JP6847474B2 - Evaporation solid-liquid separation method - Google Patents

Description

The present invention relates to an evaporative solid-liquid separation method in which seawater is evaporated at a specific temperature and a specific pressure to separate a useful and novel composition of mineral water and a salt mixture. Furthermore, the present invention relates to a mineral water and salt mixture having a novel composition obtained by using the evaporative solid-liquid separation method, and an evaporative solid-liquid separation device for the evaporative solid-liquid separation method.

Many methods are known to remove sodium chloride from seawater to obtain fresh water.
For example, Patent Documents 1 to 3 describe a desalting treatment method, a method for producing a salt concentrate, a freshwater combined water purification device, and the like using a reverse osmosis membrane.
Further, Patent Document 4 describes a method for treating seawater using a mosaic charged membrane, and Patent Documents 5 and 6 describe a method for producing a mineral component-containing composition (mineral water, etc.) using an ion exchange membrane. Has been described.

Further, for example, Patent Document 7 and the like describe devices and methods related to flash evaporation.
As a device for heating to evaporate water in seawater and liquefying the obtained water vapor, for example, Patent Document 8 describes an evaporator for a multi-effect type water maker, and Patent Documents 9 and 10 describe permeation. Evaporation equipment and water production equipment that use a membrane together are described.

However, these techniques are aimed at simply obtaining fresh water from seawater, and the obtained fresh water only needs to have its sodium chloride concentration reduced to the extent that it can be used for beverages and the like. No consideration was given to the composition of salts obtained as a residue, the presence or absence of trace elements, and the like.
That is, these conventional techniques merely secure ordinary beverages or simply secure agricultural water as a substitute for river water, and the obtained "liquid called fresh water (soft water)" can be used as, for example, cosmetics. It was not used in fields where trace components (content ratio) are important, such as (raw materials) and health foods (raw materials).

That is, there has been almost no solid-liquid separation method for seawater that can be used with an advantage even in applications where a trace amount of component composition is important.

JP-A-2007-267747 Japanese Unexamined Patent Publication No. 2015-029935 Japanese Unexamined Patent Publication No. 2016-203056 Japanese Unexamined Patent Publication No. 2006-007084 JP-A-2002-238515 Japanese Unexamined Patent Publication No. 2015-019638 Japanese Unexamined Patent Publication No. 2000-107502 Japanese Unexamined Patent Publication No. 2007-198701 Japanese Unexamined Patent Publication No. 2015-150553 Japanese Unexamined Patent Publication No. 2016-0972328

The present invention has been made in view of the above background technology, and the problem is to obtain a mineral water and salt mixture that can be used for applications in which a small component ratio is important and applications in which the presence or absence of a trace amount of components (elements) is important. To provide.

As a result of diligent studies to solve the above problems, the present inventor has "a specific pressure range" necessary for suitable evaporation solid-liquid separation while maintaining the temperature of the object at 25 ° C. or higher and 60 ° C. or lower. And (more preferably, gas discharge capacity) ”, and for the first time, we were able to realize a device that can achieve such conditions (even in industrial quantities).
And, at least during the main evaporation solid-liquid separation, as a result of applying the evaporation conditions etc. to seawater, surprisingly, a trace amount of components (elements) can remain (maintain) as natural products. We have come to the present invention by finding that water (and a salt mixture) can be obtained.

That is, the present invention is an evaporative solid-liquid separation method for separating seawater into a salt mixture and mineral water by evaporating solid-liquid separation.
At least during the main evaporation solid-liquid separation, the temperature of the seawater is maintained at 25 ° C. or higher and 60 ° C. or lower, and the pressure inside the container is maintained at 1 kPa or higher and 20 kPa or lower using a decompressor. It provides a separation method.

The present invention also provides the above-mentioned evaporation solid-liquid separation method for evaporating solid-liquid separation of seawater by performing at least all of the following operations (1) to (4).
(1) A heating operation in which the inside of the container is heated by a heating unit so that the temperature of the seawater is maintained in a temperature range of 25 ° C. or higher and 60 ° C. or lower, at least during the main evaporation solid-liquid separation.
(2) At least during the main evaporation solid-liquid separation, the water ejector is used as a decompressor to reduce the pressure, the inside of the container is maintained at 1 kPa or more and 20 kPa or less, and the seawater is cooled by the heat of vaporization of water contained in the seawater. A cooling operation that cools and maintains the temperature of the seawater in the temperature range of 25 ° C or higher and 60 ° C or lower.
(3) A liquefaction operation in which the gas flowing out of the container is liquefied using a cooler to obtain mineral water.
(4) Extraction operation of taking out the salt mixture remaining in the container from the powder outlet of the container to obtain the salt mixture.

The present invention also provides a method for producing a salt mixture and a method for producing mineral water, which are characterized by evaporating solid-liquid separation of seawater using the above-mentioned evaporation solid-liquid separation method.

Further, the present invention is an evaporation solid-liquid separation device for the above-mentioned evaporation solid-liquid separation method.
At a minimum, the present invention provides an evaporation solid-liquid separation device including a container having a stirrer, a heating unit and a powder outlet; a decompressor which is a water ejector; and a cooler.

The present invention also provides a salt mixture and mineral water, which are obtained by evaporating solid-liquid separation of seawater using the above-mentioned evaporation solid-liquid separation method.

The present invention can solve the above-mentioned conventional problems and problems, and provide mineral water containing trace components (elements) contained in natural seawater and a salt mixture close to natural seawater. it can. As a result, it is possible to provide a mineral water and salt mixture having a novel component composition that can be used for applications in which a trace amount of component composition is important.
Unlike conventional distillation, which heats to the boiling point of water (at normal pressure, etc.), there is no alteration or loss of trace components in seawater due to excessive heating, and compared to such general-purpose (normal) distillation, " Since metal ions and the like in seawater are present (residual) in the "obtained evaporation", that is, trace metal ions and the like that would be removed by the original evaporation are also contained in the "evaporated material". Therefore, with respect to "property other than the overwhelmingly large property of sodium chloride", mineral water (evaporation amount obtained by evaporation) can be obtained while having "property of natural seawater as a raw material". As a result, as a result of applying the mineral water of the present invention to an organism, an excellent effect is exerted on the organism as described later.

On the other hand, at 60 ° C. or less, sufficient vacuum (e.g., about ^1Pa a rotary pump (10 -2 mmHg)) to so as to obtain fresh water to evaporate water methods are of course known. However, such a method does not give an excellent mineral water or salt mixture as in the present invention. That is, the lower limit of pressure is important.
Moreover, while maintaining the temperature at a low temperature of 25 ° C or higher and 60 ° C or lower, the pressure is relatively high at 1 kPa or higher and 20 kPa or lower (without increasing the degree of decompression), and the amount of seawater that is industrially acceptable is industrially applied. Evaporation within a reasonable time has not been done conventionally for reasons such as the need for a special decompressor; and the result was not expected to be excellent.

Conventional evaporation of seawater emphasizes evaporation efficiency, cost reduction, etc., and secures drinking water or water for agriculture (water whose sodium chloride concentration is below a certain concentration). However, the mineral water produced by the evaporative solid-liquid separation method of the present invention has characteristics such as being adaptable to a living body, and therefore can be suitably used for high-value-added fine chemicals as described above.

The mineral water produced by the method for separating solid and liquid by evaporation of the present invention has a generally lower calcium (Ca) content than commercially available mineral water, but sodium (Na), magnesium (Mg), and potassium (K). ) Is definitely high. In addition, it is highly possible that other seawater components remain without being dissipated.

