WO2018163563A1 - Evaporation solid-liquid separation method - Google Patents

Abstract

The present invention addresses the problem of providing mineral water and a salt mixture that can be used for applications where a trace constituent composition is important, and a production method therefor. The problem is solved by an evaporation solid-liquid separation method for carrying out evaporation solid-liquid separation of sea water into a salt mixture and mineral water, characterized in that, at least during a main evaporation solid-liquid separation step, the temperature of the sea water is maintained at a temperature between 25°C and 60°C and the pressure in a vessel is maintained within 1-20 kPa using a pressure reducer, and by a salt mixture and mineral water produced by the production method.

Description

Evaporative solid-liquid separation method

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 into mineral water and a salt mixture having a useful and novel composition. 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 for removing sodium chloride from seawater to obtain fresh water are known.
For example, Patent Documents 1 to 3 describe a desalination treatment method, a method for producing a salt concentrate, a fresh water combined water purifier using a reverse osmosis membrane, and the like.
Patent Document 4 describes a seawater treatment method using a mosaic charged membrane, and Patent Documents 5 and 6 describe a method for producing a mineral component-containing composition (such as mineral water) using an ion exchange membrane. Are listed.

Further, for example, Patent Document 7 describes an apparatus and a method related to flash evaporation.
For example, Patent Document 8 describes an evaporator for a multi-effect fresh water generator, and Patent Documents 9 and 10 describe osmosis as materials that heat and evaporate water in seawater and liquefy the water vapor obtained. An evaporator and a fresh water generator that use a membrane together are described.

However, the purpose of these techniques is simply to obtain fresh water from seawater, and the obtained fresh water should mainly be reduced so that the sodium chloride concentration can be used for beverages, etc. It did not consider the composition of salts obtained as a residue, the presence or absence of trace elements, and the like.
In other words, these conventional technologies merely secure ordinary drinks or simply secure agricultural water instead of river water. The obtained “liquid called fresh water (soft water)” It was not used in fields where trace amounts of components (content ratio) such as food (raw materials) and health food (raw materials) are important.

That is, there is almost no solid-liquid separation method for seawater that can be used with superiority in applications where a small amount of component composition is important.

JP 2007-267747 A JP2015-029935A JP 2016-203056 A JP 2006-007084 A JP 2002-238515 A JP2015-019638A JP 2000-107502 A JP 2007-198701 A JP2015-150553A JP 2016-097328 A

This invention is made | formed in view of the said background art, The subject is the mineral water and salt mixture which can be used also for the use where a slight component ratio is important, and the use where the presence or absence of a trace amount component (element) is important. It is to provide.

As a result of intensive studies to solve the above-mentioned problems, the present inventor has found that the “specific pressure range necessary for suitably evaporating solid-liquid separation while maintaining the temperature of the object at 25 ° C. or more and 60 ° C. or less. And (more preferably gas discharge capacity) ", and an apparatus capable of achieving such a condition (even in industrial quantities) could be realized for the first time.
And at least during the main evaporative solid-liquid separation, as a result of applying the evaporation conditions to seawater, surprisingly, a mineral with a novel composition in which trace amounts of components (elements) can remain (maintain) as natural products It has been found that water (and a salt mixture) can be obtained, leading to the present invention.

That is, the present invention is an evaporative solid-liquid separation method in which seawater is separated into evaporated solid and liquid, and separated into a salt mixture and mineral water,
At least during the main evaporative solid-liquid separation, the temperature of the seawater is maintained at 25 ° C. or higher and 60 ° C. or lower, and the pressure in the container is maintained at 1 kPa or higher and 20 kPa or lower using a decompressor. A separation method is provided.

The present invention also provides the above-described method for evaporating solid-liquid separation, in which seawater is subjected to evaporative solid-liquid separation by performing at least all of the following operations (1) to (4).
(1) A heating operation for heating the inside of the container with a heating unit so that the temperature of the seawater is maintained within a temperature range of 25 ° C. or more and 60 ° C. or less during at least main evaporation solid-liquid separation;
(2) During at least main evaporative solid-liquid separation, the water ejector is decompressed using a decompressor to maintain the inside of the container at 1 kPa or more and 20 kPa or less, and the seawater is removed by the evaporation heat of water contained in the seawater. A cooling operation for cooling and maintaining the temperature of the seawater in a temperature range of 25 ° C. or higher and 60 ° C. or lower;
(3) A liquefaction operation for liquefying the gas flowing out of the container using a cooler to obtain mineral water;
(4) Taking out the salt mixture remaining in the container from the powder outlet of the container to obtain a salt mixture

The present invention also provides a method for producing a salt mixture and a method for producing mineral water, characterized in that seawater is separated by evaporating solid / liquid using the above evaporative solid / liquid separation method.

Further, the present invention is an evaporative solid-liquid separation apparatus for the above evaporative solid-liquid separation method,
The present invention provides an evaporative solid-liquid separation device comprising: a container having at least a stirrer, a heating unit, and a powder outlet; a decompressor that is a water ejector; and a cooler.

The present invention also provides a salt mixture and mineral water characterized by being obtained by evaporating solid-liquid separation of seawater using the above evaporative solid-liquid separation method.

The present invention solves the above-mentioned conventional problems and problems, and provides a mineral water holding a trace component (element) 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 where a trace component composition is important.
Unlike conventional distillation that 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, In the “evaporation obtained”, metal ions in seawater exist (remain), that is, trace metal ions that would be removed by the original evaporation are also included in “evaporated”. Therefore, mineral water (evaporated matter obtained by evaporation) can be obtained that has more “nature of seawater as a raw material” with respect to “properties other than the properties of sodium chloride overwhelmingly”. As a result, as a result of applying the mineral water of the present invention to a living organism, it exerts an excellent effect on the living organism as described later.

