WO2006025117A1 - 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 - Google Patents
機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 Download PDFInfo
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- WO2006025117A1 WO2006025117A1 PCT/JP2004/013086 JP2004013086W WO2006025117A1 WO 2006025117 A1 WO2006025117 A1 WO 2006025117A1 JP 2004013086 W JP2004013086 W JP 2004013086W WO 2006025117 A1 WO2006025117 A1 WO 2006025117A1
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- evaporation chamber
- brine
- pressure
- evaporation
- steam
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Classifications
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2803—Special features relating to the vapour to be compressed
- B01D1/2818—Cleaning of the vapour before compression, e.g. demisters, washing of the vapour
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/284—Special features relating to the compressed vapour
- B01D1/2846—The compressed vapour is not directed to the same apparatus from which the vapour was taken off
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/284—Special features relating to the compressed vapour
- B01D1/2856—The compressed vapour is used for heating a reboiler or a heat exchanger outside an evaporator
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2881—Compression specifications (e.g. pressure, temperature, processes)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
- B01D1/305—Demister (vapour-liquid separation)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
- B01D5/0009—Horizontal tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray evaporation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Definitions
- the present invention relates to a seawater desalination apparatus, and more particularly, to an evaporation chamber used in a seawater desalination apparatus using a single-stage flash evaporation method combined with a mechanical vapor compression method.
- TVC Multi-effect evaporator water generator
- MVC single-stage flash evaporation water generator combined with mechanical vapor compression
- MS F has many achievements as a large-capacity fresh water generator, but as shown in Fig. 6, the evaporation chamber 10 1 divided into a number of compartments (stages) with different operating pressures was used. Since the configuration is such that flash evaporation is performed stepwise at low pressure, the evaporation chamber is large and the necessary heat transfer surface As a result, the scale of the entire facility increases, requiring a large site and increasing the construction cost.
- the evaporation chamber is divided into a number of stages with different operating pressures, it is difficult to control each stage to bring the pressure to an equilibrium state. Therefore, since it is difficult and time-consuming to start and stop the equipment, it is generally a principle of continuous operation.
- the TVC pressurizes the steam in the final stage 1 1 2 of the 4 to 5 multi-effect evaporator 1 1 1 with the ejector 1 1 3 using steam around 20 Bar. Since all the latent heat of the steam for pressurization can be used, construction costs and energy costs required for water production are cheaper than MFS.
- the multi-effect evaporator 1 1 1 has a large heat transfer coefficient because it performs evaporation heat transfer, does not require a circulation of the pipeline, and is easy to operate and maintain because there are no moving parts. Therefore, it is often used as a medium-capacity or small-capacity fresh water generator.
- the conventional MVC as shown in Fig. 8, compresses the steam generated in the evaporation chamber with mechanical steam compression means 1 2 2 such as a blower or compressor, and converts the steam that has been heated to high temperature and pressure by compression.
- This heat transfer tube is evaporative heat transfer like TVC, so it has a large heat transfer coefficient, does not require the circulation of the brain, and has a smaller heat transfer area and facility scale than MSF, and has a large site. It is not necessary, and construction costs are low, and there are advantages such as easy start / stop and operation control. However, as described below, there is a difficulty in increasing the capacity, and in the medium capacity and small capacity fields, TVC is easier to operate and maintain, and there have been few achievements. A problem common to these various fresh water generators is the generation of hard scale in the evaporation chamber.
- the solubility of Ca SO 4 the main component of the hard scale, varies with temperature.
- the crystal form in which C a SO 4 precipitates varies depending on the temperature, and below 70 ° C
- Dihydrate C a S0 4 2H 2 0 is an anhydrous salt C a SO 4 at 70 ° C to 90 ° C
- hemihydrate C a S0 4 ⁇ I / 2H2O is precipitated at 90 ° C and above .
- the pressure of the steam passing through the heat transfer tube is set to 0 so that the temperature of the outer surface of the heat transfer tube is maintained from a temperature range where the solubility of the anhydrous salt C a SO is sufficiently high, that is, from 65 ° C to 70 ° C.
- the specific volume of steam generated by flash evaporation becomes extremely large in this low pressure region that has been conventionally used in these various fresh water generators.