The mineral water produced by using the evaporative solid-liquid separation method of the present invention is obtained by reducing only sodium chloride (NaCl), which is the overwhelming main component thereof, from seawater, and dissipates (trace amount) components of other seawater. It remains without.
On the other hand, water obtained by evaporating seawater at 100 ° C or desalinating using a membrane includes not only sodium chloride (NaCl) but also other (trace) components (highly likely to be metal elements). It has been removed.
The mineral water of the present invention has almost no dissipated substances from "natural seawater". Therefore, it is considered that trace components (elements) necessary for the living body remain as they are.

Although the "(trace) component" has not been clarified, the growth rate of plants (vegetables, etc.) in sprinkled soil, the flavor of the vegetables; the flavor of the mineral water itself of the present invention, and the dishes using the mineral water. It is clear that the taste of vegetables and the taste of pickles; etc. are completely different from those obtained from "soil that has not been supplemented with trace components (elements) for many years". It is highly possible that the "other (trace) component" is not an organic component but a specific element (for example, a metal or a metal salt).
The (trace) components have not been specifically clarified in the present invention, but all of them have not been clarified by the current (analytical) advanced technology. The present invention gives up the approach from the identification (analysis) of the (trace) component to the above-mentioned improvement of the action on the living body, which cannot be understood by the current (analytical) technology, and uses the antibacterial agent as a natural product antibiotic. It was made by relying on seawater, which is a natural product, as it relies on.

The salt mixture produced by using the evaporative solid-liquid separation method of the present invention has extremely low sodium chloride (NaCl) content and sodium (Na) content as compared with commercially available salt (shio) (implementation). See example). On the other hand, the salt mixture produced by using the evaporative solid-liquid separation method of the present invention has a magnesium (Mg) content, a calcium (Ca) content, and potassium (C) as compared with a commercially available salt (salt). The content of K) is also high (see Examples).

Since both the mineral water, which is the evaporated component produced by using the evaporative solid-liquid separation method of the present invention, and the salt mixture, which is the residue thereof, have a novel composition and water structure, for example, cosmetics such as drinking water. Foods (raw materials); health foods (raw materials); general foods (raw materials) such as pickles and drinking water, water for agricultural products; water for cultivation of fish etc. (raw materials); etc. The content ratio) can be used particularly preferably for applications that affect (and therefore become important) its performance.

The fact that the mineral water and salt mixture produced by the method for separating solid and liquid evaporation of the present invention will each have a novel composition, a cluster structure of water, etc., is actually observed when used for the above purpose. It has been confirmed by showing a flavor different from that of conventional products and an effect on humans (skin, etc.).
The difference in "taste and odor" (flavor) that can be perceived by humans and the difference in the effect on humans (skin), etc. exceed the current ability of instrument analysis (below the detection limit). ) Is a common general technical knowledge, it is impossible or almost impractical to directly specify the trace component or delicate component content ratio showing the excellent effect (“impossible / impractical circumstances””. There is).

It is the schematic which shows one form of the apparatus used in this invention. It is schematic cross-sectional view which shows one form of the container, the cooler, the recovery container and the like provided in the apparatus used in this invention. It is a schematic perspective view which shows one form of the stirrer which the container provided in the apparatus used in this invention has. It is schematic cross-sectional view which shows one form of the horizontal injection type water ejector which is a preferable decompressor provided in the apparatus used in this invention. It is a schematic cross-sectional view which shows one form of a horizontal injection type water ejector, a water tank, a circulation pump and the like which are preferable decompressors provided in the apparatus used in this invention.

Hereinafter, the present invention will be described, but the present invention is not limited to the following specific aspects, and can be arbitrarily modified within the scope of the technical idea.

The evaporative solid-liquid separation method of the present invention is an evaporative solid-liquid separation method in which seawater is separated by evaporative solid-liquid separation into a salt mixture and mineral water, and the temperature of the seawater is adjusted at least during the main evaporative solid-liquid separation. It is characterized in that the temperature in the container is maintained at 1 kPa or more and 20 kPa or less by using a decompressor while maintaining the temperature at 25 ° C. or higher and 60 ° C. or lower.

The evaporative solid-liquid separation device used in the present invention is an apparatus whose use is limited to the "evaporative solid-liquid separation method of the present invention". The evaporative solid-liquid separator used in the present invention is an evaporative solid-liquid separator having the ability to be used in the evaporative solid-liquid separation method of the present invention, and is at least a container having a stirrer, a heating unit and a powder outlet; It is equipped with a decompressor (preferably a decompressor which is a water ejector); and; a cooler.

A preferred example of the apparatus used in the present invention is at least, as shown in FIGS. 1 and 2, for example.
It has a stirrer 110 for stirring the seawater A, a heating unit 120 for heating the inside of the seawater A and the container 100, a gas outlet 130 for taking out the gas generated from the seawater A, and a powder outlet 140 for taking out the salt mixture B after the treatment. Container 100;
A cooler 200 that cools the gas taken out from the gas outlet 130;
Decompressor 300 that decompresses the inside of the container 100;
It is provided with a recovery container 400; which collects the liquefied mineral water C cooled by the cooler 200.

The evaporative solid-liquid separation method of the present invention preferably performs at least all of the following operations (1) to (4).
(1) A heating operation in which the inside of the container is heated by a heating unit so that the temperature of the seawater is maintained in a temperature range of 25 ° C. or higher and 60 ° C. or lower, at least during the main evaporation solid-liquid separation.
(2) At least during the main evaporation solid-liquid separation, the water ejector is used as a decompressor to reduce the pressure, the inside of the container is maintained at 1 kPa or more and 20 kPa or less, and the seawater is cooled by the heat of vaporization of water contained in the seawater. A cooling operation that cools and maintains the temperature of the seawater in the temperature range of 25 ° C or higher and 60 ° C or lower.
(3) A liquefaction operation in which the gas flowing out of the container is liquefied using a cooler to obtain mineral water.
(4) Extraction operation of taking out the salt mixture remaining in the container from the powder outlet of the container to obtain the salt mixture.

The particularly preferable method for producing the salt mixture B and the mineral water C by evaporating solid-liquid separation of the seawater A of the present invention is not limited to the following, but is specifically carried out as follows, for example.

First, at the start of the operation, the cooling water supply device is filled with cooling water, and the cooling water is circulated in the cooler 200. Next, the seawater A is poured into the container 100 from the seawater inlet 103, and the lid 104 is closed.
After the seawater A is put into the container 100, if necessary, the stirrer 110 is rotated to perform a stirring operation for stirring the seawater A in the container 100. The stirring operation and the (particularly) preferable conditions and structure of the stirring machine 110 will be described later.
Next, a heating operation is performed in which the inside of the container 100 is heated by the heating unit 120 so that the temperature of the seawater A is maintained in a temperature range of 25 ° C. or higher and 60 ° C. or lower, at least during the main evaporation solid-liquid separation.

In the present invention, the "main evaporation solid-liquid separation" means from the initial stage of the evaporation solid-liquid separation operation until 70% by mass or more of the seawater put into the container is evaporated solid-liquid separation. Further, preferably 80% by mass or more, more preferably 90% by mass or more, particularly preferably 98% by mass or more may be maintained under specific temperature conditions and specific pressure conditions described later until the evaporation solid-liquid separation is performed. desirable.

Heat is applied from the outside by supplying heating steam from the steam supply device into the steam chamber 121. A heating unit 120 for heating the seawater A and the inside of the container 100 is installed in the container 100, and in the heating unit 120, the steam heated by the steam supply device 122 is transferred to the container 100 (preferably the lower half of the container 100). It is sent to a steam chamber installed around the cylindrical portion 101).

