position, and opens the outlet valve when the pressures above it are comparable, thereby achieving - that pressure surges in the system are prevented, - the outlet valve is relieved of the great pressure differences, and - that the valve has a long life, because cavitation corrosion is thereby prevented. In a preferred embodiment the control of the piston movement is additionally such that the slide valve shuts off admission of liquid from the outlet valve when the piston has reached a position before its bottom postion and allows discharge of liquid to the discharge conduit when the pressures above it are comparable, which likewise imparts a long life to the valve, because cavitation corrosion is thereby prevented. In a preferred embodiment, the pumping-in cylinder associated with the liquid displacement means communicates with an exhaust valve to which a relief valve is coupled, said relief valve being set to open when the pressure in the system exceeds a desired pressure, thereby ensuring - that the same amount is always pumped in as is pumped out, irrespective of dissolved gasses and differences in coefficients of expansion, - that the pressure is kept constant, such that the system is not subjected to e.g. harmful pressures ' , and - the energy is not lost at a greater pumping-in stroke volume. In a preferred embodiment a heat source feeds heat to the separation section inside it, outside and into it, or the vapour discharge means include a section outside the separation section which is heated by a heat source. In a preferred embodiment the last part of the separation section is a cyclone or a separatory funnel. In a preferred embodiment, in particularly the one in which the last part of the separation section is a cyclone or a separatory funnel, a heat source for addition of heat to the separation section is positioned radially within a helical course of the predominant part of the separation section, thereby achieving that both the formed vapour possible drops and the liquid are affected by a centri¬ fugal force which separates the vapour and the liquid from each other and ensures that residue-containing drops, if any, are preferably forced into the liquid phase. In a preferred embodiment the liquid feeding means feeds the liquid in the bottom of the separation section. Definition of Expressions By the expression "distillation" is meant in the sense of the invention a combination of first a phase shift from liquid to vapour and then a subsequent phase shift from vapour to liquid, in which a liquid comprising a solution of substances can be separated in one or more fractions. If no residue is withdrawn, or if the residue constitutes a very small portion with respect to the distillate, this means a "heat pressure treatment" in the sense of the invention. By the expression "solid" is meant in the sense of the invention insoluble as well as soluble substances, such as insoluble and soluble organic and inorganic substances which are retained in the residue at the given conditions of distillation. 3. BRIEF DESCRIPTION OF DRAWINGS The invention will be explained more fully below with reference to the drawings, in which Fig. 1A shows a flow diagram for a conventional distillation apparatus utilizing vapour compression according to the prior art, fig. IB shows a T,S diagram of the distillation apparatus of fig. 1A and according to the invention. fig. 2A shows a flow diagram for a distillation apparatus utilizing water compression according to the invention, fig. 2B shows a t,h diagram of the water-vapour system at pressures around the critical point, fig. 2C shows isobar solubility diagrams of NaCl in the water-vapour system around the critical point, fig. 3A shows a desalination apparatus according to the invention, fig. 3B shows an embodiment of the apparatus of fig. 3A, fig. 3C shows another embodiment of the apparatus of fig. 3A, fig. 4 shows an enlarged section of the pumping device A, fig. 5 shows an enlarged section of the withdrawal device C, fig. 6 shows an enlarged section of the separator, fig. 7 shows the desalination apparatus of fig. 3A and fig. 3B equipped with a pulsator, fig. 8 shows the desalination apparatus of fig. 3A and fig. 3B equipped with a cyclone, fig. 9 shows the desalination apparatus of fig. 8 where the cyclone is replaced by a filter, fig. 10 shows another embodiment of a desalination heat- pressure treatment apparatus provided with a vapour compressor and a sludge trap, fig. 11 shows an enlarged section of the pumping device A of fig. 10, fig. 12 shows an enlarged section of the vapour compressor of fig. 11, fig. 13A shows a heat-pressure treatment apparatus according to the invention, fig. 13B shows another embodiment of the apparatus of fig. 13A, fig. 14A shows a preferred embodiment of the separation section with a cyclone, fig. 14B shows a cross-section of the embodiment of fig. 14A, and fig- 15A shows a preferred embodiment of the separation section with