KR20110014744A

KR20110014744A - Method to produce a drinking-water from the deep seawater or the surface seawater

Info

Publication number: KR20110014744A
Application number: KR1020090072235A
Authority: KR
Inventors: 박귀조; 서희동
Original assignee: 박귀조
Priority date: 2009-08-06
Filing date: 2009-08-06
Publication date: 2011-02-14

Abstract

The present invention relates to a method for producing a beverage from deep sea water or surface sea water, and more particularly, to desalination, sterilization, and hardness control of deep sea water or deep sea water in a clean area deeper than 200 m at sea level. It relates to a method of producing a beverage.

To this end, the present invention in the production of beverages from deep sea or surface sea water, the pretreatment step of producing filtered water by pretreatment of the suspended solids in the water by taking the deep sea or surface sea water, the salt contained in the filtered water First desalination step of producing first demineralized water by primary desalination by extraction, sterilization step of producing sterilized water by sterilizing the first demineralized water, and second desalting treatment of fresh water The secondary desalination step to produce the neutralization and hardness adjustment of the fresh water, and then characterized by consisting of the step of producing a beverage after filling, packaging and inspection of the container.

Deep sea water, surface sea water, beverages, desalination, sterilization, hardness adjustment

Description

Method to produce a drinking-water from the deep seawater or the surface seawater}

In general, when desalination of seawater is used to produce beverages, the reverse osmosis treatment is mainly performed as in Document 1 to Document 4, but seawater, such as surface seawater or deep sea water, has a salt concentration in the range of 3.4 to 3.5 wt%, The osmotic pressure of the brine is about 25 atmospheres (atm) in order to desalination it is supplied to the reverse osmosis filtration device at a high pressure of 50 to 60 atm to desalination 35 to 45% of the inflow flow high operating cost is required In addition, the fouling of the membrane (Fouling) is so severe that there is a problem of high maintenance costs are not widely used as a drink.

In the case of producing beverages, sterilization is carried out at the final stage. However, in the case of producing beverages from seawater, bromine (Bromine) compounds and organic substances contained in seawater are present. ₂ ), chlorine dioxide (ClO ₂ ), hypochlorite (NaClO, KClO, Ca (ClO) _2, etc.), chlorine oxide (Cl ₂ O), chloroisocyanurates, hydrogen peroxide (H ₂ O ₂ ), ozone Oxidizing substances such as sterilization by oxidizing agents such as (O ₃ ), sterilization by radiation (γ-ray) irradiation, sterilization by electron beam irradiation, sterilization by electrooxidation, and discharging treatment by high-frequency high-voltage power supply. When produced and sterilized, bromate salt, chloric acid (HClO ₃ ), chloroacetic acid, dichloroacetic acid, chloroform, dibromochloromethane, which are harmful to humans (Dibromochlorometha ne), trihalomethane, trichloroacetic acid, bromoform, bromoform, bromodichloromethane, formaldehyde, etc. have.

Literature Information of the Prior Art

[Document 1] Korean Patent Registration No. 10-0589795 (June 07, 2006)

[Document 2] Japanese Patent Registration No. 4088788 (March 07, 2008)

[Document 3] Japanese Patent Registration No. 3634237 (January 7, 2005)

[Document 4] Japanese Patent Registration No. 3557125 (May 21, 2004)

The present invention is a method that can solve the problems in the prior art, pretreatment filtration by taking deep sea water or surface seawater, the first desalination treatment by the electric extraction method, the sterilization treatment after adjusting the pH, the second desalination by reverse osmosis It is an object of the present invention to provide a method for producing a beverage by adjusting the neutralization and hardness of fresh water produced by treatment.

In the present invention, in the production of beverages from deep sea water or surface sea water, the pretreatment step of producing filtered water by pretreatment of the suspended solids in the water by taking the deep sea water or surface sea water, the salt contained in the filtered water to the electrical extraction First desalination step to produce the first demineralized water by the first desalination treatment, sterilization step to produce sterilization water by sterilizing the first demineralized water, second desalination treatment of the sterilized water to produce fresh water (淡水) The second desalination step, the neutralization and hardness adjustment of the fresh water, characterized in that consisting of the step of producing a beverage after filling, packaging and inspection of the container.

In the present invention, since the mineral water is adjusted to the fresh water desalted in deep seawater or superficial seawater, the mineral water is adjusted so that the beverage can be produced with excellent water taste and hygienically safe drinking water. It is expected to be widespread in production.

The deep sea waters of deep seabeds or clean areas deeper than 200m from the sea level contain various minerals as shown in Table 1 "Analysis of Deep Sea Waters and Surface Seawater". Available as a drink.

Table 1 Analysis of Principal Components of Deep Sea Water and Surface Sea Water

Item Deep ocean water Surface waters
General item Water temperature （℃） 1 to 3 16.5-24.0 pH 7.98 8.15 DO dissolved oxygen (mg / l) 7.80 8.91 TOC Organic Carbon (mg / l) 0.962 1.780 Soluble evaporation residue (mg / l) 40,750 37,590 M-alkalido (mgCaCO ₃ / L) 114.7 110.5
Major element Cl chloride (mg / l) 22,370 21,920 Na sodium (mg / l) 10,800 10,300 Mg magnesium (mg / l) 1,300 1,310 Ca calcium (mg / L) 456 441 K potassium (mg / L) 414 399 Br bromine (mg / L) 68.8 68.1 Sr Strontium (mg / L) 7.77 7.61 B boron (mg / L) 4.44 4.48 Ba barium (mg / l) 0.044 0.025 F fluorine (mg / L) 0.53 0.56 SO ₄ ^2- Sulfate ion (mg / l) 2,833 2,627
Nutrients NH ₄ ⁺ ammonia nitrogen (mg / l) 0.05 0.03 NO ₃ ^- Nitrogen Nitrate (mg / l) 1.158 0.081 PO ₄ ^3- phosphate (mg / l) 0.177 0.028 Si silicon (mg / l) 1.89 0.32
Trace elements Pb lead (μg / ℓ) 0.102 0.087 Cd cadmium (µg / l) 0.028 0.008 Cu copper (㎍ / ℓ) 0.153 0.272 Fe iron (㎍ / ℓ) 0.217 0.355 Mn manganese (μg / L) 0.265 0.313 Ni nickel (µg / l) 0.387 0.496 Zn zinc (µg / l) 0.624 0.452 As arsenic (㎍ / ℓ) 1.051 0.440 Mo molybdenum (㎍ / ℓ) 5.095 5.555 Bacteria Viable count (dog / ml) 10 ² 10 ⁴ ^3-10

As shown in Table 1, "Analysis of Major Components of Deep Sea Water and Superficial Sea Water," the deep sea water and superficial sea water contain 4.44-4.48 mg / L of boron (B), and boron (H ₃ BO ₃ ) and boron is difficult to remove by reverse osmosis because boron has a small particle size of 0.23Å. In addition, boric acid (H ₃ BO ₃ ) in water has a dissociation constant pKa of about 9, which is almost undissolved in water, and hardly exists in an ionic state. However, there is a problem that the treatment is difficult even by the electric extraction method. Thus, boric acid is treated with resin adsorption, coagulation sedimentation, and pH in an alkali (Alkali) range of 9 to 11 to convert boric acid to poly boric acid in a gel state and filtered in reverse osmosis filtration. Boric acid should be removed.