The heat applied to the container 100 is transferred to the seawater A, and the seawater A is agitated by the stirrer 110 or by boiling, so that the water in the seawater A evaporates and the (concentrated) seawater A The temperature, concentration, viscosity, etc. become uniform.
In the present invention, it is preferable to maintain the temperature of seawater A at 25 ° C. or higher and 60 ° C. or lower, and distill off at a pressure equal to or slightly lower than the vapor pressure of water at that temperature (for example, a pressure 10% lower). At that time, seawater A boils. Therefore, since stirring is performed by the boiling, the stirrer 110 is not essential, but it is preferable that the stirrer 110 is present for more uniform temperature transfer, final extraction, and the like.

Seawater A is heated by appropriately adjusting the temperature and amount of the heating steam sent into the steam chamber 121.
On the other hand, by adjusting the amount, pressure, injection speed, etc. of water supplied to the water ejector 301 of the decompressor 300 to appropriately set the gas discharge capacity and the pressure in the container 100, and adjusting the evaporation rate. Seawater A is cooled by the heat of vaporization.
That is, at least during the main evaporation solid-liquid separation, the inside of the container 100 is maintained at 1 kPa or more and 20 kPa or less, the seawater A is cooled by the heat of vaporization of water contained in the seawater A, and the temperature of the seawater A is adjusted. Maintain in the temperature range of 25 ° C. or higher and 60 ° C. or lower.

By setting the gas discharge capacity of the decompressor 300 to "a normal pressure volume of 20 m ^{3 / hour or more when converted to a container having an internal volume of 1 m 3} ", the seawater A is rapidly heated by the heating unit 120. Even if the temperature is about to rise, the temperature of the seawater A can be lowered to a predetermined temperature or lower by the heat of vaporization of the water in the seawater A.

The actual volume of the container 100 is not particularly limited, but the range is important from the viewpoint of whether or not the conditions for evaporation solid-liquid separation in the present invention are effective.
The maximum input capacity (L) of seawater A, that is, the bulk (L) of seawater A that can be input, is preferably 20 L or more and 5000 L or less, preferably 35 L or more and 4000 L or less, and particularly preferably 50 L or more and 3000 L or less. The maximum input capacity (L) of seawater A is preferably substantially equal to the volume of the lower semi-cylindrical portion 101 of the container 100 described above.

When the actual volume of the container 100 or the volume of the lower semi-cylindrical portion 101 of the container having the shape shown in FIGS. 2 and 3 is too small, the amount of processing at one time becomes too small and the cost increases. Therefore, it cannot be used commercially. In addition, the meaning of applying the special evaporative solid-liquid separation conditions (pressure in the container, gas discharge capacity, etc.) and the device (stirring machine, decompressor, etc.) described above or described later in the present invention may be diminished.
On the other hand, if it is too large, the decompressor 300 that can exert the above-mentioned effect of the present invention is absent or extremely expensive so that it is not realistic; in particular, the temperature rise of seawater A can be suppressed by the heat of vaporization of water. When the decompressor 300 having "gas discharge capacity and decompression degree commensurate with the size of the container" does not exist or becomes extremely expensive as unrealistic; when the decompression load is excessively applied to the housing of the container 100; etc. ..

The mass of seawater A that evaporates and solid-liquid separates in one treatment is not particularly limited because it depends on the volume of the container 100 used, but is preferably 5 kg or more and 300 kg or less, more preferably 20 kg or more and 200 kg or less, and 30 kg or more and 100 kg. The following are particularly preferred.
If it is too small or too large, the same thing as when the above-mentioned "volume of the container 100 or the lower semi-cylindrical portion 101" is too small or too large may occur.
In particular, when the amount of seawater A is too small, there are (preferable) requirements / features such as "pressure during main evaporation solid-liquid separation", decompressor type, gas discharge capacity, and utilization of heat of vaporization for cooling in the present invention. It may not be used. The present invention is particularly effective when the amount of seawater A is equal to or higher than the above lower limit.

In the evaporative solid-liquid separation method of the present invention, when the volume of the container is V [L] and the mass of seawater A charged into the container is M [kg], V [L] is M [kg]. ] Is preferably set to 2 times or more and 5 times or less, more preferably 2.2 times or more and 3.5 times or less, and particularly preferably 2.5 times or more and 3.0 times or less.
If the value of V [L] / M [kg] is too small, stirring, evaporation, etc. may not be performed well. On the other hand, if the value of V [L] / M [kg] is too large, the large container 100 is wasted; the container 100 is too large to fully exert the gas discharge capacity of the decompressor 300, and as a result. , The seawater A cannot be cooled by the heat of vaporization, and the temperature of the seawater A exceeds the upper limit of the temperature range; etc. Further, if it is too small or too large, the same thing as when the above-mentioned "volume of the container 100 or the lower semi-cylindrical portion 101" is too small or too large may occur.

In this way, the heating operation for the seawater A by the heating unit 120 and the cooling operation for the seawater A by the decompressor 300 are performed, and the temperature of the seawater A is set to a range of 25 ° C. or higher and 60 ° C. or lower (further, a more preferable range described later). Maintain in a particularly preferable range).
The container 100 is provided with a vacuum gauge 108 for measuring the pressure (decompression degree) in the container 100 and thermometers 109a and 109b. These are provided for measuring the pressure (decompression degree) and temperature in the container 100 and indirectly measuring the temperature of seawater A, and also determine the start and end of the operation of evaporation solid-liquid separation. Also provided to do.
The thermometers 109a and 109b are installed so that the temperature of the seawater A can be accurately measured by utilizing the heat conduction of the container 100 (including the stirrer 110). That is, even if the seawater A is about to be rapidly cooled by the heat of vaporization of water, or conversely, even if the seawater A is about to be rapidly heated by the heating unit 120, the temperature of the seawater A is sufficiently accurately measured. It can be so.

In the present invention, it is essential to maintain the temperature of the seawater A at 25 ° C. or higher and 60 ° C. or lower, at least during the main evaporation solid-liquid separation, but preferably 27 ° C. or higher and 50 ° C. or lower, more preferably 29 ° C. It is maintained at 45 ° C. or higher, more preferably 31 ° C. or higher and 40 ° C. or lower, and particularly preferably 33 ° C. or higher and 37 ° C. or lower.

If the temperature is too low, considering the commercial or industrial scale, the evaporation solid-liquid separation will take too long; up to a low pressure adapted to the low vapor pressure of water at low temperatures, "commercial". When there is no "decompressor" that can increase the degree of vacuum (decompression degree) while having a large gas discharge capacity that sufficiently corresponds to the amount of seawater A on a scale or industrial scale; is there.

On the other hand, if the temperature is too high, the evaporated content will be similar to or similar to that of fresh water (soft water) produced by the conventional distillation method, and the residue will have a component composition similar to or similar to that of the natural salt produced by the conventional production method. In some cases, the effect of the present invention may not be exhibited.

In the present invention, by defining the lower limit of the temperature of seawater A, the salt mixture B and the mineral water C can be produced in an allowable treatment time (operation time) even in a commercial amount.
On the other hand, by defining the upper limit of the temperature of seawater A, unlike the conventional "distilled water of seawater" and the conventional "natural salt by evaporative dryness of seawater", a new component composition can be obtained.
If the temperature is too high, the resulting salt mixture B or mineral water C may be similar to or similar to the conventional one, and as a result, specifically, for example, the obtained salt mixture. The flavor of the "foods such as pickles" used was not improved, the flavor of fish cultivated in water in which the obtained salt mixture was dissolved was not improved, or the obtained mineral water was sprinkled (watered) on the agricultural products. In some cases, the flavor may not be improved.

The container 100 is provided with a gas outlet 130 for taking out the gas generated from the seawater A. It is preferable that the vicinity of the gas outlet 130 is also maintained in the temperature range by sufficient heat conduction or the like so that water droplets do not occur (condensation does not occur) in the vicinity of the gas outlet 130.