- MV C performs single-stage flash evaporation, so the temperature difference between the evaporation chamber inlet and outlet brine (or seawater) is small.
- the amount of water produced by the desalinator is the product of “the difference in brine (or seawater) temperature between the inlet and outlet of the evaporation chamber” and “the amount of brine (or seawater) that passes through the evaporation chamber”.
- this brine temperature difference is about 6 7 deg C
- MV C the sea water temperature difference is about 3.5 deg C to 5 deg C. There is an opening.
- MVC in order to produce the same amount of water, MVC must circulate a large amount of brine or seawater, which is 13 to 20 times that of MSF. There was a recognition that would be higher. There is no track record of large-capacity MVC operated at atmospheric pressure until now, even if the blower and other problems can be solved by the invention of the blower mentioned above and the idea of operation at atmospheric pressure. This is thought to be because the problem of scale generation and the cost of power necessary for the circulation of brine or seawater have not been solved. In order to realize a large-capacity MVC, prevent evaporation from occurring in the evaporation chamber, especially its heat transfer surface, reduce the power required for circulation of brine or seawater, and minimize flash evaporation.
- the present invention introduces a brine that is heated to a temperature equal to or higher than the saturation temperature of the pressure in the steam chamber, and flashes and evaporates water from the brine to generate steam,
- steam 1 Mechanical vapor compression means for compressing the generated steam
- steam 2 Heating the brine sent to the evaporation chamber by condensing the compressed steam
- An evaporating chamber for use in a single-stage flash evaporating water-making apparatus using a mechanical vapor compression method having a communication pipe for returning brine from the heat exchange means to the evaporating chamber;
- the saturation pressure of the temperature of the steam 2 is supplied to the heat exchange means. It is an evaporation chamber placed at a higher position than the heat exchange means so as to give a water head difference greater than the difference in pressure between steam and steam 1. That is, the heat exchange means for heating seawater used in the conventional MVC is replaced with an evaporation chamber provided in the interior, and an evaporation chamber dedicated to flash evaporation of brine and steam It is an MVC that separates the heat exchange means dedicated to heating the brine by condensation of 2.
- the evaporation heat transfer of seawater is performed on the heat transfer surface, and thus the occurrence of a scale on the heat transfer surface is unavoidable.
- the evaporation chamber is formed on the heat transfer surface. Condensation heat transfer of the steam generated in step 3 is performed, so if the brine pressure on the heated side is kept above the saturation pressure of the temperature of the steam 2 on the heating side, boiling of the brine is easily prevented and scale is generated. Can be suppressed. To that end, the brine in the heat exchange means must always be able to maintain a pressure equal to or higher than the saturation pressure of the temperature of the steam 2 on the heating side, regardless of the operating conditions of the fresh water generator.
- the water head difference suppresses the generation of scale in the brine in the heat exchange means.
- the required pressure that is, a pressure equal to or higher than the saturation pressure of the temperature of steam 2 can be applied. More specifically, the saturation pressure at the temperature of steam 2 obtained by compressing steam 1 generated in the evaporation chamber by mechanical compression means is designed and operated so as to have a certain differential pressure with respect to the pressure of steam 1.
- the pressure of the brine in the heat exchange means during normal operation is obtained by adding the pipe resistance from the heat exchange means to the evaporation chamber and the water head difference to the pressure in the evaporation chamber. If the sum of the head differentials is above a certain differential pressure, brine boiling usually does not occur inside the heat exchange means.
- the evaporation chamber should be positioned higher than the heat exchange means so that the value obtained by adding the water head difference between the evaporation chamber and the heat exchange means to the pressure of the evaporation chamber is equal to or higher than the saturation pressure of the temperature of the steam 2 described above.
- the problem of scale generation on the heat transfer surface can be avoided in any operating condition.
- the crystal of the scale is larger than that of a desalinator that operates at 65 ° C to 70 ° C. Since the deposition rate becomes extremely high, it is necessary to always secure this water head difference so as not to precipitate the scale.
- a portion where the brine flows from the communication pipe to the evaporation chamber is a nozzle, and a part of the static pressure held by the brine is efficiently a horizontal speed component.