When boric acid in water is subjected to alkali treatment, it is converted into polyboric acid in gel state by the following reaction formula (1).

B (OH) ₃ + OH ^_ → [B (OH) ₄ ] ^- → [B ₃ O ₃ (OH) ₄ ] ^- → [B ₄ O ₅ (OH) ₄ ] ^2- → [B ₅ O ₆ (OH ) ₄ ] ^- … (One)

In general, the sterilization of drinking water is sterilization by heating to 110-120 ° C, heat sterilization under high pressure, sterilization by ultraviolet irradiation, sterilization by radiation (γ-ray) irradiation, sterilization by irradiation of heat or photoelectron beam, and electrooxidation. Sterilization by sterilization, sterilization by injection of oxidant (sterilizer), sterilization by discharge treatment of high frequency high voltage power supply, sterilization by pressure energization treatment, pulse treatment of AC high electric field Combination of one or more sterilization methods, such as sterilization by Joule's heat generated by applying AC power, sterilization by energization of DC power, or magnetization (also called magnetic treatment) It is sterilized by.

In the case of producing beverages from mineral water or tap water from river water, sterilization is carried out in the final stage, but in the case of producing beverages from sea water, bromine (Bromine) compounds and organic substances are present in trace amounts. Chlorine (Cl ₂ ), chlorine dioxide (ClO ₂ ), hypochlorite (NaClO, KClO, Ca (ClO) _2, etc.), chlorine oxide (Cl ₂ O), chloroisocyanurates, hydrogen peroxide (H ₂ Sterilization by oxidizing agents such as O ₂ ) and ozone (O ₃ ), sterilization by radiation (γ-ray) irradiation, sterilization by electron beam irradiation, sterilization by electro-oxidation, discharging treatment by high frequency high voltage power supply when sterilized by generating oxidants as is harmful to the human body bromine salt (Bromate salt), acid (HClO _3), chloroacetic acid (Chloroacetic acid), dichloroacetic acid (Dichloroacetic acid), chloroform (chloroform), d' Oxidation reactions such as dibromochloromethane, trihalomethane, trichloroacetic acid, bromoform, bromodichloromethane, and formaldehyde will be produced. It is recommended to avoid sterilization methods in which oxidants or oxidizing substances are produced.

However, in the case of sterilization by a sterilization method in which an oxidizing agent or an oxidizing substance is produced, the nano-filtration process or reverse osmosis of the final desalination process is carried out before the final desalination process and the oxidizing reactants, sterilized microorganisms and their spores harmful to the human body are treated. Sterilization should be carried out as a process of removing with salinity in the administration process.

Chlorine (Cl ₂ ), Chlorine Dioxide (ClO ₂ ), Hypochlorite (NaClO, KClO, Ca (ClO) _2, etc.), Chlorine Oxide (Cl ₂ O), Chloroisocyanurates, Hydrogen Peroxide (H ₂ O ₂ ), Sterilization by injecting an oxidizing agent such as ozone (O ₃ ), or electrooxidation, irradiation of an electron beam, radiation or gamma ray, or high frequency. In the case of sterilization treatment in which oxidative substances are generated, such as discharge treatment of high voltage power source, bromine component in saline is oxidized, which is carcinogenesis and deformity to fetus. The reaction mechanism in which bromate salt, which is a teratogenesis substance that causes the formation of bromine, is produced, is represented by the following reaction formulas (2) to (4).

Br ⁻ (Bromide ion) + O ₃ (Ozone) → BrO ⁻ (Hypobromite ion) + O ₂ ... … (2)

^{_{BrO - + O 3 → BrO 2}} - (Bromite ion) + O 2 ... … … … … … … … … … … … … (3)

BrO ₂ ⁻ + O ₃ → BrO ₃ ⁻ (Bromate ion) + O ₂ . … … … … … … … … … … … (4)

Therefore, if the above-mentioned deep seawater or superficial seawater is desalted to produce a drink, the method does not cause fouling of the membrane in the reverse osmosis membrane due to calcium salt and a reasonable sterilization method in which no harmful substances are produced in the human body. This must be taken.

Therefore, in the case of producing a beverage by desalination of the deep sea or superficial seawater, there is a method of preventing fouling of the membrane in the reverse osmosis membrane due to calcium salt and a reasonable sterilization method in which no harmful substances are generated in the human body. Should be taken.

In the present invention, while solving the above problems, a method of reasonably producing a beverage from deep sea water or surface sea water, with reference to the accompanying drawings in detail as follows.

Ⅰ. Pretreatment stage

1. Intake process

Intake of deep sea water from the deep sea deeper or deeper than 200m from the sea surface in a clean area can be taken from the ship's top, or piped to the intake point, or a water well is installed below the sea level. It is collected by the siphon principle and sent to the sump.

In case of deep sea water collected in the sump, the temperature is low and the viscosity is high. The heating method may be supplied with heat from a boiler, or may use surface seawater in summer.

2. Pretreatment Filtration Process

The pretreatment filtration process uses sand filters to remove suspended solids (SS) in water.

At this time, the filtration pressure is determined in consideration of the pressure loss of the filter and the pressure loss of the pipe according to the operating conditions.The filtration speed of sand filtration is 6-10 m / hour, and the effective diameter of the filter sand is 0.3-0.45 mm, the uniformity coefficient shall be 2.0 or less, and the thickness of the filtrate layer shall be 0.5-1.0 m.

The sand filtration is a rapid sand filtration or a slow sand filtration, and select one of the two depending on the amount and concentration of suspended solids in the water, in the case of rapid sand filtration rate of 120 ~ 200m / day, the thickness of the filtrate It is designed to 60 ~ 70㎝, in the case of slow sand filtration, the filtration rate is 4 ~ 5m / day, the thickness of the filter layer is designed to 70 ~ 90㎝.

At this time, the turbidity of the superficial seawater or deep seawater withdrawn is less than 2 degrees (NTU, Nephelometric Turbidity Unit), and the low concentration of suspended solids does not cause sand filtration.