On the other hand, a method of obtaining fresh water by evaporating water at 60 ° C. or less at a sufficiently reduced pressure (for example, about 1 Pa (10 ⁻² mmHg) with a rotary pump) is known. However, such a method cannot provide 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 more and 60 ° C. or less, the pressure is 1 kPa or more and 20 kPa or less at a relatively high pressure (without increasing the degree of decompression), and the industrially applicable amount of seawater is industrially used. Evaporating within a working time requires a special pressure reducer; and it has not been predicted that the resulting product was excellent;

Conventional seawater evaporation focuses on evaporative efficiency, cost reduction, etc., and ensures drinking water and water for agriculture (water with a sodium chloride concentration below a certain level). However, the mineral water produced by using the evaporative solid-liquid separation method of the present invention has characteristics such as adapting to a living body, and therefore can be suitably used for the above-mentioned high added value fine chemicals.

The mineral water produced by using the evaporation solid-liquid separation method of the present invention has a calcium (Ca) content generally lower than that of commercially available mineral water, but sodium (Na), magnesium (Mg), potassium (K). ) Content is certainly high. In addition, other seawater components are likely to 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 the overwhelming main component sodium chloride (NaCl) from seawater, and other seawater (trace) components are dissipated. It remains without.
On the other hand, water obtained by evaporating seawater at 100 ° C. or using a membrane to desalinate 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 dissipative material from “natural seawater”. For this reason, it is considered that trace components (elements) necessary for the living body remain as they are.

The "(trace) component" has not been clarified, but the growth rate of plants (vegetables, etc.) in the sprinkled soil, the flavor of the vegetable; the flavor of the mineral water itself of the present invention, a dish using the mineral water It is clear from the fact that the taste and the taste of pickles 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) component is not specifically clarified in the present invention, but is not yet clarified by the current (analytical) advanced technology. In the present invention, with respect to the improvement of the action on the living body as described above, which cannot be fully understood by the current (analytical) technique, we give up approaching from the identification (analysis) of the (trace) component, and the antibacterial agent is an antibiotic which is a natural product. It depends on seawater, which is a natural product.

The salt mixture produced by using the evaporative solid-liquid separation method of the present invention has much less sodium chloride (NaCl) content and sodium (Na) content than commercially available salt (practice). See example). On the other hand, the salt mixture produced using the evaporation solid-liquid separation method of the present invention has a magnesium (Mg) content, calcium (Ca) content, potassium ( The content of K) is also large (see Examples).

Since both mineral water, which is an evaporation component produced using the evaporation solid-liquid separation method of the present invention, and the remaining salt mixture have a novel composition and water structure, for example, makeup such as lotion (Raw materials); health food (raw materials); general foods (raw materials) such as pickles and drinking water, water for agricultural products; water for fish farming (raw materials); The content ratio) can be particularly preferably used for “uses that are important for (becomes important for) the performance”.

The mineral water and salt mixture produced using the evaporative solid-liquid separation method of the present invention will all have a novel composition, a cluster structure of water, etc. It has been confirmed from the fact that it has a different flavor from conventional products and has an effect on humans (such as its skin).
In addition, the difference in "taste and smell" (flavor) that can be perceived by humans and the effect on human (skin) etc. are beyond the capabilities of current instrumental analysis (below the detection limit). ) Is technical common sense, it is impossible or almost impractical to directly specify the trace component and the subtle component content ratio that show the excellent effect ("impossible / unpractical circumstances") There).

It is the schematic which shows one form of the whole apparatus used for this invention. It is a schematic sectional drawing which shows one form of the container, cooler, collection | recovery container, etc. with which the apparatus used for this invention is equipped. It is a schematic perspective view which shows one form of the stirrer which the container with which the apparatus used for this invention is equipped has. It is a schematic sectional drawing which shows one form of the horizontal injection type water ejector which is a preferable pressure reducer with which the apparatus used for this invention is equipped. It is a schematic sectional drawing which shows one form, such as a lateral injection type water ejector, a water tank, a circulation pump, etc. which are the preferable pressure reducers with which the apparatus used for this invention is equipped.

Hereinafter, the present invention will be described, but the present invention is not limited to the following specific embodiments, 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 into evaporative solid-liquid and separated into a salt mixture and mineral water, and the temperature of the seawater is set at least during main evaporative solid-liquid separation. While maintaining at 25 degreeC or more and 60 degrees C or less, the pressure in a container is maintained at 1 kPa or more and 20 kPa or less using a decompressor.

The evaporative solid-liquid separator used in the present invention is an apparatus whose use is limited to the “evaporated solid-liquid separation method of the present invention”. The evaporative solid / liquid separation apparatus used in the present invention is an evaporative solid / liquid separation apparatus having an ability that can be used in the evaporative solid / liquid separation method of the present invention, and includes at least a stirrer, a heating unit, and a powder outlet. 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.
A stirrer 110 that stirs the seawater A, a heating unit 120 that heats the seawater A and the container 100, a gas outlet 130 that extracts the gas generated from the seawater A, and a powder outlet 140 that extracts the salt mixture B after processing. Container 100;
A cooler 200 for cooling the gas taken out from the gas outlet 130;
A decompressor 300 for decompressing the inside of the container 100; and;
A recovery container 400 for recovering the mineral water C cooled and liquefied 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 for heating the inside of the container with a heating unit so that the temperature of the seawater is maintained within a temperature range of 25 ° C. or more and 60 ° C. or less during at least main evaporation solid-liquid separation;
(2) During at least main evaporative solid-liquid separation, the water ejector is decompressed using a decompressor to maintain the inside of the container at 1 kPa or more and 20 kPa or less, and the seawater is removed by the evaporation heat of water contained in the seawater. A cooling operation for cooling and maintaining the temperature of the seawater in a temperature range of 25 ° C. or higher and 60 ° C. or lower;
(3) A liquefaction operation for liquefying the gas flowing out of the container using a cooler to obtain mineral water;
(4) Taking out the salt mixture remaining in the container from the powder outlet of the container to obtain a salt mixture

The particularly preferable method of 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 specifically, for example, as follows.

First, at the start of operation, the cooling water supply device is filled with cooling water, and the cooling water is circulated through the cooler 200. Next, seawater A is introduced into the container 100 from the seawater inlet 103 and the lid 104 is closed.
When the seawater A is put into the container 100, the stirrer 110 is rotated if necessary, and the stirring operation for stirring the seawater A in the container 100 is performed. A stirring operation and (particularly) preferable conditions and structure of the stirrer 110 will be described later.
Next, during at least main evaporation solid-liquid separation, 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 within a temperature range of 25 ° C. or more and 60 ° C. or less.