- the nozzle has a shape in which the cross section of the flow path gradually decreases according to the flow, and is directed in a direction between 0 ° and 50 ° from horizontal to upward,
- the bottom of the evaporation chamber has a horizontal part that is until the flash evaporation of the brine decompressed through the nozzle is almost completed, and the brine that has been almost completed is the vacuum in the evaporator.
- a vaporization chamber having a portion facing the brine outlet at a position opposite to the nozzle and having a bottom surface inclined at an angle between 20 ° and 60 ° upward from the horizontal.
- the brine pushed by the circulation means and exits the heat exchange means flows upward through the connecting pipe and reaches the evaporation chamber.
- a nozzle with a gradually reducing channel cross section is provided, which is directed from 0 ° to 50 ° upward from the horizontal. Enter the evaporation chamber through the nozzle and flash evaporate the water from the brine.
- the nozzle cross-section By gradually reducing the nozzle cross-section, part of the static pressure of the brine efficiently changes to dynamic pressure, and the nose direction changes from horizontal to upward from 0 ° to 50 °. By doing so, the brine that exits the nozzle contains a lot of horizontal velocity components.
- the brine exiting the nozzle flows through the evaporation chamber toward the brine outlet at a position opposite to the nozzle due to the horizontal velocity component while performing intense flash evaporation.
- the bottom of the evaporation chamber is close to the nozzle, that is, where flash evaporation is taking place.
- the horizontal velocity component of the brine is The brine is efficiently reconverted to static pressure by running up the inclined bottom surface.
- This converted static pressure has the effect of reducing the power required for the circulation means.
- the nozzle is provided in a form having a slit-like outlet extending in the lateral direction near the bottom surface of the wall facing the horizontal portion of the bottom surface of the evaporation chamber, It is desirable that the ejection direction from the nozzle should be 20 ° to 50 ° upward from the horizontal.
- the nozzle having a gradually reduced cross section is used so that the width of one wall of the evaporation chamber is effectively used to have a slit-like outlet extending in the lateral direction. Then, the brine can be made into a thin plate and flow into the evaporation chamber.
- the brine is simply poured along the bottom surface of the evaporation chamber, only the area of the top surface of the brine covering the bottom surface of the evaporation chamber is involved in the evaporation. Therefore, by directing the nozzle ejection direction 20 ° to 50 ° upward from the horizontal, the brine is ejected obliquely upward from the nozzle, and between the plate-like flow of the ejected brine and the bottom of the evaporation chamber. Create a space. As a result, the ejected plate-like flow has two areas on the upper and lower sides that are involved in evaporation, and evaporation is accelerated accordingly. Moreover, the steam generated from the lower surface of the ejected plate-like flow breaks through the plate-like flow and escapes upward, so that the ejected plate-like flow is disturbed, and evaporation is further accelerated.
- the pressure of the brine entering the nozzle from the connecting pipe is higher than the pressure in the evaporation chamber, as compared with the “saturation pressure corresponding to the temperature of the brine” and “the evaporation chamber. It is desirable that the pressure difference is higher by 1.1 to 1.5 times the differential pressure.
- the heat exchanging means is arranged at a position lower than the evaporation chamber by the head differential, so that the two are connected by a connecting pipe that is vertically connected.
- the evaporation chamber of the present invention has a wall that divides the evaporation chamber into an upper part and a lower part, and the wall passes the vapor 1 from the lower part of the evaporation chamber through the wall in the vicinity of the brine outlet.
- An opening that circulates to the upper part of the evaporation chamber; and an outlet of the vapor 1 is provided on the opposite side of the opening at the upper part of the evaporation chamber, and the vapor 1 passes from the lower part of the evaporation chamber through the opening to the upper part of the evaporation chamber It is desirable to reverse the direction when As described above, in the evaporation chamber of the present invention, the brine ejected from the slit-like nozzle outlet provided on the one wall is flushed while flowing toward the opposite wall by the horizontal velocity component. Evaporate.
- a brine outlet is provided near the opposite wall, through which the pipeline is sent from the evaporation chamber to the circulation means.
- a wall that divides the evaporation chamber into an upper part and a lower part is provided, and an opening is provided as described above, and the outlet of the vapor 1 from the evaporation chamber is opposite to the opening, in other words, a wall that is divided into two parts in the vertical direction.