3. Adsorption process of organic matter

If the concentration of organic matter is high in the surface seawater from which suspended solids are removed in the pretreatment filtration process, the seawater from which suspended matter is removed from sand filtration is sent to an adsorption column filled with activated carbon to adsorb and remove organic matter in the water. Send to precision filtration process.

The adsorption column is filled with activated carbon at a linear velocity of 4 to 10 m / hour and a residence time of at least 1 hour.

If the concentration of COD _Mn in seawater is 3 mg / l or less and the concentration of organic matters is not a problem, the adsorption step of organic matters is omitted.

4. Precision filtration process

The first stage desalination treatment is carried out by filtering the surface seawater or the deep seawater treated in the pretreatment filtration process and the organic material adsorption process alone or in combination of two kinds of microfilters or ultrafiltrations. Suspended solids (SS), which can cause fouling of membranes in the process, nanofiltration and reverse osmosis filtration, have a water fouling index (FI) of 2 to The filtered water filtered in the range 4 is sent to the first desalination process by electroextraction of the first desalination step.

The FI value is a numerical value representing the fine turbidity concentration in the target water and is expressed as in the following equation (5).

FI = (1-T ₀ / T ₁₅ ) x 100/15... … … … … … … … … … … … … … … … (5)

T ₀ is the time required for filtration of the first 500 mL of sample water when the sample water was filtered under pressure of 0.2 MPa using a 0.45 μm microfiltration membrane, and T ₁₅ was filtered for 15 minutes in the same state as T _0. It is the time required for the filtration of 500 ml of sample water later.

The microfilter and ultrafilter are not limited to the type of filtration membrane, and the supply pressure of the pump is determined in consideration of the filtration speed and the pressure loss according to the vendor specification.

II. First desalination step

The most important part in the production of beverages by desalination of surface seawater or deep sea water is the first desalination process.In general, when desalination of seawater is used to produce drinks, reverse osmosis is mainly performed. The same seawater has a high osmotic pressure, so when desalting a 1st stage desalination with a reverse osmosis filtration system, it must be operated at a high pressure. Therefore, the operation cost is high and the fouling phenomenon of the membrane is high. There is.

In addition, the electrodialysis method has a high operating cost than reverse osmosis because it is removed from the anode chamber and the cathode chamber due to the decomposition of salt in the anode chamber and the cathode chamber due to the distance between the anode and the cathode. Is in.

Therefore, in the present invention, the process of primary desalination is applied by the method of extracting the salt in the brine by the following electrical attraction, and the details are shown in FIG. 2 "Description of the primary desalination mechanism by the electroextraction process". When described in detail with reference to as follows.

1. Primary desalination process by electric extraction

In the present invention, in order to solve the problem of high power consumption when desalting seawater such as surface seawater or deep seawater by reverse osmosis or electrodialysis, the anode 5 and the cathode 6 inside the salt extraction chamber 3. Desalination apparatus (in the present invention referred to as "electric extraction process") provided with a desalination chamber (4) separated by a cation exchange diaphragm (8) and an anion exchange diaphragm (7), attached drawings When described in detail with reference to as follows.

FIG. 2 is a diagram illustrating the first desalination treatment mechanism by the electroextraction process, wherein the negative electrode 6 is the positive ion between the positive electrode 5 and the negative electrode 6 installed inside the salt extraction chamber 3. Surface seawater or deep sea water by a desalination device by an "extracting process" consisting of an exchange membrane 8 and an anode 5 membrane with an anion exchange membrane 7 and an isolated desalination chamber 4. Desalination of seawater such as

Seawater, such as pre-treated surface seawater or deep seawater, is supplied to the desalination chamber 4 while supplying the seawater of the seawater storage tank 1 to the salt extraction chamber 3 and the desalination chamber 4 by the seawater transfer pump 2. The air in the air is aerated from the air blower 10 through the diffuser 11, and a direct current of 4 to 50 volts is applied from the rectifier to the desalination chamber 4 to generate an electric field. When the electric field is formed, the cations (Na ⁺ , K ⁺ , Ca ²⁺ , Mg ²⁺ , Fe ²⁺ , Fe ³⁺ ,) contained in the seawater of the desalting chamber 4 by electrophoresis. Zn ²⁺ ..., etc.) is moved to the cathode 6 side of the cation-exchange membrane (8) transmitted by salt extraction chamber 3, the anion ^{(Cl -, Br -, NO} 3 -, SO 4 2-, _{^{_{^{HCO 3 -, CO 3 2-,}}}} HPO 4 2-, PO 4 3- ... , etc.) as to move to the positive electrode 5 is extracted by passing through the anion exchange membrane (7) on the side of the salt chamber (3), the extracted salt In the chamber (3), the concentrated brine is discharged, and in the desalting chamber (4), This salt is treated yudoen primary desalting. Primary demineralized water is sent to the sterilization step.

The concentrated brine is moved from the desalting chamber (4) to the salt extraction chamber (3) to send salt production and mineral components to produce salts and mineral salts (salt water).

The concentration of salin in which salt contained in the seawater in the desalting chamber 4 is transferred to the salt extraction chamber 3 by electrical attraction is the BOMEDO specific gravity indicator controller (BIS :) installed in the salt extraction chamber (3). Adjust the inflow of pretreated seawater so that the specific gravity of Baume's hydrometer indicating switch is in the range of 6-12 ° Be. At this time, if the specific gravity of the bomedo in the salt extraction chamber (3) is lower than 6, the power consumption may increase because the liquid resistance is large. If the specific gravity of the bomedo is 12 or more, CaSO ₄ and CaCO ₃ having low solubility in water Since the precipitation of salts occurs, the salt concentration in the salt extraction chamber (3) needs to adjust the flow rate of the incoming seawater so that the specific gravity of Bumedo is maintained in the range of 6-12 ° Be.

The Bomedo (° Be) of the Baume's hydrometer, which shows the specific gravity of the brine, is pure water at 0 ° Be, 15% saline at 15 ° Be, and divided into 15 equal parts. In the case of brine, the relationship between the specific gravity (° Be) and the specific gravity (d) of Bume is given by the following equation (6). In addition, in the case of sea water, bomedo (° Be) approximates the salt concentration (wt%), and thus is widely used as a measure of concentration.

d = 144.3 / (144.3- ° Be). … … … … … … … … … … … … … … … … … (6)

The salt concentration in the demineralized primary desalted water supplied to the desalination chamber (4) by supplying the seawater of the pretreated seawater storage tank (1) to the desalination chamber (4) is an electrical conductivity indicator controller (ECIS) installed in the primary demineralized water discharge line. : Supplying the seawater of the pretreated seawater storage tank 1 to the desalination chamber 4 by the seawater transfer pump 2 so that the electric conductivity of the electric conductivity indicating switch is maintained in the range of 5 to 12 mW / cm. Adjust the inflow of seawater.