In the present invention, “main evaporative solid-liquid separation” refers to the period from the initial stage of evaporative solid-liquid separation until evaporating solid-liquid separation of 70% by mass or more of seawater charged into the container. Moreover, it is preferably maintained at a specific temperature condition and a specific pressure condition described later until 80% by mass or more, more preferably 90% by mass or more, and particularly preferably 98% by mass or more is evaporated and solid-liquid separated. desirable.

Heat is applied from the outside by supplying steam for heating into the steam chamber 121 from the steam supply device. The container 100 is provided with a heating unit 120 that heats the seawater A and the inside of the container 100. In the heating unit 120, water vapor heated by the steam supply device 122 is converted into the container 100 (preferably the lower half of the container 100. It is fed into a steam chamber installed around the cylindrical part 101).

The heat applied to the container 100 is transferred to the seawater A, and the seawater A is stirred by the stirrer 110 or by boiling, whereby water in the seawater A evaporates and the (concentrated) seawater A Temperature, concentration, viscosity, etc. become uniform.
In the present invention, it is preferable that the temperature of the seawater A is maintained at 25 ° C. or more and 60 ° C. or less and distilled off at the same or slightly lower pressure (for example, 10% lower pressure) than the vapor pressure of water at the temperature. At that time, the 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 transmission, final removal, and the like.

Seawater A is heated by appropriately adjusting the temperature and amount of the steam for heating fed into the steam chamber 121.
On the other hand, by adjusting the amount of water supplied to the water ejector 301, which is the decompressor 300, the pressure, the injection speed, etc., and appropriately setting the gas discharge capacity and the pressure in the container 100, The seawater A is cooled with the heat of evaporation.
That is, at least during main evaporative solid-liquid separation, the inside of the vessel 100 is maintained at 1 kPa or more and 20 kPa or less, and the seawater A is cooled with the heat of evaporation of water contained in the seawater A, so that the temperature of the seawater A is increased. It is maintained in a temperature range of 25 ° C. or more and 60 ° C. or less.

By setting the gas discharge capacity of the decompressor 300 to “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 when the temperature is likely to rise, the temperature of the seawater A can be lowered to a predetermined temperature or less by the evaporation heat of the water in the seawater A.

The substantial volume of the container 100 is not particularly limited, but the range is important from the viewpoint of whether or not the evaporating solid-liquid separation conditions 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 20L to 5000L, preferably 35L to 4000L, and particularly preferably 50L to 3000L. The maximum input capacity (L) of the seawater A is preferably substantially equal to the volume of the lower semi-cylindrical portion 101 of the container 100 described above.

When using the substantial volume of the container 100 or the container having the shape as shown in FIGS. 2 and 3, if the volume of the lower semi-cylindrical portion 101 is too small, the amount of processing at one time becomes too small and the cost increases. So it can not be used commercially. In addition, the meaning of applying the above-mentioned or later-described special evaporative solid-liquid separation conditions (pressure in the container, gas discharge capability, etc.) and apparatus (stirrer, decompressor, etc.) in the present invention may be reduced.
On the other hand, if the pressure is too large, the decompressor 300 that can exhibit the above-described effect of the present invention does not exist or becomes extremely expensive so as to be impractical; When the decompressor 300 having the “gas discharge capacity and degree of decompression commensurate with the size of the container” does not exist or becomes extremely expensive unrealistically; when the decompression load is excessively applied to the casing of the container 100, etc. .

The mass of the seawater A to be evaporated and solid-liquid separated in one treatment depends on the volume of the container 100 to be used, and is not particularly limited, but is preferably 5 kg to 300 kg, more preferably 20 kg to 200 kg, more preferably 30 kg to 100 kg. The following are particularly preferred:
If the amount is too small or too large, the same thing as the case where “the volume of the container 100 or the lower semi-cylindrical portion 101” is too small or too large may occur.
In particular, when there is too little seawater A, there are (preferred) requirements / features such as “pressure during main evaporative solid-liquid separation”, decompressor type, gas discharge capacity, and heat of evaporation used for cooling in the present invention. It may not be alive. The present invention is particularly effective when the amount of seawater A is not less than the above lower limit.

In the evaporative solid-liquid separation method of the present invention, when the volume of the vessel is V [L] and the mass of seawater A charged into the vessel is M [kg], V [L] is M [kg]. 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 and evaporation may not be performed satisfactorily. 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 and the gas discharge capacity of the decompressor 300 cannot be fully exhibited, and as a result The seawater A cannot be cooled by the heat of evaporation, and the temperature of the seawater A exceeds the upper limit of the temperature range. Moreover, even if it is too small or too large, the same thing as the case where the above-mentioned "volume of the container 100 or the lower semi-cylindrical part 101" is too small or too large may occur.

Thus, 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 in the range of 25 ° C. to 60 ° C. Particularly preferred range).
The container 100 is provided with a vacuum gauge 108 and thermometers 109a and 109b for measuring the pressure (decompression degree) in the container 100. These are provided to measure the pressure (decompression degree) and temperature in the container 100 and indirectly measure the temperature of the seawater A, and also determine the start and end of the operation of evaporating 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 using heat conduction or the like of the container 100 (including the stirrer 110). That is, even if the seawater A is likely to be rapidly cooled by the evaporation heat of water, or conversely, even if the seawater A is likely to be rapidly heated by the heating unit 120, the temperature of the seawater A is measured sufficiently accurately. It can be so.

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

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

On the other hand, if the temperature is too high, the amount of evaporation will be the same or similar to that of fresh water (soft water) by the conventional distillation method, and the residue will have the same or similar component composition as the natural salt by the conventional manufacturing method. Thus, the effects of the present invention may not be exhibited.