- the 180 ° reorientation at this opening allows many parts of the mist contained in the steam to be separated by inertia, greatly reducing the mist in the steam going to the mechanical vapor compression means. be able to.
- the evaporation chamber of the present invention is provided with a plurality of substantially vertical mist separators that block the flow of the vapor 1 whose direction is reversed at the upper portion of the evaporation chamber, and at least the flow of the vapor 1 It is desirable to provide a cleaning spray device for the mist separator installed on the most upstream side of the mist.
- mist separators By installing a plurality of mist separators in such a way as to block the flow of steam 1 flowing in the lateral direction above the evaporation chamber, it is possible to further separate and collect the mist that could not be separated even at the above 180 ° direction change. .
- mist captured by the mist separator is held while adhering to the mist separator, it will be re-scattered by the force of the steam 1 passing through it, increasing the mist amount of the steam 1 again. End up.
- the horizontal mist separator which is arranged in a way that blocks the steam flowing in the vertical direction, which is often used in the conventional MVC, has a problem of re-scattering because the trapped mistakes are not discharged smoothly.
- the mist separator substantially vertical in the present invention, the captured mist can easily flow down along the mist separator, and re-scattering can be prevented.
- a cleaning spray device is installed at least in the mist separator installed on the most upstream side of the steam 1 flow.
- the washing water sprayed by this device has the following effects by diluting the mist adhering to the mist separator to prevent scale and by making steam 1 into saturated steam.
- the brine flowing into the evaporation chamber is higher than the saturation temperature of the evaporation chamber pressure.
- the temperature at the brine outlet of the evaporation chamber is higher than the saturation temperature by the amount corresponding to NETD, the steam 1 in contact with it is slightly overheated.
- the mist separator can prevent the precipitation of scale in the mechanical vapor compression means and reduce the problems associated therewith.
- the sprayed cleaning water also contributes to the improvement of the separator efficiency of the mist separator.
- the water used in this cleaning spray device in MVC is generally condensed water condensed by heat exchange means. Since this condensed water is maintained at a temperature higher than the saturation temperature of the evaporation chamber, when it exits the spray device, a part of it is splashed and evaporated, generating mist itself and increasing the amount of mist.
- the main body of the mist separator is a thin wire hardened in a sponge shape. Steam containing mist travels through the narrow gap between the wires while repeating collisions, and the retained mist is left on the main body due to the collision, thereby exerting the effect of trapping mist. Therefore, if a certain amount of mist adheres to the mist separator, the narrow gap becomes narrower and the collision becomes intense and the mist is easily captured.
- the mist separator provided with the spray device improves the separator efficiency for the same reason.
- the mist separator By making the mist separator almost vertical, the water used for cleaning can also be mist separated. It flows down from top to bottom along the screen to help clean the bottom of the mist separator. By adopting an almost vertical mist separator, water that has been washed is easily discharged.
- the evaporation chamber of the present invention is preferably configured such that the cleaning spray device divides the mist separator to be cleaned into several parts and can sequentially wash the divided parts. .
- the increase in the pressure loss of the mist separator due to the attachment of the washing water is limited to a part of the range during washing, so the overall pressure loss is reduced.
- the increase can be mitigated and the wash water can be used effectively by intermittent washing.
- the problem of scale generation on the heat transfer surface necessary for practical use of a large-capacity MVC is solved, less power is required for circulation of the brine, and the brine of the entire system is reduced.
- FIG. 1 is an explanatory diagram of the whole of a single-stage flash evaporation method water making apparatus using a mechanical vapor compression method in which an embodiment which is the best mode of an evaporation chamber according to the present invention is used.
- FIG. 2 is a sectional view of an embodiment which is the best mode of the evaporation chamber according to the present invention.
- FIG. 3 is an explanatory view of an embodiment of a nozzle provided in the evaporation chamber according to the present invention.
- FIG. 4 is a table showing examples of the flow velocity, dynamic pressure, static pressure, and total pressure of the brine at each point of the nozzle shown in FIG.
- FIG. 5 is an explanatory view of an embodiment of the cleaning spray device provided in the evaporation chamber according to the present invention.
- Fig. 6 is an explanatory diagram of MSF that has been used in the past.
- Figure 7 is an illustration of TVC that has been used in the past.