If the value of the electrical conductivity is 5 kW / cm or less, the capacity of the device increases, and there is a problem in that the power consumption increases due to the increase in the liquid resistance. Since there is a problem of lowering the efficiency of the secondary desalination treatment, the primary demineralized water is desalted in an electric conductivity range of 5-12 mW / cm and then sent to a sterilization step.

The conductivity measured in the electrical conductivity indicator controller is an indicator of the degree of conduction of an aqueous solution and is widely used as a standard for representing salt concentration in water.The unit is ㎳ / cm (Siemens) corresponding to the inverse of the electrical resistivity of the aqueous solution. / meter), and the relationship between the electrical conductivity (EC) and the total soluble salt (TSS) in water is shown in the following equation (7).

TSS (ppm) = 640 X EC (mm / cm). … … … … … … … … … … … … … … (7)

The conductivity value is expressed in units of millimenss / meter, or microsiemens / centimeter, which is an international system of units, and ㎳ / m = 10 μs / cm (or 10 μmhos / cm).

In actual desalination apparatus, the desalination chamber (4) is provided by providing a cation exchange diaphragm (8) at the cathode 6 side and an anion exchange diaphragm (7) at the anode 5 side in the salt extraction chamber 3 (4). Seawater storage tank (1) installed between the anode (5) and the cathode (6), and pretreated in the desalination chamber (4) of the desalination apparatus by electric extraction alternately and repeatedly installed according to the processing capacity. Supplying seawater to the seawater transfer pump (2) while applying direct current electric current from the rectifier to form an electric field in the desalination chamber (4), the electrophoresis causes salt to be extracted into the salt extraction chamber (3). The desalination apparatus for extraction and desalination is applied.

In the desalination treatment of salts contained in seawater, the salt extraction chamber (3) and the desalting chamber (4) of the seawater of the seawater storage tank (1) pretreated in the desalting apparatus subjected to desalting treatment by electric extraction to the seawater transfer pump (2). While supplying air from the air blower 10 to the diffuser 11 installed below the salt extraction chamber 3 and aeration, and directing the DC electricity of 4 to 50 volts from the rectifier to the anode 5 When an electric field is formed in the desalination chamber 4 by applying it to the cathode and the cathode 6, the cations contained in the seawater of the desalination chamber 4 by electrophoresis are discharged to the cathode 6 side. The cation exchange diaphragm 8 is transferred to the salt extraction chamber 3, and the anion passes through the anion exchange diaphragm 7 on the anode 5 side to the salt extraction chamber 3, while the desalting chamber The salts contained in the seawater in (4) are desalted.

The above-described electrochemical reaction mechanism in which salts in seawater are desalted by a desalting apparatus by electroextraction is as follows.

In the case of NaCl in the salt contained in seawater, NaCl is dissociated into Na ⁺ ions and Cl ^- ions by hydrolysis in seawater as shown in the following reaction formula (8).

_{^{NaCl -H 2 O → Na + +}} Cl - ... … … … … … … … … … … … … … … … … (8)

When a direct current is applied from the rectifier to the positive electrode 5 and the negative electrode 6 to form an electric field inside the desalination chamber 4, Na ⁺ , K ⁺ , Ca contained in seawater in the desalination chamber 4 by electrophoresis. Cations such as ²⁺ , Mg ²⁺ , and Sr ²⁺ pass through the cation exchange diaphragm 8 on the cathode 6 side and move to the salt extraction chamber 3, and Cl ⁻ , Br ⁻ , SO ₄ ^2- Anion, such as anion, penetrates the anion exchange diaphragm 7 toward the anode 5 and moves to the salt extraction chamber 3, while salts (NaCl, KCl, CaSO ₄ , CaCO ₃ , MgCl) from seawater of the desalination chamber 4 are transferred. ₂ , MgSO ₄ , MgBr ₂ , SrSO ₄ ...) Are removed (desalting). In the case of NaCl, the reaction mechanism is as follows.

Na ⁺ --septum-> Na ⁺ ... … … … … … … … … … … … … … … … … … … (9)

Cl ^{- -} Diaphragm ^- → Cl - ... … … … … … … … … … … … … … … … … … 10

Na ⁺ ions and Cl ⁻ ions transferred to the salt extraction chamber 3 are in situ in the original NaCl state.

Na ⁺ + Cl ⁻ —H ₂ O → NaCl... … … … … … … … … … … … … … … … … … (11)

On the anode 5 and cathode 6 sides, if the following side reactions occur, odor generation and power consumption may increase. Therefore, air from the air blower 10 is diffused to the diffuser. : Aeration through 11) to minimize the following side reactions.

^{_{2Cl - → Cl 2 (aq)}} + 2e - ... … … … … … … … … … … … … … … … … … … … (12)

Cl _{2 (aq)} → Cl _{2 (g)} ↑. … … … … … … … … … … … … … … … … … … … … (13)

Cl _{2 (aq)} + H ₂ O → HClO _(aq) + HCl... … … … … … … … … … … … … … … … (14)

_{^{2HClO (aq) + 2H + +}} 2e - → Cl 2 (g) ↑ + 2H 2 O ... … … … … … … … … … … (15)

_{^{2H 2 O + 2e - → 2OH}} - + H 2 (g) ↑ ... … … … … … … … … … … … … … … … … (16)

At this time, the supply amount of air supplied from the air blower 10 through the diffuser 11 is such that the intensity of aeration is 1.2 to 2.0 [air (m 3) / bath volume (m 3 · hour)].

A feature of the present invention is that salts (NaCl, etc.) are not desalted by decomposing reactions at all compared to the desalting method by electrolysis or electrodialysis, and are contained in seawater in the desalting chamber 4. When the salt is applied to the positive electrode 5 and the negative electrode 6 from the rectifier to form an electric field, electrophoresis causes cations (Na ⁺ , K ⁺ , Ca ²⁺ , Mg ²⁺ , Sr ^2+, etc.). After passing through the cation exchange diaphragm 8 on the negative electrode 6 side and moving to the salt extraction chamber 3, anions (Cl ⁻ , Br ⁻ , SO ₄ ² ⁻ , etc.) are transferred to the anion exchange diaphragm ( 7) Because it moves to the salt extraction chamber (3) and is extracted and removed in situ reaction in the state of the original salt, it is characterized by low power consumption because salt does not consume current due to decomposition. have.

The salt extraction chamber (3) and the desalting chamber (4) are made of flame resistant stainless steel, titanium, epoxy coating or lining of carbon steel. Lining the glass fiber reinforced plastic (FRP).