In this invention, the salt mixture B and the mineral water C can be manufactured by the processing time (operation time) which is accept | permitted even if it is a commercial quantity by prescribing the temperature lower limit of the seawater A.
On the other hand, by defining the upper temperature limit of the seawater A, unlike the conventional “distilled water of seawater” and the conventional “natural salt by evaporation and drying of seawater”, a new component composition can be obtained.
If the temperature is too high, the obtained salt mixture B or mineral water C may be similar to or similar to the conventional one. As a result, specifically, for example, the obtained salt mixture The flavor of the “food such as pickles” used was not improved, the flavor of fish cultured with water obtained by dissolving the obtained salt mixture was not improved, or the mineral water obtained was sprinkled (supplied) The flavor may not be improved.

The container 100 is provided with a gas outlet 130 for extracting gas generated from the seawater A. It is preferable that the vicinity of the gas outlet 130 is also maintained in the temperature range with sufficient heat conduction or the like so that water droplets are not generated (no condensation) in the vicinity of the gas outlet 130.

A liquefaction operation is performed to liquefy the gas flowing out of the container 100 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. The container 100 is preferably liquefied and the pressure inside the container 100 is reduced.
The cooling medium of the cooler 200 is water having a temperature of “10 ° C. or higher and 5 ° C. or lower (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 as the cooling medium is too high, part of the gas may not be liquefied. Such a cooler 200 may be a known one.

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

In the apparatus used in the present invention, for example, as shown in FIG. 1, a decompressor 300 for decompressing the inside of the container 100 is provided behind the cooler 200.
As shown in FIG. 1, the decompressor 300 is preferably a water ejector 301, and the water ejector 301 is particularly preferably a lateral injection type water ejector 301 having a water circulation pump.
In the case of the water ejector 301, particularly the lateral injection type water ejector 301 having a water circulation pump, the degree of pressure reduction (pressure in the container) is optimal considering the vapor pressure of water and the boiling point of water under reduced pressure. Regarding the gas discharge capacity, the water ejector 301, particularly the lateral injection type water ejector 301 having a water circulation pump, is optimal because the capacity is extremely large.

By sucking with the decompressor 300, the gas in the container 100, that is, the water vapor and air containing minerals in the seawater A are sucked through the gas pipe 131, and the water contained in the seawater A in the container 100 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 to be sucked by the decompressor 300. When the water ejector 301 is used as the decompressor 300, the injection nozzle diameter, 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 to be described later. The inside of the container 100 is maintained at a predetermined pressure (range).

The decompressor 300 is converted when a container having an internal volume of 1 m ³ is used so that the temperature of the seawater A does not exceed 60 ° C. (preferably not exceeding 45 ° C.) due to the heat of evaporation of water. Thus, 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 a decompressor 300 having a large gas discharge capacity. When the decompressor 300 having only a small gas discharge capacity compared to the internal volume of the container 100 is used (unless the gas discharge capacity is increased according to the internal volume of the container 100), the seawater A is generated by the heat of evaporation of water. It may become difficult to cool the seawater A, and the temperature of the seawater A may increase.

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 of normal 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 at least 2 m ³ / hour of atmospheric pressure is preferable. When a container having an internal volume of 0.5 m ³ is used, a gas having an atmospheric pressure 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.

"In terms of when the internal volume was used containers 1 m ^3, normal pressure body volume 20 m ³ / time or more gas discharge capability" is preferred, that value is always pressure body volume 22m ³ / time than 300 meters ³ / time more preferably not more than atmospheric pressure body volume 25 m ³ / time than 200 meters ³ / time or less are more preferred, atmospheric pressure body volume 27m ³ / time than 150 meters ³ / time or less is particularly preferred.
When the gas discharge capacity of the decompressor 300 is too small, when the processing time is long, it is difficult to obtain the effect of preventing the excessive increase in temperature of the seawater A due to the heat of evaporation of water, and the temperature of the seawater A is too high. is there.
If the gas discharge capacity of the decompressor 300 is too large, there may be no decompressor 300 having such a large gas discharge capacity while achieving the following degree of decompression, or it may be very expensive or extremely large. is there.

As shown in FIG. 1, water (preferably water previously cooled by a water chilling unit) is stored in a water tank 303, water pressurized by a water circulation pump 302 is fed, and the pressurized water is ejected by a water ejector 301. The pressure is reduced by blowing out the water. A flowing liquid uses a property (Bernoulli's theorem) that has a lower pressure than a stationary liquid to exhaust a gas such as water vapor.

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

Specifically, the pressure in the container (decompression degree) by the decompressor 300 is 1 kPa (−100.3 kPa with respect to 1 atm (101.3 kPa)) or more and 20 kPa (1) during at least main evaporation solid-liquid separation. It is essential to perform evaporation / solid separation while maintaining the pressure (−81.3 kPa) or less with respect to the atmospheric pressure (101.3 kPa).
The pressure in the container 100 is maintained at 1.5 kPa (−99.8 kPa with respect to 1 atm (101.3 kPa)) or more and 15 kPa (−86.3 kPa with respect to 1 atm (101.3 kPa)). It is preferable to do.
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),
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),
It is particularly preferably 3.3 kPa (−98 kPa with respect to 1 atm) or more and 8.3 kPa (−93 kPa with respect to 1 atm).

If the pressure in the vessel (the degree of decompression) is too low (if the pressure is too high), the cooling of the seawater A due to the evaporation heat of water cannot be expected, and if the temperature of the seawater A becomes too high, it takes time to separate the evaporated solid and liquid. As a result, the resulting salt mixture or mineral water may be similar to or approximate to the conventional one. Specifically, for example, the same thing as the case where the above-described temperature is too high may occur.

On the other hand, when the pressure in the container (the degree of pressure reduction) 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 preferred temperature range of seawater” described below, There is a case where it is not necessary to make the pressure so low, and after satisfying the above-mentioned lower limit of one seawater treatment amount that is industrially and commercially applicable, it has the above-mentioned gas discharge capability in the first place, and There are cases where the decompressor 300 that can increase the degree of decompression does not exist, or it is unrealistically very large and expensive.