- Fig. 8 is an illustration of MVC that has been used in the past.
- Fig. 9 is a solubility curve of calcium sulfate.
- FIG. 1 is an overall explanation of a single-stage flash evaporation method fresh water generator using a mechanical vapor compression method in which an embodiment which is the best mode of an evaporation chamber according to the present invention is used.
- FIG. 1 is an overall explanation of a single-stage flash evaporation method fresh water generator using a mechanical vapor compression method in which an embodiment which is the best mode of an evaporation chamber according to the present invention is used.
- steam 1 is compressed by mechanical steam compression means 6 such as a blower or a compressor, and becomes steam (steam 2) having a higher temperature and pressure than steam 1.
- Steam 2 is led to heat exchanging means 4 and condensed with heat exchange with brine 3 3 to produce product water 3 6.
- the majority 3 3 3 of the pipeline 3 2 that has finished flash evaporation is returned to the heat exchange means 4 by the circulating means 9 such as a pump together with the replenished sea water 3 8,
- the remaining part 3 4 is discharged by the brine discharge pump 1 2 after preheating the seawater supplied by the seawater preheater 1 1.
- the production water 3 6 also preheats the seawater 3 8 replenished in the seawater preheater 1 1 and is sent to the place where it is needed by the production water pumps 1 4 and 1 5.
- the replenished seawater 3 8 is sent into the system by the seawater pump 17 and the seawater preheater 1 1 receives heat from the discharged pipeline 3 4 and the produced water 3 6 and then circulates in the brine 3 3 It is mixed in.
- a tube / shell type heat exchanger is assumed to be used as the seawater preheater 11, but it is naturally possible to use a plate type heat exchanger or MSF instead. It is.
- the evaporation chamber 3 is arranged at a position higher than the heat exchanging means 4, and the brine difference H in the heat exchanging means 4 is utilized by utilizing the water head difference H.
- the required head differential H is selected as follows.
- the saturation pressure at the temperature of steam 2 compressed by mechanical compression means 6 is designed and operated so as to have a constant differential pressure with respect to the pressure of steam 1.
- the pressure of the brine in the heat exchanging means 4 is the pressure of the steam chamber 3 plus the pipe resistance and the head difference between them, so the sum of the pipe resistance and the head difference is the above. If it is above the “certain differential pressure”, boiling of the brine in the heat exchange means 4 does not occur under normal operating conditions. It is also conceivable that the flow of the brine stops for some reason and the pipe resistance at the nozzle after exiting the heat exchange means 4 becomes zero.
- evaporating chamber 3 is adjusted from heat exchanging means 4 so that the value obtained by adding the water head difference H between evaporating chamber 3 and heat exchanging means 4 to the pressure of the vapor chamber is equal to or higher than the saturation pressure of the temperature of vapor 2. If it is placed at a high position, even if the brine circulation stops, The pressure of the steam is kept above the saturation pressure of the temperature of steam 2, boiling of the brine is avoided, and scale generation can be suppressed.
- the water head difference H is the water head difference between the upper surface of the heat exchanging means 4 and the lower surface of the evaporation chamber 3 as shown in the figure. It is necessary to think in.
- FIG. 2 shows a cross-sectional view of one embodiment of the best mode of the evaporation chamber 3.
- the heated brine 3 1 passes through the connecting pipe 1 8 to the nozzle 5 which is the inlet of the evaporation chamber 3, and when injected into the evaporation chamber 3, the brine 3 9 Water flashes to generate steam.
- Nozzle 5 has a shape in which the cross section of the flow path is gradually reduced, and part of the static pressure held by brine 31 is efficiently converted into dynamic pressure, so that the brine is evaporated at a speed corresponding to the dynamic pressure. Injected into 3.
- the sprayed brine has a large horizontal velocity component, which depends on the horizontal velocity component. Then, it flows toward the brine outlet 24 located near the wall opposite to the nozzle 5 of the evaporation chamber 3. (The bottom of the evaporation chamber 3 is close to the nozzle 5, that is, the portion 25 where flash evaporation is performed is horizontal, and the portion 26 ahead is an angle from 20 ° to 60 ° from the horizontal to the upper side.) Holds 3 and tilts.
- the pipe resistance until returning to 9 is about 6 m.