The material of the negative electrode (6) plate is a lining treatment of Raney nickel on a steel plate having a high hydrogen generation overvoltage, but a flame-resistant stainless steel or titanium plate is used. The anode (5) plate is a die plate coated with TiO ₂ -RuO ₂ on a titanium plate made of a material having high corrosion resistance and high oxygen and chlorine generation overvoltage. DSA: Use a dimensionally stable anode (DSA) electrode.

Seawater is removed by removing all monovalent salts (NaCl, KCl, KBr, etc.) and polyvalent salts (多價鹽, MgCl ₂ , MgSO ₄ , CaSO ₄ , FeCl ₂ , FeCl ₃ , SrSO ₄ . In the case of the desalting treatment, the cation exchange diaphragm 8 on the cathode 6 side uses a cation exchange diaphragm which permeates all cations, and the anion exchange diaphragm 7 on the positive electrode 5 side anion exchange penetrates all anions. Use a diaphragm.

However, even if the desalination efficiency is slightly decreased, the diaphragm on the positive electrode 5 side and the negative electrode 6 side is equally asbestos, nylon, polypropylene, and polyvinylidene fluoride in consideration of economical efficiency. Poly vinylindene fluoride, Polyolefin, Polyethylene, Polyester, Hexafluoropropylene, Polyfluoroolefin, Tetrafluoroethylene or Polytetrafluoroethylene One kind of membrane may be used among (PTFE: Polytetrafluoroethylene).

The cation exchange diaphragm which permeates all cations is a load-electrode membrane which fixes negatively charged R-SO ₃ ^- in the main chain of a polystyrene-divinylbenzene system. In order to selectively permeate monovalent cations to the surface of the membrane selectively, cationic polymer electrolytes such as polyethyleneimine are coated or bonded in a thin layer to prevent modification. Cation exchange membranes are used.

The anion exchange diaphragm that permeates all anions is a positively charged membrane in which primary and tertiary amines or primary and tertiary amines or ammonium groups are immobilized in the polymer chain of the substrate to introduce a cation into the membrane. The membrane which does not modify the surface of a membrane so that a monovalent anion may permeate selectively on the surface of a positive electrode is used.

The diaphragm supporter 9 is flame resistant stainless steel on the outside of the cation exchange diaphragm 8 and the anion exchange diaphragm 7 on a nonwoven fabric made of viscose rayon of 1 to 10 mm thickness or synthetic resin such as nylon. Fix with titanium perforated plate or grid.

Example 1

The specifications of the desalination apparatus as shown in FIG. 2 include the desalination chamber 3 having a capacity of 0.1 m 3 (25 mm × 1,000 mm × 4,000 mm) in a capacity of 3.6 m 3 (750 mm × 1,200 mm × 4,000 mm) of the salt extraction chamber. 2 sheets of DSA (Dimensionally stable anode) coated with a TiO ₂ -RuO ₂ coated on a 1000 mm × 1,200 mm titanium plate, and a cathode 1,000 mm × 1,200 mm titanium plate Titanium plate) 2 sheets alternately installed between both ends of the desalination chamber, and 3,600 mm x 3 mm thick polyester with the same material and size of the diaphragm on the anode side and the diaphragm on the cathode side. A desalting apparatus using a 1,000 mm diaphragm was prepared.

Deep sea water as shown in Table 1 is applied to the positive and negative poles of the desalination unit from a rectifier to 8 Volt DC electricity, and supplying air from the air blower to the salt extraction chamber at a flow rate of 4.5 Nm3 / hour. Was heated to 25 ° C and supplied to the salt extraction chamber while adjusting the Bomedo specific gravity of the BOME installed in the salt extraction chamber within the range of 8 to 10 ° Be. When the electrical conductivity of the electric conductivity indicator controller (ECIS) installed in the discharge line was supplied in the range of 8 to 10 kW / cm, the concentrations of the important salts contained in the primary demineralized water were as shown in Table 2 below.

Table 2 Concentrations of Important Salts in Primary Demineralized Water

Item Na Mg Ca K B Cl Br SO ₄ ^2- Deep Sea Water (mg / ℓ) 10,800 1,300 456 414 4.44 22,370 68.8 2,833 Primary demineralized water (mg / ℓ) 690 416 146 18 2.93 4,032 12.6 850

In the desalination apparatus, the first deep desalted water was discharged at 1.52m 3 / hour, and the concentrated brine was discharged at 0.58m 3 / hour. The current in the rectifier was 16.2 amps.

III. Sterilization Step

In general, the method of sterilizing water includes heat sterilization heated to 110 to 120 ° C., heat sterilization under high pressure, sterilization by ultraviolet irradiation, sterilization by radiation (γ-ray) irradiation, irradiation by heat or photoelectron beam. Sterilization, sterilization by electrooxidation, sterilization by injection of oxidizer (sterilizer), sterilization by discharge treatment of high frequency high voltage power supply, sterilization by pressure energization treatment, pulse of AC high electric field One or more of sterilization by pulse treatment, sterilization by Joule's heat generated by applying AC power, sterilization by energization of DC power, or magnetization treatment (also called magnetic treatment). The sterilization treatment is performed by a combination of sterilization treatment methods.

In the case of producing beverages from mineral water or tap water from river water, sterilization is carried out in the final stage. However, in the case of producing beverages from sea water, bromine (Bromine) compounds and organic substances are present in trace amounts. Chlorine (Cl ₂ ), chlorine dioxide (ClO ₂ ), hypochlorite (NaClO, KClO, Ca (ClO) _2, etc.), chlorine oxide (Cl ₂ O), chloroisocyanurates, hydrogen peroxide (H) ₂ O ₂ ), sterilization by oxidizing agents such as ozone (O ₃ ), sterilization by radiation (γ-ray) irradiation, sterilization by irradiation of electron beam, sterilization by electro-oxidation, discharge treatment of high frequency high voltage power supply In case of sterilization by producing oxidizing material like sterilization, bromate salt, chloric acid (HClO ₃ ), chloroacetic acid, dichloroacetic acid, chloroform (Chlorofor) m), dibromochloromethane, trihalomethane, trihalomethane, trichloroacetic acid, bromoform, bromodichloromethane, formaldehyde, and the like. Because oxidants may be produced, they should not be sterilized by sterile methods that produce oxidants or oxidizing substances.

However, if the sterilization treatment is performed by a sterilization method in which an oxidizing agent or an oxidizing substance is produced, the second desalination treatment is carried out before the second desalting treatment (final desalting treatment), and the second desalination of the oxidizing reactants and the sterilized microorganisms and their spores harmful to the human body is performed. In the reverse osmosis filtration process of the treatment, the sterilization treatment may be performed by removing the salt together with the salt.