The temperature dependence of the water vapor pressure is shown below.
Water temperature (℃) 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

It is preferable that the decompressor 300 is a lateral injection type water ejector 301 having a water circulation pump 302 because it has a high gas discharge capacity as well as a high degree of decompression. That is, it is preferable from the viewpoint that both the degree of decompression and the gas discharge capacity can be achieved and the effects of the present invention can be easily achieved. It is particularly easy to increase the gas discharge capacity when the water circulation pump 302 is provided and the horizontal injection type is used.

In general, the decompressor includes a rotary pump, an oil diffusion pump, a mercury diffusion pump, a differential pump, and the like. For example, although the rotary pump can achieve about 1 Pa (10 ⁻² mmHg) and the oil diffusion pump about 0.1 mPa (10 ⁻⁶ mmHg), a high vacuum can be achieved, but the gas discharge capacity is extremely low. On the other hand, in a commercially available or general ejector, there are cases where the pressure is usually higher than 20 kPa (the degree of decompression cannot be increased).

The coexistence of the gas discharge capability and the degree of pressure reduction can be achieved only by the “water ejector 301”. Particularly, by using the lateral injection type water ejector 301 having the water circulation pump 302, both can be suitably achieved.
The numerical value of the high gas discharge capacity described above is not a general-purpose numerical value although it can be achieved by the water ejector 301. The numerical value of the high gas discharge capacity described above is obtained by adjusting the temperature of the water to be injected, the injection nozzle diameter, the injection speed, the injection amount per unit time, the injection distance, and the like.

A particularly preferable aspect of the “lateral injection type water ejector” in the present invention is shown in FIGS.
The “lateral injection type water ejector” shown in FIGS. 4 and 5 is provided with a cylindrical driving water inlet piece 1 for receiving driving water and a downstream side of the driving water inlet piece 1. 1 has a main pipe throat 6 for mixing driving water and suction gas flowing in from 1 and an output piece 7 formed by connecting to the downstream end of the main pipe throat 6 and having a pipe whose inner diameter is widened toward the end. Yes.
Further, if necessary, it has a cylindrical shape and is provided at the downstream end portion of the output piece 7, and is attached to the silencer 12 for flowing a mixed gas of driving water and suction gas, and attached to the silencer 12. An air intake pipe 11 is provided to take in air into the silencer 12 when it flows out and to prevent a sudden change in atmospheric pressure in the silencer 12.

Further, the water ejector 301 described above includes a jacket pipe 8 that accommodates the driving water inlet piece 1, the main pipe throat 6, and the output piece 7, and a suction pipe 3 that supplies suction gas to the jacket pipe 8. The outer pipe 8 is connected to the silencer 12, and the main pipe throat 6 is formed by a cylindrical pipe having a plurality of gas suction holes 4 provided to be connected to the terminal end of the driving water inlet piece 1.

A circulation pump 16 that sucks water from the water tank 303 and discharges the water 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. The path is preferably 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 thereto, 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 drive water inlet piece 1 is chamfered to reduce water flow resistance.

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 tube wall are opened at the inlet of the main pipe throat 6, and the suction holes 4 receive suction gas when evacuated (reduced pressure) through the suction pipe 3. This is for sucking into the main pipe throat 6.

In the vicinity of the end of the main pipe throat 6, a pipe-shaped exit piece 7 having a diameter larger than that of the main pipe throat 6 is connected. The outlet piece 7 has an internal shape that widens toward the outlet.
Moreover, the jacket pipe 8 which coat | covers the drive water inlet piece 1, the main pipe throat 6, and the outlet piece 7 is connected cylindrically outside. A water ejector 301 is constituted by these members 1 to 8.
Reference numeral 12 denotes a silencer. As shown in FIG. 4, the silencer 12 has a pipe shape whose inner diameter is thicker 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.
A hollow circular partition plate 5 is provided so that the evacuation function is performed only through the suction tube 3. The inner part of the partition plate 5 is fixed to the outer part of the main pipe throat 6, and the outer peripheral part of the partition plate 5 is fixed to the jacket tube 8 so that sufficient airtightness is maintained.

As shown in FIG. 5, the decompressor 300 according to the present invention includes a water tank 303 in which water is stored so that the silencer 12 can be immersed in order to achieve a very high gas discharge capacity of the water ejector, and is used in the water ejector 301. The driving water is once stored in the water tank 303.
The water ejector 301 is fixed from the outside of the water tank 303 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 with the flange 10. Thereby, 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 suction gas flows out into the water in the water tank 303 from the end 12c. It has become.
Further, the drive water is circulated and reused through a return pipe 14 connected to a circulation pump 16 that creates a water flow.
A 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 connection part of the water ejector 301 in the silencer 12, and the intake port of the intake pipe 11 is positioned above the water tank water level 17 so that the intake port is below the water surface. A structure that does not soak. The water tank 303 is provided with an overflow vent 18 for setting the water level 17.

A preferred water ejector 301 in the present invention is provided with a suction hole 4 in the main pipe throat 6 as shown in FIG. Thereby, it has a higher (larger) gas discharge capacity than a conventional ejector that sucks gas from the gap between the tubes.

Further, 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 as shown in FIG. The “lateral 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 from 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. Although depending on the amount of seawater A, 3 to 50 L / hr is preferable, 10 to 40 L / hr is more preferable, and 20 to 30 L / hr is particularly preferable. “L” is the volume of mineral water C to be obtained.

The evaporative solid-liquid separation method of the present invention takes into consideration the vapor pressure of water at the “optimum temperature for evaporative solid-liquid separation of seawater”, and lowers the pressure (decompression degree) in the container 100 more than necessary with respect to the vapor pressure. Regardless of this, it was possible to achieve this on an industrial (commercial) scale for the first time by cooling the seawater A with evaporative heat while turning that amount toward improving the gas discharge capacity.

“Seawater” and “liquid in which the water in the seawater evaporates to a high viscosity” is preferably boiled at least during the main evaporation solid-liquid separation, so stirring is not essential. Is preferably performed.
The stirrer may be of a horizontal blade type or a screw type, but is preferably agitated by the rotating concave portions 113a and 113b and the fixed convex portion 111 using the stirrer 110 as shown in FIG. Is particularly preferred.