A liquefaction operation is performed in which the gas flowing out of the container 100 is liquefied using the cooler 200. In the evaporative solid-liquid separation method of the present invention, for example, as shown in FIG. 1, a cooler 200 for cooling the gas taken out from the gas outlet 130 provided in the container 100 is provided behind the container 100. It is preferable to liquefy and depressurize the inside of the container 100.
As the cooling medium of the cooler 200, water having a temperature of "10 ° C. or higher, which is 5 ° C. or higher (particularly preferably 7 ° C. or higher) lower than the temperature of the gas taken out from the gas outlet 130 of the container 100". Is preferable from the viewpoint of efficiency of cooling and liquefying.
If the temperature of water, which is a cooling medium, is too high, a part of the gas may not be liquefied. As such a cooler 200, a known one can be used.

In the present invention, at least during the main evaporation solid-liquid separation, the water ejector 301 is used as a decompressor 300 to reduce the pressure, the inside of the container 100 is maintained at 1 kPa or more and 20 kPa or less, and the water contained in the seawater A evaporates. The seawater A is cooled by heat, and a cooling operation is performed to maintain the temperature of the seawater A in a temperature range of 25 ° C. or higher and 60 ° C. or lower.

The device used in the present invention is provided with a decompressor 300 for decompressing the inside of the container 100 behind the cooler 200, for example, as shown in FIG.
As shown in FIG. 1, the decompressor 300 is preferably a water ejector 301, and the water ejector 301 is particularly preferably a horizontal injection type water ejector 301 having a water circulation pump.
In the case of a water ejector 301, particularly a horizontal injection type water ejector 301 having a water circulation pump, the degree of decompression (pressure in the container) is optimal if the vapor pressure of water and the boiling point of water under decompression are taken into consideration. Regarding the gas discharge capacity, the water ejector 301, particularly the horizontal injection type water ejector 301 having a water circulation pump, is most suitable because the capacity is extremely large.

By sucking with the decompressor 300, the gas in the container 100, that is, water vapor and air containing minerals and the like in the seawater A are sucked through the gas pipe 131, and the water contained in the seawater A in the container 100 is sucked. Evaporate other components (metal ions, etc.).
At that time, the pressure (decompression degree) in the container 100 is adjusted by adjusting the amount and suction force of suction by the decompressor 300. When the water ejector 301 is used as the decompressor 300, the diameter of the injection nozzle, the injection amount and temperature of the water to be injected, the size of the water ejector 301 itself, etc. are adjusted so as to have a sufficient gas discharge capacity described later. Keep the inside of the container 100 at a predetermined pressure (range).

The decompressor 300 is converted into a case where a container having ^{an internal volume of 1 m 3} is used so that the temperature of seawater A does not exceed 60 ° C. (preferably not exceeding 45 ° C.) due to the heat of vaporization of water. Therefore, it is preferable to use one having a gas discharge capacity of 20 m ^{3 / hour or more at normal pressure.}

If the internal volume of the container 100 is large, it is necessary to use the decompressor 300 having a large gas discharge capacity. When the decompressor 300, which has a small gas discharge capacity compared to the internal volume of the container 100, is used (the gas discharge capacity must be increased according to the internal volume of the container 100), seawater A is generated by the heat of vaporization of water. It becomes difficult to cool the gas, and the temperature of the seawater A may rise.

Specifically, for example, when a container having an internal volume of 1 m ³ is used, a water ejector 301 having a gas discharge capacity of ^{20 m 3} / hour or more at an atmospheric pressure is preferable, and a container having ^{an internal volume of 0.1 m 3 is used.} When used, a water ejector 301 having a gas discharge capacity of ^{2 m 3} / hour or more at a normal pressure volume ^{is preferable, and when a container having an internal volume of 0.5 m 3} is used, a gas having a normal pressure volume of 10 m ³ / hour or more is used. A water ejector 301 having a discharge capacity is preferable, and ^{when a container having an internal volume of 2 m 3} is used, a water ejector 301 having a gas discharge capacity of a normal pressure volume of 40 m ^{3 / hour or more is preferable.}

"Gas discharge capacity with a normal pressure volume of 20 m ³ / hour or more when converted to a container having an internal volume of 1 m ³ " is preferable, but the value is such that the normal pressure volume is 22 m ³ / hour or more and 300 m ³ / hour. The following is more preferable, a normal pressure volume of 25 m ³ / hour or more and 200 m ³ / hour or less is further preferable, and a normal pressure volume of 27 m ³ / hour or more and 150 m ³ / hour or less is particularly preferable.
If the gas discharge capacity of the decompressor 300 is too small, the treatment time may be long, or it may be difficult to obtain the effect of preventing the seawater A from overheating due to the heat of vaporization of water, and the temperature of the seawater A may rise too much. is there.
If the gas discharge capacity of the decompressor 300 is too large, the decompressor 300 having such a large gas discharge capacity while achieving the following degree of decompression may not exist, or may be extremely expensive or extremely large. is there.

As an example shown in FIG. 1, water (preferably water previously cooled by a water chilling unit) is stored in a water tank 303, pressurized water is sent by a water circulation pump 302, and the pressurized water is sent by a water ejector 301. The pressure is reduced by ejecting. A fluid liquid exhausts a gas such as water vapor using the property that the pressure is lower than that of a static liquid (Bernoulli's theorem).

The pressure inside the container (decompression degree) by the decompressor 300 is preferably 0.1 times or more and 1 times or less, and 0.2 times or more and 0.99 times the vapor pressure at the temperature of seawater A, at least during the main evaporation solid-liquid separation. The following is more preferable, 0.4 times or more and 0.95 times or less is further preferable, and 0.6 times or more and 0.9 times or less is particularly preferable.
When the pressure inside the container is equal to or higher than the above lower limit, a decompressor having such a capability can be realized. In addition, there is no cooling of seawater A due to excessive heat of vaporization. On the other hand, when the pressure inside the container is not more than the above upper limit, the seawater A boils gently and distilling is efficient.

Specifically, the pressure inside the container (decompression degree) by the decompressor 300 is at least 1 kPa (-100.3 kPa with respect to 1 atm (101.3 kPa)) or 20 kPa (1) during the main evaporation solid-liquid separation. It is indispensable to maintain the temperature below -81.3 kPa) with respect to the atmospheric pressure (101.3 kPa) for evaporation solid-liquid separation.
The pressure in the container 100 is maintained at 1.5 kPa (-99.8 kPa for 1 atm (101.3 kPa)) or more and 15 kPa (-86.3 kPa for 1 atm (101.3 kPa)) or less. It is preferable to do so.
More preferably, it is 2 kPa (-99.3 kPa with respect to 1 atm) or more and 10 kPa (-90.3 kPa with respect to 1 atm) or less.
More preferably, it is 2.5 kPa (-98.8 kPa with respect to 1 atm) or more and 8.6 kPa (-92.7 kPa with respect to 1 atm) or less.
Particularly preferably, it is 3.3 kPa (-98 kPa with respect to 1 atm) or more and 8.3 kPa (-93 kPa with respect to 1 atm) or less.

If the pressure inside the container (decompression degree) is too low (if the pressure is too high), cooling of seawater A due to the heat of vaporization of water cannot be expected, and if the temperature of seawater A becomes too high, it takes time for evaporation solid-liquid separation. As a result, the obtained salt mixture or mineral water may be similar to or similar to the conventional one. Specifically, for example, the same thing as when the temperature is too high may occur.