- the dynamic pressure of the brine at point C in FIG. 3 to be described later that is, 1.25 m, which is half of the dynamic pressure of the brine injected into the evaporation chamber 3, is converted back to the static pressure. This will save approximately 20% of the circulating power.
- the injection direction ⁇ of the nozzle 5 is not horizontal, but obliquely upward and at an angle of 20 ° to 50 ° upward from the horizontal, forming a plate shape from the nozzle 5.
- the sprayed brine 39 is discharged in the direction of spraying and progresses while drawing a parabola while performing flash evaporation, and there is a space between the brine 39 and the bottom surface 25.
- This ejected plate-like flow of pipeline 39 not only generates vapor 41 by flash evaporation from the upper surface, but also generates vapor 42 from the lower surface. That is, when the brine is simply ejected along the bottom of the evaporation chamber in the form of a plate, the top surface does not participate in the force and evaporation, whereas the top and bottom surfaces have a double area involved in evaporation. Evaporation is accelerated accordingly. Furthermore, the vapor 42 generated from the lower surface of the plate-like pipeline 39 creates a vapor flow 43 that breaks through the plate-like flow 39 everywhere and escapes upward, so that the plate-like flow 39 is greatly disturbed and further evaporated. Accelerated.
- FIG. 3 is an explanatory diagram of an embodiment of the nozzle 5 provided in the evaporation chamber 3.
- the slit that extends in the lateral direction effectively uses the width of one wall of the evaporation chamber as the inlet of the brine to the evaporation chamber. It is desirable to adopt a shape having a shaped outlet. So nozzle 5 is the evaporation chamber
- the front wall 21 of 3 has a full width, and has a slit-like outlet 24 extending close to the bottom surface 22 of the evaporation chamber 3.
- the pipeline 31 fed by the connecting pipe 18 enters the nozzle 5, and the brine flow rate increases as the cross-section of the flow path gradually decreases, including the point A at the inlet, the point B in the middle, and the point C at the outlet 24.
- the brine static pressure decreases by the increase in dynamic pressure and becomes equal to the pressure in the evaporation chamber 3 at point C.
- Fig. 4 shows that each of the nozzles in the case where the evaporation chamber 3 is operated at 1.02 bar at almost atmospheric pressure and the difference between the temperature of the brine 31 and the saturation temperature of the evaporation chamber, that is, the flash temperature difference is 5 deg C.
- Examples of the flow velocity (mZs), dynamic pressure (m), static pressure (m), and total pressure (m) of the brine at the point are shown.
- This is a calculation example of a nozzle with the ratio of the ratio of 3: 2: 1 at the A, B, and C points of the nozzle, and the height is a ratio of 3: 2: 1.
- the static pressure is displayed as Om.
- the above flash temperature difference of 5 de gC corresponds to a pressure difference of 0.195 bar (1.95 m). Therefore, compared to the pressure of the steam chamber, 1. If the pressure is more than 95 m, the brain will not flash. .
- the wall 51 has a wall 51 that divides the interior into two parts, an upper part and a lower part.
- the wall 51 has an opening 52 in the vicinity of the brine outlet 24.
- Steam 4 1, 4 2, 4 3 generated by flash evaporation once flows in the lower part 5 3 of the evaporation chamber along the flow of brine 3 9 in the direction of brine outlet 2 4, and reverses through this opening 52.
- the steam outlet 5 5 While flowing into the upper part 5 4 of the steam chamber and passing through the mist separators 6 1 and 6 2 provided in the upper part 5 4 of the steam chamber, the steam outlet 5 5 provided in the direction opposite to the opening 5 2 To mechanical vapor compression means.
- This 180 ° reorientation at the opening 52 allows the majority of the mist contained in the steam to be separated by inertia, greatly reducing the mist in the steam going to the mechanical vapor compression means. can do.
- the portion 5 1 a of the wall 51 near the nozzle 5 should have a slope starting from the upper part of the nozzle outlet so that the flow passage cross section of the lower part of the evaporation chamber 53 gradually spreads from the nozzle outlet. .
- two nearly vertical mist separators 6 1 and 6 2 are provided in the upper part 5 4 of the steam chamber so as to block the flow of steam whose direction is reversed at the opening 52.