a separatory funnel, fig. 15B shows a cross-section of the embodiment of fig. 14A. 4 DETAILED DESCRIPTION Distillation with Vapour Compression (according to the prior art) Fig. 1A shows a flow diagram of a conventional distilla¬ tion with vapour compression according to the prior art. A feed stream 10 feeds liquid via a 3-stream heat exchanger 20 and an optional auxiliary heat exchanger 21 to an evaporator condenser 30 where liquid is evaporated, optionally by boiling. The vapour is compressed in a compressor 50 so that the difference between the satura¬ tion temperature of the liquid in the compressed and non- compressed vapour is greater than the heat transfer temperature difference between the liquid and the vapour in the evaporator condenser 30. Fig. IB shows a T,S diagram, from which it appears that compression work is to be performed on the vapour from P 1 to P to raise the temperature from T., to T 2 . Distillation of Liquid with Water Compression (according to the invention) Fig. 2A shows a flow diagram of distillation with water compression according to the invention. A feed stream 10 is fed via a water pump 20A to a heating zone 31 in which it is heated and from which the heated liquid is fed to a separation zone 32, to which pressure and temperature are applied such that the liquid in the separation zone is in a super critical state, and in which it undergoes a phase shift forming a water phase 43 and liquid residue 53 which are separated by a liquid surface 45 and are discharged via pressure valves 20B and 20C. As appears from fig. IB and fig. 2B, it is achieved at an isobar P above the critical pressure P that addition of evaporation heat is not required to obtain a phase shift from liquid to vapour, just as the slope of the isobar curve in the T,S diagram under this condition is greater than zero for all values of T and S, so that according to the invention the liquid and the vapour serve as heat sources that do not possess latent evaporation heat. The curves shown in fig. 2B appear from Table 3 in "Properties of Water and Steam in Si-Units", Ed. U. Grigull and E. Schmidt, Springer-Verlag, Berlin 1989. Furthermore, referring to fig. 2C, it appears from the solubility diagram of NaCl in water, "Natrium, Gmelins Handbuch der Anorganischen Chemie, 8. Auflage, Verlag Chemie, Weinheim 1973, that for a pressure above the critical pressure, e.g. 250 bars, super critical water vapour at a temperature of about 420 °C may be saturated with about 0.05% NaCl and super critical water with about 25% NaCl. Therefore, by applying a pressure and a tempe- rature above the critical point to the separation zone salt water can be separated in a fraction with a low content of NaCl and a fraction with a high content of NaCl. With suitable outlets several fractions of the vapour 33 and the residue 53 may be withdrawn with different NaCl contents. It is shown in fig. 3A and fig. 6 how the residue outlet is positioned immediately below the liquid surface. However, it will be possible to provide more outlets if a residue with a lower concentration of e.g. salt is de¬ sired, provided that these outlets are used in connection with withdrawal of the residue immediately below the liquid surface. Correspondingly, it will be possible to discharge vapour with different contents of e.g. NaCl by mounting the vapour outlet at different distances from the liquid surface or by regulating the temperature of the vapour at the outlet. Figs. 3A-C show specific embodiments in which the vapour 43 is discharged with phase shift from vapour to liquid as a distillate 40, the temperature of the vapour in the vapour phase being raised by - adding heat to the separation section via a heat source (60) (fig. 3A), - withdrawing the heat from the separation section 32 and heating it outside by a heat source 60 (fig. 3B), or - introducing a heat source 60 in the separation section 32 (fig. 3C), the distillate being discharged such as to release its heat to the liquid in the heating section 31. Correspondingly, the residue 53 is discharged such as to release its heat to the liquid in the heating section 31. As appears from fig. 3A, the separation section 32 is part of the heating section 31 so that a pressure equal to the pressure of the separation section is applied to the heating section, but in another specific embodiment (not shown), the separation section 32 is separated from the heating section 31 and connected with suitable feed and discharge means. The heating section is heated e.g. as shown in a specific embodiment by recovering heat from the vapour 33 and from the residue 53, but the heat for heating the heating section may originate from another heat source or sources. Figs. 14A,B and 15A,B show preferred embodiments of a predominant part of the separation zone/section 32A which is shaped as a helix, in which the vapour phase 43 and the residue 53 in the individual turns of the helix are sepa¬ rated by a liquid surface because of the centrifugal force. In fig. 14A, and 14B the last part of the separation section is a cyclone 33, which is a separatory funnel in the embodiment of figs. 15A and 15B. Expedient embodiments of the method and the apparatus appear from the claims, the drawings and the following examples. 