On the other hand, when the pressure inside the container (decompression degree) is too high (when the pressure is too low), the relationship between the "boiling point of water at the pressure" and the "essential temperature range or preferable temperature range of seawater" described below is determined. It may not be necessary to reduce the pressure to that extent, and it has the above-mentioned gas discharge capacity and has the above-mentioned gas discharge capacity after satisfying the above-mentioned lower limit of the amount of one-time seawater treatment that is commercially applicable. In some cases, there is no decompressor 300 capable of increasing the degree of decompression to that extent, or it is unrealistically extremely large and expensive.

The temperature dependence of the vapor pressure of water is shown below.
Water temperature (° C) Water vapor pressure (kPa)
15 1.7
20 2.3
25 3.2
30 4.2
35 5.6
40 7.4
45 9.6
50 12.3
55 15.7
60 19.9
65 25.0

The decompressor 300 is preferably a horizontal injection type water ejector 301 having a water circulation pump 302 because it has a high degree of decompression and a high gas discharge capacity. That is, it is preferable because the degree of decompression and the gas discharge capacity can be compatible with each other and the effect of the present invention can be easily exerted. If the water circulation pump 302 is provided and is a horizontal injection type, it is particularly easy to increase the gas discharge capacity.

The decompressor generally includes a rotary pump, an oil diffusion pump, a mercury diffusion pump, a differential pump, and the like. For example, a rotary pump to about ^1Pa (10 -2 mmHg), a high degree of vacuum both of about the oil diffusion pump ^0.1mPa (10 -6 mmHg) is very low gas discharge ability of what can be achieved. On the other hand, with a commercially available or general ejector, the pressure may usually be higher than 20 kPa (the degree of decompression cannot be increased).

The compatibility between the gas discharge capacity and the degree of decompression can be achieved only by the "water ejector 301", and in particular, the compatibility can be preferably achieved by using the horizontal injection type water ejector 301 having the water circulation pump 302.
Although the above-mentioned high gas discharge capacity value can be achieved by the water ejector 301, it is not a general-purpose value. The above-mentioned numerical value of high gas discharge capacity can be obtained by adjusting the temperature of the water to be injected, the diameter of the injection nozzle, the injection speed, the injection amount per unit time, the injection distance, and the like.

A particularly preferable aspect of the "horizontal injection type water ejector" in the present invention is shown in FIGS. 4 and 5.
The "horizontal injection type water ejector" shown in FIGS. 4 and 5 is provided on the cylindrical drive water inlet piece 1 that receives the drive water and the downstream side of the drive water inlet piece 1, and is provided on the downstream side of the drive water inlet piece 1. It has a main pipe throat 6 that mixes the driving water flowing in from 1 and suction gas, and an output piece 7 that is connected to the downstream end of the main pipe throat 6 and has a divergent inner diameter. There is.
Further, if necessary, a silencer 12 having a cylindrical shape and provided at the downstream end of the output piece 7 to flow a mixed gas of the driving water and the suction gas, and a silencer 12 attached to the silencer 12 to allow the driving water to flow. It is provided with an intake pipe 11 that takes in air into the silencer 12 when it flows out and prevents a sudden change in air pressure in the silencer 12.

Further, in the water ejector 301 described above, the outer cover pipe 8 for accommodating the drive water inlet piece 1, the main pipe throat 6 and the output piece 7 is provided, and the suction pipe 3 for supplying the suction gas to the outer cover pipe 8 is provided. Attached, the outer cover pipe 8 is connected to the silencer 12, and the main pipe throat 6 is composed of a cylindrical pipe provided in connection with the terminal portion of the drive water inlet piece 1 and having a plurality of gas suction holes 4.

A circulation pump 16 including a circulation pump 16 that sucks water from the water tank 303 and discharges it from the drive water inlet piece 1, the drive water inlet piece 1, the main pipe throat 6, the output piece 7, and the silencer 12. It is preferable that the path is set lower than the water level 17 in the water tank 302.

FIG. 4 shows an outline of the water ejector 301 and the silencer 12 connected to the water ejector 301, and FIG. 5 shows a form in which the water ejector 301 is installed in the lateral direction and connected to the water tank 303. In the water ejector 301 of FIG. 4, the driving water inlet piece 1 is chamfered in order to reduce the flow resistance of water.

A main pipe throat 6 having a diameter larger than that of the driving water inlet piece 1 is connected to the inlet piece 1. The shape of the main pipe throat 6 is a simple pipe shape.
A plurality of suction holes 4 penetrating the pipe pipe wall are formed at the inlet of the main pipe throat 6, and the suction holes 4 draw suction gas when vacuuming (depressurizing) through the suction pipe 3. It is for sucking into the main pipe throat 6.

Near the end of the main throat 6, a pipe-shaped protruding piece 7 having a diameter larger than that of the main throat 6 is connected. The outlet piece 7 has an internal shape that spreads divergently toward the outlet.
Further, the driving water inlet piece 1, the main pipe throat 6, and the outer pipe 8 covering the outlet piece 7 are connected to the outside in a cylindrical shape. The water ejector 301 is composed of the members shown in 1 to 8.
Reference numeral 12 denotes a silencer, and as shown in FIG. 4, the inner diameter of the silencer 12 has a pipe shape larger than the inner diameter of the outlet of the output piece 7 of the water ejector 301.

A discharge pipe 15 from the circulation pump 16 shown in FIG. 5 is connected to the water ejector inlet piece 1 shown in FIG. 4 via an inlet side flange 2.
A hollow circular partition plate 5 is provided so that the evacuation function is performed only through the suction pipe 3. The inner portion of the partition plate 5 is fixed to the outer portion of the main pipe throat 6, and the outer peripheral portion of the partition plate 5 is fixed to the outer tube 8 to maintain sufficient airtightness.

As shown in FIG. 5, the decompressor 300 in the present invention includes a water tank 303 containing water for immersing the silencer 12 in order to achieve an extremely high gas discharge capacity of the water ejector, and was used in the water ejector 301. The driving water has a structure that is once stored in the water tank 303.
The water ejector 301 is fixed from the outside of the water tank 303 by using the output side flange 9 at the end thereof.
The silencer 12 is fixed at the same position as the output side flange 9 from the inside of the water tank 303 by the flange 10. As a result, in the water tank 303, the water ejector 301 and the silencer 12 are connected inside the water tank 303.

The silencer 12 has a horizontal portion 12a and a vertical portion 12b bent downward at a right angle at the tip thereof, and the driving water mixed with the suction gas flows out from the terminal 12c into the water in the water tank 303. It has become.
Further, the drive water is circulated and reused through the return pipe 14 connected to the circulation pump 16 that creates a water flow.
The circulation path including the return pipe 14, the circulation pump 16, the discharge pipe 15, the water ejector 301, and the silencer 12 is set lower than the water level 17 in the water tank 303.

An intake pipe 11 for taking in air is provided near the connecting portion of the water ejector 301 in the silencer 12, and the intake port of the intake pipe 11 is positioned above the water level 17 of the water tank so that the intake port is below the water surface. The structure should not be soaked. The water tank 303 is provided with an overflow ventilation port 18 for setting the water level 17.

As shown in FIG. 4, the preferred water ejector 301 in the present invention is provided with a suction hole 4 in the main throat 6. As a result, it has a higher (larger) gas discharge capacity than a conventional ejector that sucks gas through the gap between pipes.

Further, as shown in FIG. 5, the preferred water ejector 301 of the present invention and the silencer 12 connected to the water ejector 301 have a water circulation path lower than the water level 17 of the water tank 303, and can be used and installed sideways and horizontally. The "horizontal injection type water ejector having a water circulation pump" has a higher (larger) gas discharge capacity than a decompressor such as a conventional ejector.