Sterilization treatment in the present invention will be described in detail with reference to Figure 3 "sterilization process flow chart" method of sterilization treatment by the magnetization treatment and the constant voltage treatment by AC high voltage as follows.

1. Magnetization process

When the primary demineralized water is supplied to the primary demineralized water storage tank 12, the primary demineralized water is supplied to the magnetization apparatus 14 by the primary demineralized water transfer pump 13 to be magnetized, and then sent to the sterilization tank 16.

The magnetizing device 14 is 0.5 to 5 volts (coil) wound on a cylindrical conductive tube made of an insulating material such as synthetic resin (PVC, PE, styrene resin), ebonite, FRP, Bakelite, etc. A solenoid type magnetizer in which a magnetic field is formed inside the coil when a low voltage current in the Volt range is applied, or a magnetic flux density of 10,000 to 15,000 G (Gauss) Use one type of magnetizer with permanent magnet magnetized in the range.

When the fluid (water) passes through the magnetic field between the north pole and the south pole of the magnetization device 14 at right angles, electromotive force is generated by magneto-hydro-dynamics (MHD). As the group of water molecules collapses and becomes smaller due to electron waves, the surface tension decreases and the penetration force increases, and the redox potential decreases and the water is reformed. In addition, while killing bacteria such as E. coli, Legionella, resistant bacteria contained in the water, while destroying the cells of the bacteria to be sterilized, or inhibit the growth of bacteria.

The sterilization treatment by the magnetization treatment can further improve the sterilization efficiency by treatment in combination with the other sterilization treatment methods mentioned above, rather than by itself. It is a combination of sterilization treatment by constant voltage treatment by AC high voltage and it is a sterilization treatment method that does not produce side reactions harmful to human body.

Important functions such as bacterial cell division and osmosis control of cell membranes are controlled by weak electric signals (pulse signals) in cells. When water is magnetized in the magnetic field of the magnetization device, direct current flows by electromotive force, and when direct current is applied directly to the cell membrane of bacteria contained in the water, abnormality occurs in the command system by pulses. It impairs osmotic function, which can finally kill all bacterial cells.

When the primary demineralized water passes through the magnetic field between the north pole and the south pole of the magnetizer 14 at right angles, the generated voltage (E) is determined by the flow rate of water (V) and between the north pole and the south pole of the magnetizer 14. The law of electromagnetic induction proportional to the magnetic force (B) holds, and the MHD potential difference is proportional to the magnitude of the magnetic force and the flow velocity of the fluid.

E = V x B... … … … … … … … … … … … … … … … … … … … … … … … … … (17)

In the magnetization process, the higher the magnetic force (magnetic flux density) of the magnetizing device, the higher the flow rate of the fluid passing through the magnetic field, the higher the magnetization processing efficiency. Therefore, in the present invention, a magnetic flux density of 4,000 to 12,000 G (Gauss) magnet is used, and the cross-sectional area of the magnetic field is set so that the flow rate of the fluid passing through the magnetic field is in the range of 2 to 6 m / sec.

Therefore, when the flow rate is smaller than 2 m / sec in the magnetic field at the flow rate supplied from the primary demineralized water transfer pump 13 to the magnetizer 14, the discharge capacity from the magnetizer 14 is discharged. A part of the flow rate is returned to the primary demineralized water storage tank 12 and operated so that a flow velocity may be 2 m / sec or more in a magnetic field.

As the permanent magnet, neodymium magnet (Nd-Fe-B) or samarium cobalt magnet (Sm-Co) having a high magnetic flux density is preferably used. Because magnetization is processed in very few picoseconds. The residence time of the fluid in the magnetic field is not a big problem.

2. Sterilization process by AC high voltage

The sterilization process by AC high voltage includes a high voltage applying electrode 17 for applying an AC high voltage in the sterilization tank 16 and a ground electrode 18 connected to ground 19 on the ground. It consists of the structure which installed) alternately.

While supplying the primary demineralized water that has been magnetized in the magnetization process to the sterilization tank 16, an AC high voltage of 6,000 to 10,000 volts is output from the output terminal 15e of the AC high voltage generator 15 for 20 minutes to 6 minutes. When applied for a time, bacteria are killed and sterilized, and then sent to the pH adjusting step of the second desalting step.

The AC high voltage generator 15 is a transformer for generating AC high voltage as shown in FIG. 3, and uses an external iron type circular coil type using a stratified iron core 15c, and uses an AC power source having 110 to 220 volts. The current regulated by the variable resistor 15a is connected to the primary winding 15b of the primary circuit of the transformer, and the insulating terminal 15f of the secondary winding 15d is insulated from the secondary circuit of the transformer. The output terminal 15e of the secondary winding 15d is connected to the high voltage applying electrode 17 of the sterilization tank 16. The AC high voltage generator 15 processes ground (15g) on the ground.

An AC power supply of 110 to 220 volts is connected to the AC high voltage generator 15, and the variable resistor 15a is adjusted to provide a voltage of 6,000 to 10,000 volts at the secondary output terminal 15e of the transformer. When an AC high voltage is applied to the high voltage applying electrode 17 of the sterilization tank 16, a constant voltage is generated between the ground electrodes 18 treated with the earth 19 on the ground, and all the water contained in the water is generated. It is sterilized by killing bacteria.

The capacity of the sterilization tank 16 determines the sterilization time according to the state of the primary demineralized water and the applied voltage of the alternating high voltage, but is generally 4 to 6 hours. In addition, the material of the sterilization tank 16 is flame-resistant and corrosion-resistant, and one type of epoxy resin, fiber glass reinforced plastic, or rubber is coated on the concrete structure. Or lining, polyvinyl chloride (PVC), acrylonitrile butadiene styrene copolym (ABS), polyethylene (PE), polyethylene (PP), titanium (titanium), or flame resistant steel.

The high voltage applying electrode 17 and the ground electrode 18 are installed at intervals of 5 to 20 cm, and the material is coated with RuO ₂ -TiO ₂ on a titanium plate or a titanium plate, which is flameproof and corrosion resistant. do.

In addition, the sterilization process by the magnetization treatment process and the alternating high voltage can be sterilized by a batch operation, respectively, when the treatment capacity of the primary demineralized water is small.

[Example 2]

In Example 1, the primary demineralized water subjected to primary desalination was injected into a primary demineralized water storage tank of 2 m 3 (1,400 mmΦ × 1,700 mmH) polyethylene, and the primary demineralized water was transferred at a capacity of 6 m 3 / hour. The primary demineralized water storage tank passes the magnetized water through a magnetic field of a magnetizer equipped with an Nd-Fe-B magnet with a magnetic flux density of 11,200 gauss at 2.5 m / sec. The magnetization treatment was carried out for 30 minutes while conveying at 100%.