During the evaporation operation, the stirrer 110 is rotated in the rotation direction indicated by the arrow R in FIGS. 2 and 3, and the seawater A in the container 100 is agitated between the rotating concave portions 113 a and 113 b and the fixed convex portion 111. Seawater A is agitated.
The stirring is performed by “a plurality of rotating recesses 112a and 112b having a plurality of rotating recesses 113a and 113b” and “a plurality of fixed protrusions 111 provided on the inner surface of the container 100 (preferably the lower inner surface of the lower semi-cylindrical portion 101). In order to obtain the above-mentioned effect.

For example, FIG. 3 is a perspective view showing the configuration of the stirrer 110, and the stirrer 110 is rotated by a motor provided outside the container 100, and rotates on the end walls 105 a and 105 b of the container 100. The center axis is constituted by left and right end plates 106a and 106b that are supported, and rotating recesses 112a and 112b that are substantially in the shape of a "<" shape 115 that are fixed at both ends between the ends. (A structure that can be rotated without a central axis). The apparatus shown in FIG. 3 has two rotating concave bodies (112a and 112b), but the number of rotating concave bodies 112 may be one.

By making the rotary recesses 112a and 112b substantially “<”-shaped, the seawater A can be easily stirred, and the salt mixture B can be scraped off from the inner wall of the container 100 after the evaporative solid-liquid separation operation is completed. The salt mixture B can be suitably obtained from the powder outlet 140 with good yield by scraping it toward the powder outlet 140 (located substantially at the lower center of the container 100).

In the evaporative solid-liquid separation method of the present invention, the agitator 110 has two or more rotating recesses, and the seawater A is stirred by rotating the rotating recesses in the same direction. It is preferable to scrape the salt mixture B from the inner wall of the container 100 and scrape it toward the powder outlet.

The rotation speed of the agitator 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 to 8 rotations / minute. It is preferably 2 revolutions / minute or more and 6 revolutions / minute or less, more preferably 4 revolutions / minute or more and 5 revolutions / minute or less.
When the rotational speed is too low, the efficiency of stirring may be deteriorated, temperature unevenness may occur in the seawater A, and when the rotational speed is too high, an excessive load may be applied to the stirrer 110. is there.

The evaporative solid-liquid separation method of the present invention is not limited, but the lower portion of the container 100 is cylindrical, has a plurality of fixed projections 111 on its inner wall, and the stirrer 110 is one. The rotating recesses 112a and 112b having a plurality of rotating recesses 113a and 113b are provided. By rotating the rotating recesses 112a and 112b, the seawater A in the container 100 is converted into the fixed protrusion 111 and the rotating recess 113a. , 113b.

Reference numeral 111 in FIG. 3 denotes a plurality of fixed convex portions fixed to the inner surface of the lower semi-cylindrical portion 101. The portions corresponding to the fixed convex portions 111 in the rotary concave portions 112a and 112b are arranged in the rotary concave portions 112a and 112b. Rotating recess grooves 114a and 114b for passing through the fixed protrusion 111 are formed, and rotating recesses 113a and 113b for stirring the seawater A between the fixed protrusions 111 are provided on both sides of the groove. ing.
In FIG. 3, the fixed convex portion 111 and the rotational concave portions 113a and 113b are disposed at different positions in the circumferential direction so that the meshing is sequentially performed at different times. The momentary increase in power is prevented from occurring.

The logarithm of the rotating recesses provided in one rotating recess body depends on the size of the container 100, the stirrer 110, the rotating recess bodies 112a and 112b, and the type of seawater A to be subjected to evaporation solid-liquid separation. It is preferable that one rotary recess body is provided with 5 to 20 pairs, and particularly preferably 8 to 14 pairs.
If there are too few rotating recesses provided in one rotating recess body, the efficiency of stirring may deteriorate, evaporation may be suppressed and the temperature may rise, and if too much, excessive stirring will 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 evaporation heat of water.

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

At the end of the operation, an extraction operation for taking out the salt mixture B in the container 100 from the powder outlet of the container 100 is performed. The stirrer 110 according to the present invention can suitably stir the seawater A by the special structure of the two or more rotating recesses of the stirrer 110 and scrape the obtained salt mixture B from the container 100. It is preferable that the powder can be suitably scraped toward the powder outlet 140.

The time required for main evaporative solid-liquid separation (from the beginning of the evaporative solid-liquid separation operation until 90% by mass of water in the seawater charged in the container is separated by evaporative solid-liquid) depends on (proportional to) the input amount. However, it is preferably 1 hour or longer and 20 hours or shorter, more preferably 2 hours or longer and 13 hours or shorter, and particularly preferably 3 hours or longer and 8 hours or shorter.

When the time is too short, there is a case where the temperature is excessively increased because the water cannot be cooled by the evaporation heat. In the first place, 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 less (preferably the temperature or less) on a full-scale production scale, or it may become extremely large so that it is not realistic. .
On the other hand, if the time is too long, time may be wasted and cost may increase. In addition, the meaning of applying the above-mentioned or later special evaporative solid-liquid separation conditions (pressure and temperature in the container, gas discharge capacity, etc.) and apparatus (stirrer, decompressor, etc.) in the present invention may be reduced. In other words, there are cases where the (preferred) requirements / features of utilizing the heat of evaporation (endotherm) due to “pressure during main evaporative solid-liquid separation”, decompressor type, gas discharge capacity, etc. in the present invention are not utilized. is there.

The above-described evaporation solid-liquid separation method of the present invention may be a batch type (batch type) or a continuous type. In the case of a batch type (batch type), the operation can be performed reliably, and in the case of a continuous type, the operation can be performed smoothly.
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 be full, 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 maintaining 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 at the substantially lower center of the container 100 (near the lower center of the lower semi-cylindrical portion 101).
By making the stirrer 110 structured as described above, that is, as shown in FIG. 3, the rotating recesses 112a and 112b are formed in the shape of “U” 115a and 115b, thereby evaporating solid-liquid separation. The salt mixture B after completion can be easily collected in the lower center of the container 100, and the salt mixture B can be easily taken out. For this purpose, 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 can be obtained by scraping the salt mixture B well from the inner wall of the container 100 and scraping it well toward the powder outlet 140 provided near the lower center of the container 100. A good (smooth) salt mixture B can be obtained.