The outflow rate when the gas flowing out of the container 100 is liquefied using the cooler 200 to obtain the mineral water C is determined by giving priority to the temperature and pressure, but also the size of the container 100 and the container. Although it depends on the amount of seawater A in the container, it is preferably 3 to 50 L / hr, more preferably 10 to 40 L / hr, and particularly preferably 20 to 30 L / hr. "L" is the volume of the obtained mineral water C.

In the evaporation solid-liquid separation method of the present invention, the pressure (decompression degree) in the container 100 is made lower than necessary with respect to the vapor pressure in consideration of the vapor pressure of water at the "optimal temperature in the evaporation solid-liquid separation of seawater". Regardless of what was done, it was achieved (completed) on an industrial (commercial) scale for the first time by cooling seawater A with the heat of vaporization by allocating that amount to improving the gas discharge capacity.

"Seawater" and "a liquid obtained by evaporating water or the like in the seawater to have a high viscosity" are preferably boiled at least during the main evaporation solid-liquid separation, so stirring is not essential, but stirring is not essential. Is preferable.
The stirrer may be a horizontal blade type or a screw type, but preferably, a stirrer 110 as shown in FIG. 3 is used, and the stirrer is agitated by the rotating recesses 113a and 113b and the fixed convex portion 111. Is particularly preferable.

During the evaporation operation, the stirrer 110 is rotated in the rotation direction of the arrow R in FIGS. 2 and 3, and the seawater A in the container 100 is agitated between the rotating recesses 113a and 113b and the fixed convex portion 111. Seawater A is agitated.
The stirring is performed by "rotary recesses 112a and 112b having a plurality of rotary recesses 113a and 113b" and "a plurality of fixed convex portions 111 provided on the inner surface of the container 100 (preferably the lower inner surface of the lower semi-cylindrical portion 101)". It is particularly preferable to carry out the above-mentioned effect in the container 100 provided with the above-mentioned effect.

For example, FIG. 3 is a perspective view showing the configuration of the stirrer 110, in which the stirrer 110 is rotated by a motor provided outside the container 100 and rotates on the end walls 105a and 105b of the container 100. The central axis is composed of the left and right end plates 106a and 106b that are possibly supported, and the rotating recesses 112a and 112b that are fixed at both ends between the tips and have the shape of a dogleg 115. It is configured to have a structure that does not have (a structure that can rotate without a central axis). The device shown in FIG. 3 has two rotating recesses (112a and 112b), but may have one rotating recess 112.

By making the rotating recesses 112a and 112b substantially in the shape of a dogleg, the seawater A can be easily agitated, and the salt mixture B can be satisfactorily scraped from the inner wall of the container 100 after the operation of the evaporation solid-liquid separation is completed. , The salt mixture B can be preferably obtained from the powder outlet 140 with good yield by scraping toward the powder outlet 140 (located substantially in the center of the lower side of the container 100).

In the evaporation solid-liquid separation method of the present invention, the stirrer 110 has two or more rotating recesses, and the seawater A is agitated by rotating the rotating recesses in the same direction, and after the evaporation solid-liquid separation. Preferably scrapes the salt mixture B from the inner wall of the container 100 and scrapes it toward the powder outlet.

The rotation speed of the stirrer 110, that is, the rotation speed of the left and right end plates 106a and 106b rotatably supported by the left and right end walls 105a and 105b of the container 100 is 1 rotation / minute or more and 8 rotations / minute or less. Preferably, 2 rotations / minute or more and 6 rotations / minute or less are more preferable, and 4 rotations / minute or more and 5 rotations / minute or less are particularly preferable.
When the rotation speed is too low, the efficiency of stirring may deteriorate, the temperature of seawater A may be uneven, etc. On the other hand, when the rotation speed is too high, the stirrer 110 may be overloaded. is there.

The method for separating evaporative solids and liquids of the present invention is not limited, but the lower part of the container 100 has a cylindrical shape, has a plurality of fixed convex portions 111 on the inner wall thereof, and has one stirrer 110. By having the rotary recesses 112a and 112b having the plurality of rotary recesses 113a and 113b and rotating the rotary recesses 112a and 112b, the seawater A in the container 100 is supplied to the fixed convex portion 111 and the rotary recess 113a. , 113b and preferably agitate.

Reference numeral 111 in FIG. 3 is a plurality of fixed convex portions fixed to the inner surface of the lower semi-cylindrical portion 101. Rotating recesses 114a and 114b for passing through the portion of the fixed convex portion 111 are formed, and rotary recesses 113a and 113b for stirring seawater A with the fixed convex portion 111 are provided on both sides of the groove. ing.
In addition, in FIG. 3, the fixed convex portion 111 and the rotary concave portions 113a and 113b are arranged so as to be displaced in the circumferential direction so that the meshing is sequentially performed by shifting the time, thereby driving the motor of the stirrer 110. The momentary increase in power of the car is prevented.

The logarithm of the rotary recesses provided in one rotary recess depends on the size of the container 100, the stirrer 110, the rotary recesses 112a and 112b, and the type of seawater A to be separated by evaporation solid liquid. It is preferable that one rotating recess body is provided with 5 pairs or more and 20 pairs or less, and 8 pairs or more and 14 pairs or less are particularly preferable.
If the number of rotating recesses provided in one rotating recess is too small, the efficiency of stirring may deteriorate, evaporation may be suppressed and the temperature may rise, etc. On the other hand, if the number is too large, excessive stirring may occur. Therefore, when a load is applied to the rotation, the evaporation rate may increase too much and the temperature of the seawater A may decrease too much due to the heat of vaporization of water.

The logarithm of the rotary recesses provided in the rotary recess body is assumed to be a pair of rotary recesses in one rotary recess groove. For example, in FIG. 3, since 10 rotary recess grooves are provided in one rotary recess body, 10 pairs of rotary recesses are provided in one rotary recess body.

At the end of the operation, a take-out operation is performed in which the salt mixture B in the container 100 is taken out from the powder outlet of the container 100. The stirrer 110 in the present invention can preferably agitate seawater A and preferably scrape the obtained salt mixture B from the container 100 by the special structure of two or more rotating recesses of the stirrer 110. , It is preferable that the powder can be preferably scraped toward the powder outlet 140.

The time required for the main evaporation solid-liquid separation (from the initial stage of the evaporation solid-liquid separation operation until 90% by mass of the water in the seawater charged into the container is separated by evaporation solid-liquid) also depends on (proportional) to the input amount. However, (in terms of 30 kg of seawater to be added) is preferably 1 hour or more and 20 hours or less, more preferably 2 hours or more and 13 hours or less, and particularly preferably 3 hours or more and 8 hours or less.

If the time is too short, cooling by the heat of vaporization of water may not be possible and the temperature may rise excessively. In addition, on a full-scale production scale, there is a case where there is no decompressor that can evaporate water in a short time at a relatively low temperature of 60 ° C. or lower (preferably the temperature or lower), or the size becomes extremely large, which is not realistic. ..
On the other hand, if the time is too long, the time may be wasted and the cost may increase. In addition, the meaning of applying the special evaporative solid-liquid separation conditions (pressure and temperature in the container, gas discharge capacity, etc.) and the device (agitator, decompressor, etc.) described above or later in the present invention may be diminished. In other words, there are cases where the (preferable) requirements / characteristics of using the heat of vaporization (endothermic) due to the "main pressure during solid-liquid separation of evaporation", the type of decompressor, the gas discharge capacity, etc. in the present invention for cooling are not utilized. is there.

The evaporative solid-liquid separation method of the present invention described above may be a batch type (batch type) or a continuous type. In the case of the batch type (batch type), the operation can be reliably performed, and in the case of the continuous type, the operation can be smoothly performed.
In the case of seawater A, since the bulk density of the salt mixture B is large, it is difficult for the container 100 to fill up, so a continuous type is also preferable. In the case of the continuous type, the seawater A is continuously fed into the container 100 while keeping the pressure in the container 100 within the above range.