- the mist separator 61 on the upstream side of the steam is provided with a spray cleaning device 63 for cleaning.
- the mist separator By making the mist separator almost vertical, the captured mist easily flows down along the mist separator and can be easily discharged from the discharge path 64 provided at the bottom of the mist separator. The problem that the captured mist is not discharged smoothly but re-scatters like the horizontal mist separator used in the conventional MVC 1 2 4 (see Fig. 8) can be solved.
- the cleaning spray device 63 on the upstream mist separator 61, as described above, the mist adhering to the mist separator 61 is diluted to prevent scale and pass through the mist separator. Steam overheating can be eliminated to reduce problems associated with scale deposition in mist separators 61, 62 and mechanical vapor compression means.
- the mist separator 6 1 Since the mist separator 6 1 is almost vertical, the cleaning water sprayed on the upper part of the mist separator 6 1 by the cleaning spray device 6 3 follows the mist separator. From the top to the bottom, it is washed to the bottom, and it is easily discharged from the discharge path 64.
- Fig. 2 two mist separators are provided, and one upstream is used for cleaning.
- a spray device is provided has been shown, it is possible to further increase the separation efficiency by increasing the number of mist separator cleaning spray devices.
- the spray device for cleaning 63 can divide the mist separator 6 1 to be cleaned into several sections, in the case of the figure, 4 sections, and wash the divided parts in order. I am doing so.
- the washing water injection part is divided into 4 nozzles 6 5 a, 6 5 b, 6 5 c, 6 6 d, and valves 6 6 a, 6 6 b, 6 6 c, 6 6 d is provided, and control is performed by the control device 67 so that these valves are individually opened and closed.
- valves 6 6 b is open and the other valves are closed. Washing water is sprayed only from Nozu No 6 65 b and flows down along vertical mist separator 61. The bottom is being cleaned.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP04772900.9A EP1798202B1 (en) | 2004-09-02 | 2004-09-02 | Single stage flash evaporation apparatus based on mechanical vapor compression method |
PCT/JP2004/013086 WO2006025117A1 (ja) | 2004-09-02 | 2004-09-02 | 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 |
JP2006531227A JP4592700B2 (ja) | 2004-09-02 | 2004-09-02 | 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2004/013086 WO2006025117A1 (ja) | 2004-09-02 | 2004-09-02 | 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006025117A1 true WO2006025117A1 (ja) | 2006-03-09 |
Family
ID=35999780
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/JP2004/013086 WO2006025117A1 (ja) | 2004-09-02 | 2004-09-02 | 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室 |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1798202B1 (ja) |
JP (1) | JP4592700B2 (ja) |
WO (1) | WO2006025117A1 (ja) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011092863A (ja) * | 2009-10-30 | 2011-05-12 | Hitachi Zosen Corp | 多段フラッシュ式造水装置 |
CN104709953A (zh) * | 2014-12-15 | 2015-06-17 | 北京理工大学 | 热能梯级利用的多级回热加湿除湿海水淡化装置 |
CN107108269A (zh) * | 2014-12-23 | 2017-08-29 | 无排放脱盐公司 | 用于经改善的无流出物的海水脱盐的方法和装置 |
US10676373B2 (en) | 2015-01-05 | 2020-06-09 | Husham Al-Ghizzy | Thermal utilization system and methods |
CN115403203A (zh) * | 2022-08-29 | 2022-11-29 | 青岛百发海水淡化有限公司 | 高可靠性海水淡化装置 |