5 EXAMPLES A plurality of examples of preferred embodiments and use of the invention are given below. EXAMPLE 1 Desalination of Salt Water Fig. 3A shows a preferred embodiment of a desalination apparatus operating according to the method of the invention. "Separation Section" Fig. 6 shows an enlarged part of the separation section 32 which consists of a container such as a high pressure chamber 325, in which a vapour pipe terminates in the upper part and a residue pipe 327 in the lower part so that the two pipes terminate on their respective sides of a liquid surface 45 formed at the location where the phase shift for the fed liquid occurs. In the shown embodiment the separation section 32 is incorporated as part of the heating section 31, where the baffle plate 311 for the fed heated liquid and the inlet 312 directly adjoin the separation section 32. The separation section 32 may be separated from the heating section 31. "Heating of Vapour in the Separation Section" Fig. 3 shows a preferred embodiment of the heating of the vapour in the separation section, in which a heating device 60, such as a flame, heats the separation section directly. Fig. 3B shows another preferred embodiment, where the vapour is withdrawn and then heated by a heating device 60, following which it is recycled to the separation section 32. fig. 3C shows yet another embodiment in which a heating device 60, such as a heating member, is introduced in the vapour phase of the separation section above the liquid surface 45. "Heating Section" The heating section 31 consists of a device for trans¬ ferring heat, such as a heat exchanger, arranged as a counter current heat exchanger and constructed to give a 2 heat transition number of about 3 kW/m °C. It is expected that a pure counter current heat exchanger will give a better heat efficiency. "Water Pump" The water pump 20 is adapted to feed raw water to the heat exchanger 31 and the separator 32 under a constant water pressure of 240-260 bars, while distillate 40 and residue 50 are withdrawn. It is preferred that the water pump is adapted such that the energy used for pumping raw water into the heat exchanger and the separator is recovered as much as possible when the water is withdrawn again. In a preferred embodiment the water pump 20 comprises three cylinders: a) a cylinder A for pumping raw water 10 into the heat exchanger. b) a cylinder B for removal of concentrated water 50, and c) a cylinder C for withdrawal of distillate 40. In another preferred embodiment the water pump moreover comprises a cylinder D for driving a piston which is to pulsate the water in the heating and separation section (see example 2) . Fig. 4 shows an enlarged section through the raw water pumping cylinder A comprising a piston 210, an inlet valve 211 and an exhaust valve 212, both of which are non-return ball valves. When the piston 210 moves away from the top position, the inlet valve 211 opens and the exhaust valve 212 closes, so that raw water is drawn in in front of the piston. Conver¬ sely, when the piston 220 moves toward the top position, the inlet valve 211 closes and the exhaust valve 212 opens, so that the raw water is discharged into the conduit 11. The exhaust valve 212 is moreover adapted such that it is prevented from closing when the pressure becomes too big in the system. Fig. 5 shows an enlarged section through the cylinder C (cylinder B operates in the same manner) comprising a ball valve 232 and a slide valve 233 controlled via a boss 24. When the piston 230 moves toward the top position, the water is pumped out. Somewhat before the top the discharge of water is shut off by closing the slide valve 233. The water pressure in the cylinder C hereby increases to the same pressure as in the conduit 41. Simultaneously, the slide valve 233 applies a pressure to the ball valve 232 corresponding to the spring pressure with which the balls in the valves are biased. When the pressure in the cylinder C is approximately the same as in the conduit 41, the slide valve 233 permits inflow of water by lifting the ball from its seat. When the piston 230 moves toward the bottom position, the ball valve 232 is kept open until the boss 24 pulls back the slides and the ball valve 232 shuts off inflow of water and the slide valve 233 opens for discharge of the water. This arrangement entails that the ball valve 232 is safe¬ guarded against a great pressure drop across the valve, so that both cavitation and consequent corrosion and great liquid flow surges in the apparatus are avoided. In a test set up all seals were lip seals, but to reduce the consequent frictional losses it is preferred to use pistons