The container 100 is provided with a powder outlet 140 for taking out the salt mixture B. As shown in FIG. 3, the powder outlet 140 is preferably provided substantially in the lower center of the container 100 (near the lower center of the lower semi-cylindrical portion 101).
Evaporation solid-liquid separation by forming the stirrer 110 as described above, that is, by forming the rotating recesses 112a and 112b into the shape of a dogleg 115a and 115b as shown in FIG. The finished salt mixture B can be easily collected in the lower center of the container 100, and the salt mixture B can be easily taken out. Therefore, the powder outlet 140 may be provided near the lower center of the container 100. preferable.
The rotary recesses 112a and 112b having such a shape satisfactorily scrape the salt mixture B from the inner wall of the container 100 and satisfactorily scrape the salt mixture B toward the powder outlet 140 provided near the center of the lower portion of the container 100 to obtain a yield. A good (smooth) salt mixture B can be obtained.

After most of the vapor of the recovered liquid has discharged from the gas outlet 130 of the container 100, that is, after the above-mentioned "main evaporation solid-liquid separation" is completed, the temperature inside the container 100 is set higher than the above upper limit temperature. It is also preferable to completely evaporate the water to achieve good pulverization.

The present invention is also a salt mixture characterized in that it is obtained by evaporating solid-liquid separation of seawater using the above-mentioned evaporation solid-liquid separation method. Since the salt mixture is obtained at least under conditions where it has not experienced high temperatures such as "higher than 60 ° C.", for example in a limited pressure range such as "1 kPa or more and 20 kPa or less". As a result, the excellent effect as described above is obtained.

On the other hand, the gas is sucked into the container 100 through the gas pipe 131, introduced into the cooler 200, liquefied, and stored in the recovery container 400 as a recovery liquid.
When the mineral water C, which is the recovery liquid, is accumulated in the recovery container 400, the suction by the decompressor 300 is stopped, and the mineral water C is obtained from the liquid outlet 404.

The present invention is also a mineral water characterized by being obtained by evaporating solid-liquid separation of seawater using the above-mentioned evaporation solid-liquid separation method. Since the mineral water is obtained at least under conditions where it has not experienced a high temperature such as "higher than 60 ° C.", for example, a pressure range of "1 kPa or more and 20 kPa or less" is limited. , A novel composition of components, a structure of water (clusters, etc.), and as a result, the above-mentioned excellent effects are exhibited.

Hereinafter, the present invention will be described in more detail with reference to Examples and Comparative Examples, but the present invention is not limited to these Examples as long as the gist thereof is not exceeded.

<Manufacturing and evaluation of mineral water>
Example 1
30.0 kg of seawater collected off the coast of Kozushima was removed by filter filtration and placed in the container shown in FIGS. 1 to 3 (input capacity 500 L, container volume (internal volume) 1 m ³ ). The rotating concave body was rotated at 4 rotations / minute by a stirrer 110 (1.5 kW) having two rotating concave bodies 112a and 112b as shown in No. 3, and evaporation solid-liquid separation was performed while stirring.

It was heated by the heating unit 120 having a steam amount of 28 to 140 kg / hr, evacuated by the water ejector 301 shown in FIGS. 4 and 5, and the temperature of seawater was maintained at 35 ° C. ± 2 ° C. by the heat of vaporization of water.
At that time, the water temperature of the water ejector 301 and the water temperature of the cooling water of the cooler 200 were both maintained at 10 ° C. ± 2 ° C.
The water ejector 301 used is a horizontal injection type water ejector (3.7 kW) as shown in FIG. 4, and when the puller is open, the water has a gas discharge capacity of ^{20 m 3 / hour or more at normal pressure.} It was the ejector 301.

The pressure in the container 100 is maintained at least 3.3 kPa (-98.0 kPa with respect to 1 atm) or more and 6.3 kPa (-95.0 kPa with respect to 1 atm) or less during at least the main evaporation solid-liquid separation. It was.
The time required for the main evaporation solid-liquid separation was 5 hours.

Finally, 1.0 kg of salt mixture was obtained from the powder outlet 140 of the container 100.
Further, 29.0 kg of mineral water stored in the collection container was obtained from the liquid outlet 404 and evaluated as described below.

Example 2
In Example 1, the salt mixture and mineral water were used in the same manner as in Example 1 except that 30.0 kg of seawater collected off the coast of Shodoshima was used instead of 30.0 kg of seawater collected in the Seto Inland Sea. Was obtained and evaluated as described below.

Example 3
In Example 1, the salt mixture and mineral water were used in the same manner as in Example 1 except that 30.0 kg of seawater collected off Shodoshima was used instead of 30.0 kg of seawater collected off Okinawa. Was obtained and evaluated as described below.

Comparative Examples 1 to 13
Commercially available mineral waters listed in Table 1 were obtained and used for evaluation as described below.

Comparative Example 21
Seawater was distilled by heating it to 100 ° C. at normal pressure according to a conventional method, and then cooled to obtain distilled water, which was evaluated as described below.

Reference example 1
Table 1 shows the contents of only sodium (Na), magnesium (Mg), potassium (K) and calcium (Ca) in the average seawater.

Reference example 2
Table 1 shows the contents of only the above four elements (four kinds of metal ions) of the commercially available "water obtained by desalting deep sea water with an ion exchange resin".

Evaluation example 1
The contents of sodium (Na), magnesium (Mg), potassium (K) and calcium (Ca) contained in "water such as mineral water" obtained in the above Examples, the above Comparative Examples and the above Reference Examples are shown in the table. Describe in 1. The contents of sodium (Na) and potassium (K) were measured by atomic absorption spectrophotometric method, and the contents of calcium (Ca) and magnesium (Mg) were measured by ICP emission spectrometry.

Since the results in Table 1 show the above-mentioned effects of the present invention sufficiently because they contain only a limited number of four types of metal ions, Examples 1 to 3 and Comparative Examples 1 to 13 are compared. As for the content of sodium (Na), Examples 1 to 3 had a large content, but Comparative Examples 1 to 13 all had a smaller content.
The magnesium (Mg) content was high in Examples 1 to 3, but was lower in all of Comparative Examples 1 to 13 except for Comparative Example 9.
In addition, the content of potassium (K) was high in Examples 1 to 3, but was lower in all of Comparative Examples 1 to 13 except for Comparative Examples 7 and 11.
In addition, the content of calcium (Ca) was small in Examples 1 to 3, but was higher than those in Comparative Examples 1 to 13 except for Comparative Example 6.

Further, in Comparative Example 21, the contents of sodium (Na), magnesium (Mg), potassium (K) and calcium (Ca) were all below the detection limit.

In addition, other trace components (compositions) that have not been measured may affect the above-mentioned effects of the present invention.

<< Evaluation of mineral water >>
Evaluation example 2
The flavor of each of the three types of mineral water obtained in Examples 1 to 3 was examined by slowly drinking 100 mL of each in several divided doses.
In addition, the waters obtained in Comparative Examples 1 to 5 and Comparative Example 21 were also drunk in the same manner as described above, and their flavors were examined and compared.
As a result, the mineral waters obtained in Examples 1 to 3 all had a distinctly different flavor (taste and aroma) from the waters obtained in Comparative Examples.

Evaluation example 3
To 1 L of each of the three types of mineral water obtained in Examples 1 to 3, 50 g of ethanol and 10 g of glycerin were added, and the mixture was applied to the back of the hand 5 times a day for 10 days for evaluation.
Further, the waters obtained in Comparative Examples 1 to 5 and Comparative Example 21, commercially available purified water for medical use, and tap water were also evaluated in the same manner as described above and compared.
As a result, it was found that all the mineral waters obtained in Examples 1 to 3 are excellent as raw materials for cosmetic water because they are similar to living organisms unlike the waters obtained in Comparative Examples.