CN117923578B (zh) * | 2024-03-19 | 2024-06-07 | 山东驰盛新能源设备有限公司 | 一种含高盐废水的闪蒸系统及方法 |
Families Citing this family (9)
Publication number | Priority date | Publication date | Assignee | Title |
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US20100288619A1 (en) * | 2008-01-18 | 2010-11-18 | Takashi Yabe | Energy-Saving Type Apparatus For Producing Freshwater |
FR2928276B1 (fr) * | 2008-03-10 | 2011-01-14 | Ridel | Evaporateur a compression mecanique de vapeur comportant un dispositif de detente en entree de separateur |
GB0908736D0 (en) * | 2009-05-21 | 2009-07-01 | Midttun Kulde As | Method and apparatus |
US10029923B2 (en) | 2012-04-10 | 2018-07-24 | Mgr Energy Llp | Water treatment device |
WO2014196611A1 (ja) * | 2013-06-05 | 2014-12-11 | 大川原化工機株式会社 | 濃縮装置および濃縮方法 |
WO2014196610A1 (ja) | 2013-06-05 | 2014-12-11 | 大川原化工機株式会社 | 海水淡水化装置および海水淡水化方法 |
CN107226503A (zh) * | 2017-07-24 | 2017-10-03 | 张育晗 | 一种加热冷凝一体式蒸馏水机 |
BE1024466B1 (fr) * | 2017-07-27 | 2018-02-28 | Ind Advanced Services Fz Llc | Unité de dessalement d'eau par compression mécanique de vapeur |
IT202000025609A1 (it) * | 2020-10-28 | 2022-04-28 | Gdn S R L | Distillatore per termocompressione per acqua distillata per iniettabili (wfi) |
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JPS60168582A (ja) * | 1984-02-14 | 1985-09-02 | Mitsui Eng & Shipbuild Co Ltd | 蒸気圧縮式造水装置 |
JPS62225290A (ja) * | 1986-03-28 | 1987-10-03 | Hitachi Ltd | 疎水性多孔質膜を用いた蒸留方法 |
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- 2004-09-02 EP EP04772900.9A patent/EP1798202B1/en not_active Expired - Fee Related
- 2004-09-02 JP JP2006531227A patent/JP4592700B2/ja not_active Expired - Fee Related
- 2004-09-02 WO PCT/JP2004/013086 patent/WO2006025117A1/ja active Application Filing
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US2619453A (en) | 1946-04-24 | 1952-11-25 | Andersen Rolf | Vapor-compression distillation |
JPS62241592A (ja) * | 1986-04-14 | 1987-10-22 | Mitsubishi Heavy Ind Ltd | 海水淡水化装置 |
JPH05293460A (ja) * | 1992-04-15 | 1993-11-09 | Mitsubishi Heavy Ind Ltd | 造水装置 |
JP2003521375A (ja) * | 2000-02-02 | 2003-07-15 | アクア ダイン,インコーポレイテッド | 飲用水蒸留システム |
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Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011092863A (ja) * | 2009-10-30 | 2011-05-12 | Hitachi Zosen Corp | 多段フラッシュ式造水装置 |
CN104709953A (zh) * | 2014-12-15 | 2015-06-17 | 北京理工大学 | 热能梯级利用的多级回热加湿除湿海水淡化装置 |
CN104709953B (zh) * | 2014-12-15 | 2023-03-21 | 北京理工大学 | 热能梯级利用的多级回热加湿除湿海水淡化装置 |
CN107108269A (zh) * | 2014-12-23 | 2017-08-29 | 无排放脱盐公司 | 用于经改善的无流出物的海水脱盐的方法和装置 |
JP2018505056A (ja) * | 2014-12-23 | 2018-02-22 | エフルエント フリー デザリネイション コーポレイション | 改良された流出のない海水脱塩方法及び装置 |
EP3237335A4 (en) * | 2014-12-23 | 2018-11-14 | Effluent Free Desalination Corp. | Method and apparatus for improved effluent free sea water desalination |
US10676373B2 (en) | 2015-01-05 | 2020-06-09 | Husham Al-Ghizzy | Thermal utilization system and methods |
CN115403203A (zh) * | 2022-08-29 | 2022-11-29 | 青岛百发海水淡化有限公司 | 高可靠性海水淡化装置 |
CN115403203B (zh) * | 2022-08-29 | 2023-09-15 | 青岛海水淡化有限公司 | 高可靠性海水淡化装置 |
CN117923578B (zh) * | 2024-03-19 | 2024-06-07 | 山东驰盛新能源设备有限公司 | 一种含高盐废水的闪蒸系统及方法 |
Also Published As
Publication number | Publication date |
---|---|
EP1798202A1 (en) | 2007-06-20 |
JP4592700B2 (ja) | 2010-12-01 |
EP1798202B1 (en) | 2013-07-17 |
JPWO2006025117A1 (ja) | 2008-05-08 |
EP1798202A4 (en) | 2009-03-04 |
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