and cylinders without seals and made of a ceramic material or of hard metal. "Start Procedure" The apparatus is started by pumping-in distilled water until all system air has been expelled and replaced by water. Then pumping continues with activated valve lifter 25 so that outflow of water is shut off. The valve lifter 25 is deactivated at the desired pressure, and then the water pump 20 is ready. The desired pressure is obtained in that the stroke volume of the feed pump, cylinder A in fig. 4, is a few per cent greater than the stroke volume of the exhaust pump, cylinders B and C (fig. 5), so that the pressure in the system assumes a value which is balanced with the spring bias in the feed pump. Then heat is added in an amount which is regulated until a desired temperature is achieved in the separator, following which the salt water to be distilled is fed. "Tests" Tests have been performed in which the pressure in the system has been 250 bars and the temperature profile in the separation zone has been 390-425 °C. Salt water with 3% NaCl was added, and a distillate with 0.014% NaCl and a residue with 6% NaCl were obtained, which is in good agreement with the solubility diagram in fig. 2C. EXAMPLE 2 Desalination Apparatus with Pulsator Fig. 7 shows an embodiment in which the fed liquid in the heat exchanger is caused to pulsate by means of a fourth cylinder D in the water pump 20 which communicates with the heat exchanger via a conduit 71. A better separation of the salt in the separator 32 is achieved by pulsating the liquid. EXAMPLE 3 Desalination Apparatus with Cyclone Fig. 8 shows an embodiment in which the vapour, which is withdrawn from the separator in the conduit 43, is passed to a cyclone 80, from which super critical vapour both with greater particles and without is passed on for further heating and subsequent condensation in the heat exchanger 31 via the conduit 81 and 82, respectively. Alternatively, heating can take place before the cyclone. The need for separation of particles, such as salt particles, from the super critical vapour is monitored by measuring the salt concentration in the residue 51 by means of a salt sensor 90, such as a conductivity meter. In case of too great a concentration valve 91 closes slightly and valve 92 opens slightly to reduce the concentration in the residue stream 51, which is passed to the conduit 51A via the valves 91 and 92. The advantage is that the separator sector can be made smaller and throughput greater. EXAMPLE 4 Desalination Apparatus with Filter Fig. 9 shows an embodiment in which the cyclone 80 in fig. 8 has been replaced by a filter 100, such as a ceramic filter. Like in the case of the cyclone, the separator can be made smaller and through put greater. Since the filter is moreover cheaper, this embodiment is preferred, in particular in case of smaller devices. Optionally, an apparatus may comprise both a cyclone and a filter. EXAMPLE 5 Desalination Apparatus with a Vapour Compressor Fig. 10 shows an embodiment in which mechanical vapour compression is performed instead of thermal heating of the formed vapour to increase its temperature. "Vapour Compressor" Fig. 11 shows an enlarged part of the vapour compressor 120 which must be adapted to work at high temperatures, vapour lubrication and highly oxidative vapour. Vapour compression is performed in that the piston rod 123, which is operated at room temperature by the cylinder D in the moving system to the water pump 20, is moved such that the non-return ball valve 121 opens and the non¬ return ball valve 122 closes when the piston rod 123 is urged toward its top position, whereby the volume 124 is filled with vapour 43 from the separation section 32. Fig. 12 shows an enlarged part of the feed pump comprising two non-return ball valves 211 and 212 as well as a spring-loaded cylinder A, whose spring 213 is adjusted such that the pressure in the system is prevented from exceeding the desired pressure. The apparatus is moreover provided with an expansion container 110 which, in addition to serving as a pressure valve, also serves as a damper for the pulsation from the vapour compressor 120. To remove components, such as lime, which are more sparingly soluble than the salt of the main component, the heat exchanger 31 is provided with an outlet for a sludge trap 130 somewhat before the separator 32. EXAMPLE 6 Heat-Pressure Treatment Fig. 13A shows a preferred embodiment of a heat-pressure treatment apparatus which operates according to the method of heat-pressure treatment of a liquid according to the invention. The apparatus is constructed like the salination apparatus according to example 1 with the exception that residue is not withdrawn from the separator and that the water pump is just equipped with one withdrawal device. "Tests" Tests were performed with heat-pressure treatment of liquids in which carbon, cellulose, saccharose, ethanol, acetic acid and carbamide were suspended and/or