Evaluation example 4
In a field of about 2 m ² , using the same soil and the same fertilizer, the three types of mineral water obtained in Examples 1 to 3 were constantly sprinkled, and long onions and spinach were grown and harvested. The harvested green onions and spinach were boiled under the same conditions and tasted and evaluated.
In addition, the water obtained in Comparative Example 21, long onions and spinach grown by sprinkling ordinary agricultural water were also evaluated and compared in the same manner as described above.
As a result, the mineral waters obtained in Examples 1 to 3 were different from those obtained in Comparative Example 21 and ordinary agricultural water, and the flavors (particularly odors) of green onions and spinach were different. It was delicious.

The green onions and spinach grown by constantly sprinkling the three types of mineral water obtained in Examples 1 to 3 have a higher growth rate than those of Comparative Example 21 and the long onions and spinach grown by sprinkling ordinary agricultural water. However, it was 10% to 100% (twice) faster.
In the case of hydroponics, the volume of roots in the examples was about twice that in the comparative examples.

<Manufacturing and evaluation of salt mixture>
Comparative Examples 31, 32, 33
Commercially available salts listed in Table 2 were obtained and used for evaluation as described below.

Evaluation example 5
At the Salt Industry Center of Japan and the Seawater Research Institute, which are analytical institutions, the salt mixture of Example 1 and the metals of Comparative Examples 31 to 33 and sodium chloride were prepared by the method described in the 4th edition of the salt test method. Quantitative analysis was performed.
The measurement method is shown in the bottom row of Table 2. The measurement results are shown in Table 2.

The salt mixture of Example 1 obtained by using the evaporative solid-liquid separation method contained a smaller amount of sodium chloride (NaCl) and sodium (Na) than the commercially available salts of Comparative Examples 31 to 33. ..
On the other hand, the amounts of magnesium (Mg), potassium (K), and calcium (Ca) were all higher in the salt mixture of Example 1 except for potassium (K) of Comparative Example 33.

Evaluation example 6
Using 30 g each of the salt mixture obtained in Examples 1 to 3 and the commercially available salt of Comparative Example 31, dissolved as much as possible in the same amount of water at 25 ° C., a colorless and transparent thick substance having the same solid content concentration. An aqueous solution was prepared. The concentrated aqueous solution was close to a saturated aqueous solution.
When left at 25 ° C. for 10 days, no change was observed in the concentrated aqueous solution of the salt mixture obtained in Examples 1 to 3, but in the concentrated aqueous solution of commercially available salt of Comparative Example 31, crystals were formed on the container wall. It was deposited all over.
Since the salt mixture obtained in Examples 1 to 3 was a mixture of many salts, the crystallization (precipitation) of sodium chloride (NaCl) was inhibited.

Evaluation example 7
Pickled eggplants were made using the salt mixtures obtained in Examples 1 to 3 and Comparative Example 31, respectively.
When both were eaten and compared, the salt mixture obtained in Examples 1 to 3 had a better flavor than the commercially available salt (Comparative Example 31).

Since it is considered that the salt mixture and mineral water obtained by the evaporative solid-liquid separation method of the present invention are different from the conventional salt mixture and mineral water in terms of composition, water cluster structure, etc., they are used. It is useful as cosmetics, health foods, general foods, agricultural water, water for cultivating fish, etc.
Therefore, the present invention is widely used in the fields of health foods, general foods, cosmetics, agrochemicals, agriculture, fisheries and the like.

1 Drive water inlet piece 2 Inlet side flange 3 Suction pipe 4 Suction hole 5 Partition plate 6 Main pipe throat 7 Outer piece 8 Outer pipe 9 Output side flange 10 Flange 11 Intake pipe 12 Silent 12a Horizontal part 12b Vertical part 12c Termination end 14 Return pipe 15 Discharge pipe 16 Circulation pump 17 Water tank Water level 18 Overflow ventilation port 100 Container 101 Lower semi-cylindrical part 102 Upper square part 103 Seawater inlet 104 Lid 105a End wall 105b End wall 106a End plate 106b End plate 107 Inclined surface 108 Vacuum Total 109a Thermometer 109b Thermometer 110 Stirrer 111 Fixed convex part 112a Rotating concave part 112b Rotating concave part 113a Rotating concave part 113b Rotating concave part 114a Rotating concave groove 114b Rotating concave groove 115a Unit 121 Steam chamber 122 Steam supply device 130 Gas outlet 131 Gas piping 140 Powder outlet 200 Cooler 300 Decompressor 301 Water ejector 302 Water circulation pump 303 Water tank 400 Recovery container 404 Liquid outlet A Seawater B Salt mixture C Mineral water R Direction of rotation

Claims (9)

Natural seawater is separated by evaporation solid-liquid so that sodium (Na), magnesium (Mg), potassium (K) and calcium (Ca) contained in the natural seawater remain in the obtained mineral water. cosmetic, a health food, for general food, for agricultural products, or a vaporized liquid separation method for obtaining mineral water for aquaculture,
Using an evaporative solid-liquid separator equipped with a stirrer, a container with a heating unit and a powder outlet, a decompressor, and a cooler.
A method for evaporating solid-liquid separation, which comprises performing at least all of the following operations (1) to ( 3) to evaporate solid-liquid separation of natural seawater.
(1) A heating operation in which the inside of the container is heated by a heating unit so that the temperature of the natural seawater is maintained in a temperature range of 25 ° C. or higher and 40 ° C. or lower.
(2) A water ejector having a normal pressure volume of 20 m ³ / hour or more is used as a decompressor to reduce the pressure in the container in terms of the gas discharge capacity when a container having an internal volume of 1 m ^{3 is used.} A cooling operation in which the pressure is maintained at 1 kPa or more and 20 kPa or less, the seawater is cooled by the heat of vaporization of the water contained in the seawater, and the temperature of the seawater is maintained in the temperature range of 25 ° C. or more and 40 ° C. or less.
(3) the effluent gaseous from the container, the liquefied operation to obtain the mineral water and liquefied using a cooler The evaporation solid-liquid separation method according to claim 1, wherein in the operation (1), the temperature of the natural seawater is maintained in a temperature range of 25 ° C. or higher and 37 ° C. or lower. The evaporation solid-liquid separation method according to claim 1 or 2, wherein the natural seawater having a volume of 20 L or more can be charged. The evaporation solid-liquid separation method according to any one of claims 1 to 3, wherein the amount of natural seawater to be treated at one time is 5 kg or more and 300 kg or less. When the volume of the container is V [L] and the mass of the natural seawater charged into the container is M [kg], V [L] is twice or more and five times or less as M [kg]. The evaporative solid-liquid separation method according to any one of claims 1 to 4, which is set. The evaporation solid-liquid separation method according to any one of claims 1 to 5, wherein in the operation (2), the pressure in the container is maintained at 2 kPa or more and 10 kPa or less. The evaporation solid-liquid separation method according to any one of claims 1 to 6, wherein the water ejector is a horizontal injection type water ejector having a water circulation pump. Cosmetics, health foods, general foods, characterized by evaporating solid-liquid separation of natural seawater using the evaporative solid-liquid separation method according to any one of claims 1 to 7. A method for producing mineral water for food, agricultural products, or cultivation. The evaporative solid-liquid separation device for the evaporative solid-liquid separation method according to any one of claims 1 to 7.
An evaporative solid-liquid separator comprising, at least, a container having a stirrer, a heating unit and a powder outlet; a decompressor that is a water ejector; and; a cooler.

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