After the vapor of the recovered liquid has almost come out from the gas outlet 130 of the container 100, that is, after the above-mentioned “main evaporative solid-liquid separation” is finished, the temperature in the container 100 is set higher than the above upper limit temperature. Thus, it is also preferable that the water is completely evaporated to achieve good powdering.

The present invention is also a salt mixture obtained by evaporating solid-liquid separation of seawater using the above-mentioned evaporative solid-liquid separation method. The salt mixture is obtained at least under conditions that do not experience a high temperature such as “above 60 ° C.”, for example, a pressure range such as “1 kPa to 20 kPa” is limited. As a result, it has an excellent effect as described above.

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 recovered liquid, is stored in the recovery container 400, the suction by the decompressor 300 is stopped and the mineral water C is acquired from the liquid outlet 404.

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

Hereinafter, the present invention will be described more specifically with reference to examples and comparative examples. However, the present invention is not limited to these examples as long as the gist thereof is not exceeded.

<Manufacture and evaluation of mineral water>
Example 1
Remove 30.0 kg of seawater collected off the coast of Shodoshima, remove dust dispersed by filtration, and put it into the container shown in Figs. 1 to 3 (input capacity 500L, container volume (internal volume) 1m ³ ). The rotating concave body was rotated at 4 rotations / minute by the stirrer 110 (1.5 kW) having the two rotating concave bodies 112a and 112b as shown in FIG.

While heating by the heating unit 120 having a steam amount of 28 to 140 kg / hr, the water was ejected by the water ejector 301 shown in FIGS. 4 and 5, and the temperature of the seawater was maintained at 35 ° C. ± 2 ° C. by the evaporation heat 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 kept at 10 ° C. ± 2 ° C.
The used water ejector 301 is a lateral injection type water ejector (3.7 kW) as shown in FIG. 4, and water that has a gas discharge capacity of a normal pressure volume of 20 m ³ / hour or more when pulled is open. It was the ejector 301.

The pressure in the vessel 100 is kept at least 3.3 kPa (−98.0 kPa with respect to 1 atm) to 6.3 kPa (−95.0 kPa with respect to 1 atm) at least during main evaporative solid-liquid separation. It was.
The time required for main evaporative solid-liquid separation was 5 hours.

Finally, 1.0 kg of a 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, instead of using 30.0 kg of seawater collected off Shodoshima, salt mixture and mineral water were used in the same manner as in Example 1 except that 30.0 kg of seawater collected in the Seto Inland Sea was used. And evaluated as described below.

Example 3
In Example 1, instead of using 30.0 kg of seawater collected off the coast of Shodoshima, 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 Okinawa was used. And evaluated as described below.

Comparative Examples 1-13
The mineral water which is the commercial item described in Table 1 was obtained, and evaluated as described later using them.

Comparative Example 21
Seawater was distilled by heating 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 average contents of sodium (Na), magnesium (Mg), potassium (K) and calcium (Ca) in seawater.

Reference example 2
Table 1 shows the contents of only the above-mentioned four elements (four kinds of metal ions) of 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 the “water such as mineral water” obtained in the above examples, comparative examples and reference examples are shown. It is described in 1. The contents of sodium (Na) and potassium (K) were measured using atomic absorption spectrophotometry, and the contents of calcium (Ca) and magnesium (Mg) were measured using ICP emission spectrometry.

The results in Table 1 are the contents containing only four kinds of limited metal ions, and thus do not sufficiently show the above-mentioned effects of the present invention, but Examples 1 to 3 and Comparative Examples 1 to 13 are compared. As for the content of sodium (Na), Examples 1 to 3 were large, but Comparative Examples 1 to 13 were all less.
Further, the contents of magnesium (Mg) were large in Examples 1 to 3, but were lower in all of Comparative Examples 1 to 13 except for Comparative Example 9.
Further, the content of potassium (K) was large in Examples 1 to 3, but was lower in all of Comparative Examples 1 to 13 except for Comparative Examples 7 and 11.
Further, regarding the content of calcium (Ca), Examples 1 to 3 were small, but except for Comparative Example 6, all of Comparative Examples 1 to 13 were larger than them.

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

Further, other trace components (composition) that have not been measured may influence the above-described effects of the present invention.

<< Evaluation of mineral water >>
Evaluation example 2
The three types of mineral water obtained in Examples 1 to 3 were each taken in 100 mL portions and slowly drunk and examined for flavor.
Further, the water obtained in Comparative Examples 1 to 5 and Comparative Example 21 was also drunk in the same manner as described above, and its flavor was examined and compared.
As a result, the mineral water obtained in Examples 1 to 3 had a flavor (taste and fragrance) that was clearly different from the water obtained in the comparative example.

Evaluation Example 3
50 g of ethanol and 10 g of glycerin were added to 1 L of each of the three types of mineral water obtained in Examples 1 to 3 and applied to the back of the hand 5 times a day for 10 days for evaluation.
Further, the water 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, the mineral water obtained in Examples 1 to 3 was different from the water obtained in Comparative Examples and was similar to a living body, and thus was found to be excellent as a raw material for skin lotion.

Evaluation Example 4
In a field of about 2 m ² , using the same soil and the same fertilizer, the three mineral waters obtained in Examples 1 to 3 were always sprinkled, and the green onions and spinach were grown and harvested. The harvested long onion and spinach were boiled and evaluated under the same conditions.
Moreover, the long onion and spinach which were grown by sprinkling water obtained in Comparative Example 21 and normal agricultural water were also evaluated and compared in the same manner as described above.
As a result, the mineral water obtained in Examples 1 to 3 was different from those obtained using Comparative Example 21 and ordinary agricultural water, and the flavor (especially smell) of the long onion and spinach differed. It was delicious.