In a polyethylene tank 1,200 mm wide x 1,200 mm wide x 1,500 mm high, six titanium plates 1,000 mm wide x 1,000 mm wide x 3 mm thick are installed, three of which are grounded on the earth, and the remaining three are AC high voltages. Injecting the first demineralized water subjected to magnetization into the sterilization tank connected to the output terminal of the device, and applying a high voltage of 9,000 Volts from the AC high voltage generator, the sterilization state was measured by the processing time is shown in Table 3 It was like

Table 3, Results of Sterilizing Primary Demineralized Water

Item Primary demineralized water AC high voltage (processing time) Magnetized water 1 hours 2 hours Viable count (dog / ml) 112 51 6 Not detected

Sterilization treatment of the present invention is a physical sterilization method by a constant voltage treatment to which an alternating current high voltage is applied. It can be seen that complete sterilization is achieved.

Ⅳ. Second desalination stage

1. pH adjustment process

Boron contained in seawater, such as deep seawater or superficial seawater, is difficult to remove simply by reverse osmosis filtration, electrodialysis or electroextraction. As described above, boron is present in the form of boric acid (H ₃ BO ₃ ) in seawater, and boron is difficult to remove by nanofiltration and reverse osmosis because the particle size is small, such as an ion radius of 0.23 Å. In addition, boric acid (H ₃ BO ₃ ) in water has a dissociation constant pKa of about 9, which is almost undissolved in water, and hardly exists in an ionic state. However, there is a problem that the treatment is difficult even by the electric extraction method. Thus, boric acid is treated with an alkali (Alkali) in the pH range of 9-11 to poly (boric acid) in the gel (Poly) boric acid is filtered in reverse osmosis (filtration) to remove the boric acid.

After the first desalination treatment in the first desalination treatment step, the sterilized first desalination water is supplied to the pH adjustment process, and one of NaOH, NaHCO _3, or Na ₂ CO _{3 as} an alkali (Alkali) pH 9-11 The boric acid in water is treated with polyboric acid and then sent to the nanofiltration process or reverse osmosis process. Here, when the sterilized primary demineralized water is adjusted to pH 9-11 and supplied immediately to the reverse osmosis filtration process, when the fouling phenomenon of the membrane is not a problem, the nanofiltration process is omitted and sterilized. Treated primary demineralized water to pH 9-11 to treat boric acid in water with polyboric acid, which is then sent directly to reverse osmosis filtration.

In the pH adjustment step, the pH adjustment method adjusts the pH to 9-11 by injecting the alkaline agent while stirring the propagation time (retention time) for 15 to 30 minutes with a propeller stirrer of 180 to 360 RPM (rotational speed).

2. Nano filtration process

For the transmission order of the ion in the nano-filtration membrane is a cation is Ca ²⁺ ≥Mg ^2+> Li ^+> is ^{_{Na +> K +> NH 4}} +, if the anion is _{^{_{^{SO 4 2- »HCO 3 -> F}}}} -> ^{_{Cl -> Br -> NO 3}} -> and SiO _2, in the case of sulfate ions (SO ₄ ^2-) is hard to permeate than Mg ²⁺ and Ca ^2+.

In the nanofiltration process, the solubility is small, such as CaCO ₃ , CaSO ₄ , and SrSO _{4 in} seawater that is not removed in the first desalting process, and the scale is concentrated in the membrane during the reverse osmosis filtration process. In order to suppress the fouling of the membrane, the filtration water from which calcium component and sulfate ion (SO ₄ ^2- ) is removed is sent to the reverse osmosis filtration device.

The module form of the nano-filter membrane is tubular type, hollow fiber type, hollow fiber type, spiral wound type or flat plate type. Plate and frame can be used to select one type. The structure of the membrane is composed of a dense layer on one side of the membrane. Asymmetric membranes or composite membranes having a very thin separation functional layer formed of different materials on the dense layer of such asymmetric membranes can be used. Although a composite membrane is preferred, the present invention is not particularly limited to the form and structure of the membrane.

The nanofiltration membrane may be made of ceramics, polyamide, polypiperazineamide, polyesteramide, or water-soluble vinyl polymer. It can be used among crosslinked materials, and the material of the film is not particularly limited in the present invention.

In the nanofiltration process, the supply pressure should be determined according to the salt concentration. However, if the supply pressure is greater than 25 atmospheres (atm), the removal rate of calcium components and sulfate ions decreases, so operating at 20 atmospheres or less is possible. desirable. In the case of the spiral nanofiltration membrane, the membrane permeation amount is 0.7 to 1.4 m 3 / m 2 · day, and the membrane permeation amount is 70 to 80% of the inflow.

3. Reverse osmosis filtration process

When the filtered water filtered in the nanofiltration process is supplied to the reverse osmosis filtration process, the operating pressure is supplied to the filtration membrane at 10 to 20 atm, and in the case of the spiral filtration membrane, the membrane permeability is operated at 0.6 to 0.8 m 3 / m 2 · day. The boron-containing water which is not filtered is discharged after the neutralization treatment, and the filtered water filtered to the boron concentration below 0.3 mg / L, the drinking water standard, is sent to the neutralization treatment and the hardness adjustment process.

In the reverse osmosis filter, the module shape of the membrane is also tubular, tubular, hollow fiber type, spiral wound type or flat plate type. One type of shape can be selected and used from a plate and a frame, and in the present invention, the shape of the film is not particularly limited.

The reverse osmosis membrane uses a composite membrane made of acetyl cellulose, aromatic polyamide, polyvinyl alcohol, polysulfone, and the like. In the invention, there is no particular limitation.

In the reverse osmosis filtration process, even if the pH is supplied in an alkaline state of 9 to ₁₁ , scale generation is not a problem since the materials such as CaCO ₃ and CaSO ₄ , which generate scale, are removed in the nano filtration process.

Ⅴ. Steps to produce beverages

1. Neutralization and hardness adjustment process

When the filtered filtrate of the reverse osmosis filtration process is supplied to the neutralization treatment and the hardness adjustment process, acid (HCl, neutralizing agent) is supplied to neutralize the pH in the range of 5.8 to 8.5, which is the standard for drinking water, and the hardness modifier indicates the electrical conductivity. The hardness is adjusted by adjusting the electrical conductivity of the controller (Electric conductivity indicating switch) and then sent to the container filling process.