dissolved, all of which reacted with the medium to form CO, CO,,, H and H 3 , respectively, according to the following reactions: a) Reduction oxidation reactions: (water gas), b) Hydrolysis reaction: 6. C0(NH 2 ) 2 + H 2 0 -> NH 3 + C0 2 , EXAMPLE 7 Energy Consumption The energy consumption for 1000 kg of distillate for the desalination apparatus in example 1 was calculated under the following conditions: raw water, 3% NaCl: 1125 kg/h, temperature 8 °C distillate: 1000 kg/h, temperature 15 °C residue, 24% NaCl: 125 kg/h, temperature 15 °C pressure in heat exchanger and separator: 250 bars efficiency of water pump: 85% radiation loss from the apparatus: 10% of added heat a) Power consumption of pump: 0.15 x 250 x 10 5 x 1125/(3600 x 10 6 ) = 1.172 kWh b) Heat consumption 4.184 x (15-8) x 1.125/3600 = 9.150 kWh c) Radiation loss: 9.150 x 0.1 = 0.915 kWh The total energy consumption depends upon the construction of the pump, heat exchanger and insulation. EXAMPLE 8 Energy Consideration for the Apparatus To evaluate added theoretical heat in the separation zone the following enthalpies were calculated for pure water: Raw water into the heating zone: 1.5 kg, temperature 10 °C, pressure 250 bars, 99 kJ; Distillate at inlet in the top of the separation zone (vapour pipe): 1.0 kg, temperature 420 °C, pressure 250 bars, 2774 kJ; Distillate out of the heating zone: 0.5 kg, temperature 390 °C, pressure 250 bars, 107 kJ; Residue at inlet in the bottom of the separation zone (residue pipe outlet): 0.5 kg, temperature 390 °C, pressure 250 bars, 1195 kJ; and Residue out of the heating zone: 0.5 kg, temperature 20 °C, pressure 250 bars, 55 kJ. 162 kJ - 99 kJ = 63 kJ per 1.0 kg of distillate are added. EXAMPLE 9 Comparison of Vapour and Water Compression To evaluate the size of the mechanical work for a dis¬ tillation apparatus according to the invention a calcu¬ lation was made of the compression work for a distillation of raw water at a water production (distillate) of 1 kg/h under the following conditions: raw water in: 1.5 kg/h, temperature 10 °C distillate out: 1.0 kg/h, temperature 20 °C residue out: 0.5 kg/h. temperature 20 °C a) Heat loss of outgoing water (common to vapour and water compression): Q = dt x C x m/3600 = 17.43 Wh Cp = 4184 J/kg ' at 250 bars, b) Vapour Compression Work: pressure in evaporator : 1 bar, temperature 100 °C pressure in condensator: 1.5 bars, temperature 110 °C Theoretical work: L=k/(k-l) x P 1 x V χ ((P 2 /P 1 )-((k-l)/k)-l)/3600 = 19.86 Wh Expected Work: 19.86 / 0.5 = 39.7 Wh. c) Water Compression Work Pressure in heat exchanger and separator: 250 bars Theoretical work: L = P x V/3600 = 10.42 Wh, which gives L = 5.21 Wh with a recovery degree of 50%. For a continuous water production of 1 kg/h there is a saving in work of about 5 times by water compression with respect to vapour compression, which enables distillation of a liquid with a lower energy consumption than in the heretofore known methods, and the distillate is always sterile.

Claims: P a t e n t C l a i m s: 1. A method of distilling a liquid near or above the critical point of the liquid, wherein a) the liquid is fed to a heating zone (31) in which it is heated, and then b) the heated liquid is conveyed to a separation zone (32) to which a pressure is applied such that the liquid is brought to a state near or above the critical point, whereby it undergoes a phase shift forming a vapour phase (43) and a liquid residue (53) * which are separated by a liquid surface (45), and then c) the temperature of the vapour in the vapour phase (43) is raised, and d) the vapour (43) phase-shifted from vapour to liquid and the residue (53) are discharged as a distillate (40) and a residue (50), respectively, such that they release their heat to the liquid in the heating zone (31), thereby heating the liquid. c h a r a c t e r i z e d by providing in a predominant part of the separation zone a temperature profile which increases from a liquid inlet to a vapour outlet and in which the liquid assumes a temperature near or above the critical temperature of the liquid, and withdrawing the residue (53) immediately below the liquid surface (45) in the separation zone (32) . 2. A method according to claim 1, c h a r a c t e r ¬ i z e d by raising the temperature of the vapour in the vapour phase (43) by adding heat in an area of the separation zone which is at a relatively great distance from the area of the separation zone where the residue (53) is withdrawn. 3. A method according to claims 1-2, c h a r a c t e r ¬ i z e d by raising the temperature of the vapour in the vapour phase (43) by heating the vapour by addition of heat to it inside the separation zone (32) . 4. A method according to claims 1-2, c h a r a c t e r ¬ i z e d by raising the temperature of the vapour in the vapour phase (43) by heating the vapour by addition of heat to it outside or into the separation zone (32) . 