The long onion and spinach grown by constantly sprinkling the three mineral waters obtained in Examples 1 to 3 are faster than Comparative Example 21 and the long onion and spinach grown by sprinkling normal agricultural water. However, it was 10% to 100% (twice) faster.
When hydroponically cultivated, the root volume was about twice that of the comparative example.

<Production and evaluation of salt mixture>
Comparative Examples 31, 32, 33
Commercially available salt described in Table 2 was obtained and used to evaluate as described below.

Evaluation Example 5
The salt mixture of Example 1 and the metals of each of Comparative Examples 31 to 33 and sodium chloride were analyzed by the method described in the salt test method 4th edition at the salt business center and seawater research institute, which are analytical institutions. 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 amount of sodium chloride (NaCl) and sodium (Na) in the salt mixture of Example 1 obtained by using the evaporation solid-liquid separation method was smaller than the salt of Comparative Examples 31 to 33, which are commercially available products. .
On the other hand, regarding the amounts of magnesium (Mg), potassium (K), and calcium (Ca), all of the salt mixture of Example 1 was more than potassium (K) of Comparative Example 33.

Evaluation Example 6
Using each of the salt mixture obtained in Examples 1 to 3 and 30 g of the commercial salt of Comparative Example 31, each of them was dissolved as much as possible in the same amount of water at 25 ° C. An aqueous solution was prepared. The concentrated aqueous solution was close to a saturated aqueous solution.
When the solution was allowed to stand at 25 ° C. for 10 days, no change was observed in the concentrated aqueous solutions of the salt mixtures obtained in Examples 1 to 3, but the concentrated aqueous solution of the commercial salt of Comparative Example 31 was not crystallized in the container wall. It was deposited on one side.
Since the salt mixture obtained in Examples 1 to 3 was a mixture of many salts, crystallization (precipitation) of sodium chloride (NaCl) was inhibited.

Evaluation Example 7
Eggplant pickles 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).

The salt mixture and mineral water obtained by the evaporating solid-liquid separation method of the present invention are considered to be different from the conventional salt mixture and mineral water in that they have different component compositions, water cluster structures, etc. It is useful as cosmetics, health foods, general foods, agricultural water, fish water, etc.
Therefore, the present invention is widely used in the fields of health foods, general foods, cosmetics, medicines and agricultural chemicals, agriculture, fisheries, and the like.

DESCRIPTION OF SYMBOLS 1 Drive water inlet piece 2 Inlet side flange 3 Suction pipe 4 Suction hole 5 Partition plate 6 Main pipe throat 7 Outlet piece 8 Outer pipe 9 Output side flange 10 Flange 11 Intake pipe 12 Muffler 12a Horizontal part 12b Vertical part 12c Termination 14 Return pipe 15 Discharge pipe 16 Circulation pump 17 Water tank water level 18 Overflow vent 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 portion 112a Rotating concave portion 112b Rotating concave portion 113a Rotating concave portion 113b Rotating concave portion 114a Rotating concave portion groove 114b Rotating concave portion groove 115a "C" shape 115b "C" shape 120 heating Unit 12 Steam chamber 122 steam supply device 130 gas outlet 131 gas pipe 140 powder outlet 200 condenser 300 the pressure reducer 301 water ejector 302 water circulation pump 303 water tank 400 collection container 404 Ekito outlet A sea B salt mixture C mineral water R rotational direction

Claims (10)

1. An evaporative solid-liquid separation method in which seawater is separated into evaporated solid and liquid, and separated into a salt mixture and mineral water,
   At least during the main evaporative solid-liquid separation, the temperature of the seawater is maintained at 25 ° C. or higher and 60 ° C. or lower, and the pressure in the container is maintained at 1 kPa or higher and 20 kPa or lower using a decompressor. Separation method.
2. The evaporative solid-liquid separation method according to claim 1, wherein seawater is subjected to evaporative solid-liquid separation by performing at least all of the following operations (1) to (4).
   (1) A heating operation for heating the inside of the container with a heating unit so that the temperature of the seawater is maintained within a temperature range of 25 ° C. or more and 60 ° C. or less during at least main evaporation solid-liquid separation;
   (2) During at least main evaporative solid-liquid separation, the water ejector is decompressed using a decompressor to maintain the inside of the container at 1 kPa or more and 20 kPa or less, and the seawater is removed by the evaporation heat of water contained in the seawater. A cooling operation for cooling and maintaining the temperature of the seawater in a temperature range of 25 ° C. or higher and 60 ° C. or lower;
   (3) A liquefaction operation for liquefying the gas flowing out of the container using a cooler to obtain mineral water;
   (4) Taking out the salt mixture remaining in the container from the powder outlet of the container to obtain a salt mixture
3. The evaporative solid-liquid separation method according to claim 2, wherein the water ejector has a gas discharge capacity of at least 20 m ³ / hour of atmospheric pressure when converted into a container having an internal volume of 1 m ³ .
4. The evaporative solid-liquid separation method according to claim 2 or 3, wherein the water ejector is a lateral injection type water ejector having a water circulation pump.
5. When the volume of the container is V [L] and the mass of seawater charged into the container is M [kg], V [L] is set to be 2 to 5 times M [kg]. The evaporative solid-liquid separation method according to any one of claims 1 to 4.
6. A method for producing a salt mixture, characterized in that seawater is subjected to evaporative solid-liquid separation using the evaporative solid-liquid separation method according to any one of claims 1 to 5.
7. A method for producing mineral water, characterized by evaporating solid-liquid separation of seawater using the evaporative solid-liquid separation method according to any one of claims 1 to 5.
8. An evaporative solid-liquid separation device for an evaporative solid-liquid separation method according to any one of claims 1 to 5,
   An evaporative solid-liquid separation device comprising: a container having at least a stirrer, a heating unit, and a powder outlet; a decompressor that is a water ejector; and a cooler.
9. A salt mixture obtained by evaporating solid-liquid separation of seawater using the evaporating solid-liquid separation method according to any one of claims 1 to 5.
10. A mineral water obtained by evaporating solid-liquid separation of seawater using the evaporating solid-liquid separation method according to any one of claims 1 to 5.
    
    

Images