5. A method according to claims 1-2, c h a r a c t e r ¬ i z e d by raising the temperature of the vapour in the vapour phase (43) by withdrawing the vapour from the separation zone (32) and heating the withdrawn vapour. 6. A method according to claims 1-5, c h a r a c t e r ¬ i z e d in that the last part of the separation zone (32 ) is a cyclone zone (33) in which the liquid surface (45) assumes a parabolic-like shape. 7. A method according to claims 1-5, c h a r a c t e r ¬ i z e d in that the last part of the separation zone (32) is a separatory funnel (34 ) . 8. A method according to claims 6-7, c h a r a c t e r ¬ i z e d by raising the temperature of the vapour in the vapour phase (43 ) by heating the vapour by addition of heat to it inside a spiral-shaped course (32A) of the predominant part of the separation zone. 9. A method according to claims 1-8, c h a r a c t e r ¬ i z e d by feeding the liquid in the bottom of the separation zone (31). 10. An apparatus for distillation of liquid near or above the critical point of the liquid, comprising a) a separator, b) a heat exchanger, c) means for feeding liquid to the heat exchanger, d) means for heating liquid and vapour in the separator, e) means for discharging the vapour and the residue, respectively, from the separtor, f) pumps for pumping-in the liquid and pumping out the vapour and the residue, respectively, said liquid feeding means and heating being adapted to establish such a pressure and such a temperature in the separator that the vapour and the liquid in it are present near or above the critical point, and said vapour and residue discharging means discharging the vapour and the residue in the separator via the heat exchanger in which the vapour is converted to a dis¬ tillate, c h a r a c t e r i z e d in that heating means are provided in connection with a predominant part of the separation section, said heating means being adapted to establish a rising temperature profile from a liquid inlet to a vapour outlet in the separation section, and that the outlet for the residue discharging means in the separation section (32) is positioned immediately below the liquid surface (45) between the vapour (43) and the residue (53). 11. An apparatus according to claim 10, comprising reciprocating pumps with displacement means (A,B,C), such as pistons or diaphragms for liquid, residue and distillate, respectively, c h a r a c t e r i z e d in that each of the pumping-out cylinders associated with the residue replacement means (B) and the distillate displacement means (C) communicates with an outlet valve (232) and a slide valve (233) controlled by the piston movement such that the slide valve (233) shuts off outflow of liquid to a discharge conduit (42) when the piston (230) has reached a location before its top position, and opens the outlet valve (232) when the pressures above it are comparable. 12. An apparatus according to claim 11, c h a r a c t e r i z e d in that the control of the piston movement is additionally so that the slide valve (233) shuts off inflow of liquid from the outlet valve (232) when the piston (230) has reached a location before its bottom position, and opens for outflow of liquid to the discharge conduit (42) when the pressures above it are comparable. 13. A apparatus according to claims 10-12, c h a r a c t e r i z e d in that the pumping-in cylinder associated with the liquid displacement means (A) communi¬ cates with an exhaust valve (212) which is connected with a relief valve (213) adjusted to open when the pressure in the system exceeds a desired pressure. 14. An apparatus according to claims 10-13, c h a r a c t e r i z e d in that a heat source (10) adds heat to the separation section (32) inside it. 15. An apparatus according to claims 10-14, c h a r a c t e r i z e d in that a heat source (60) adds heat to the separation section (32) outside and into it. 16. An apparatus according to claims 10-14, c h a r a c t e r i z e d in that the vapour discharging means include a section outside the separation section (32) which is heated by a heat source (60). 17. An apparatus according to claims 10-16, c h a r a c t e r i z e d in that the last part of the separation section (32) is a cyclone (33). 18. An apparatus according to claims 10-16, c h a r a c t e r i z e d in that the last part of the separation section (32) is a separatory funnel (34) . 19. An apparatus according to claims 17-18, c h a r a c t e r i z e d in that a heat source (60) for adding heat to the separation section (32) is positioned radialy within a spiralrlike course of the predominant part of the separation section. 20. An apparatus according to claims 10-19, c h a r a c t e r i z e d in that the liquid feeding means feeds liquid in the bottom of the separation section (31).

Inventors: OLRIK HENRIK GERNER, OLRIK, HENRIK, GERNER
Applicants: GRUNDFOS INT, GRUNDFOS INTERNATIONAL A/S
Application year: 1992
Main classification: F22B3
IPC codes: B01D1, C02F1, F04B1, F04B7, F04B9, F04B53