When the concentration of boron in water is low and the boron concentration in the filtrate filtered in the reverse osmosis filtration process is adjusted to 0.3 mg / l or less, which is the standard of drinking water, without adjusting the pH to 9-11 in the pH adjustment step, reverse osmosis When the pH of the filtrate filtered in the administration and processing reaches 8.5 or less (range of 5.8 to 8.5), the step of supplying acid to the filtrate filtered in the reverse osmosis filtering step and neutralizing is omitted.

Hardness is converted into calcium carbonate (CaCO ₃ ) in the concentration of calcium ions (Ca ²⁺ ) and magnesium ions (Mg ²⁺ ) in mg / l or ppm as expressed by the following formula (18). Also called total hardness.

Hardness (mg / L) = [calcium ion concentration (mg / L) x 2.5] + [magnesium ion concentration (mg / L) x 4.1]. … … … … … … … … … … … … … … … … … … … … … … … … … … … … … … (18)

Water taste is not good even if the hardness is higher than 300mg / ℓ, whereas water taste is not good even if the hardness is less than 10mg / ℓ, water in the hardness range of 30 ~ 100mg / ℓ can be a good drink have. However, in the case of fermented water, water of 1,000 mg / l or more is used.

In water, magnesium ions (Ca ²⁺ ) have a bitter taste, potassium ions (K ⁺ ) have a sour taste, sulfate ions (SO ₄ ^2- ) have an acid taste, and NaCl has a salty taste that reduces the taste of water. On the other hand, calcium ions (Ca ²⁺ ) has the characteristic of softening the taste of water to improve the taste of water.

Drinking water should have a hardness in the range of 30 to 300 mg / l, with a good water index (OI) of 2.0 or higher and a healthy index (KI) of 5.2 or higher.

Index of good taste (OI) = (Ca + K + SiO ₂ ) / (Mg + SO ₄ ²⁻ ). … … … … (19)

Index of health (KI) = Ca-0.87 Na... … … … … … … … … … … … … … … … (20)

Considering the water taste index and the health index, the hardness modifier is preferably a low concentration of sulfate ion (SO ₄ ^2- ) with a Ca / Mg weight ratio of 2.0 or more, but as shown in Table 1 When Ca / Mg weight ratio is 0.35 and magnesium content is much higher than calcium and NaCl and sulfate ion concentrations are high, the depth of Ca / Mg weight ratio and the adjustment of Ca / Mg weight and sulfate ion and NaCl are used. It is preferable to make mineral salts removed as much as possible and use it as hardness modifier.

The hardness modifier (also referred to as a mineral modifier) is commercially available, and the hardness modifier is commercially available in the deep sea water, calcium sulfate (CaSO ₄ ) to Ca / Mg weight ratio of 2 to 6 minerals After adjusting the balance, trehalose, ascorbic acid, lactic acid or gluconic acid in mineral water from which salinity (NaCl) and sulfate ion (SO ₄ ^2- ) were removed by electrodialysis. (Gluconic acid) is a mixture of organic additives alone or mixed in two or more kinds in the range of 5 to 20wt%, the calcium mineral is supplied to the hardness adjuster prepared in the form of organic mineral salts, and the deep water of the sea, the Ca / Mg weight ratio of 2 to 6 After adjusting the mineral balance to the range, the hardness modifier to remove the salt (NaCl) and sulfate ions (SO ₄ ^2- ) by electrodialysis, deep sea water salt (NaCl) by electrodialysis And sulfuric acid After the ions (SO ₄ ^2- ) are removed and selected, there is a hardness modifier to which trehalose is added or a hardness modifier to remove the salt (NaCl) and sulfate ions (SO ₄ ^2- ) by electrodialysis.

The neutralization treatment and the hardness adjustment tank capacity were set to 20 to 30 minutes, and stirred with a propeller stirrer of 180 to 360 rpm (rotational speed).

2. Container filling, packaging and inspection process

In the neutralization and hardness adjustment process, the water (beverage) adjusted to the neutralization treatment and hardness is stored in a beverage storage tank, filled into a container (can or plastic bottle) in a container filling process, and then inspected and packaged into a beverage product. Ship it.

The beverage storage tank has a sealed structure, and when air circulation is required, an air filter and a sterilization facility are installed. The filling room to fill the container is a clean room, and UV air sterilization equipment is installed. The laboratory shall be installed in isolation from the manufacturing facility and shall have legally necessary equipment, water supply and ventilation for inspection.

[Example 3]

The reverse osmosis filtration process prepared the reverse osmosis filtration apparatus which consists of a spiral reverse osmosis filtration membrane of 36 m <2> of filtration area of Toray Corporation Co., Ltd. low pressure reverse osmosis membrane model number SU-710.

Injecting a caustic soda solution in the primary demineralized water sterilized in Example 2 to adjust the pH to 9.5 to convert the boron compound in the form of polyboric acid, and then skip the nanofiltration process in a short time, the reverse osmosis When the flow rate was 1.5 m3 / hour and the supply pressure was 25 kg / cm2G, the discharge volume of unfiltered and concentrated brine was 0.14 m3 / hour. Filtrate discharge was 1.36m3 / hour, recovery was about 90%, and the analysis of the major components contained in the secondary demineralized water was shown in Table 4 below.

Table 4 Analysis of Significant Values in Secondary Demineralized Water

Item Analytical value Item Quarry Na (mg / L) 38.7 Cl (mg / L) 71.6 K (mg / L) 1.3 Br (mg / L) 0.5 Ca (mg / L) 0.6 SO ₄ ^2- (mg / L) 1.2 Mg (mg / L) 1.9 pH 7.8 B (mg / L) 0.12 Viable count (dog / ml) Not detected Hardness (CaCO ₃ as mg / ℓ) 9.29 - -

As shown in Table 4, the secondary demineralized water was treated with a boron compound at a drinking water standard value of 0.3 mg / l or less, a chlorine ion temperature drinking water standard value of 250 mg / l or less, and a hardness degree of drinking water standard value of 300 mg / l or less. Also within the range of the beverage standard value of 5.8 to 8.5, it can be seen that the remaining items were also treated according to the beverage standard value, such that no viable cell count was detected.

Therefore, in the reverse osmosis filtration process of Example 3, the secondary demineralized water may be confirmed to be packaged and produced as a beverage after adjusting the hardness required as a mineral regulator.

1 is a process chart for producing beverages from deep sea or surface seawater

2 is an explanatory view of a primary desalination mechanism by an electroextraction process

3 is a sterilization treatment process diagram

1: Seawater Storage Tank 2: Seawater Transfer Pump

3: salt extraction chamber 4: desalting chamber

5: anode 6: cathode

7: anion exchange membrane 8: cation exchange membrane

9: diaphragm supporter 10: air blower

11: diffuser 12: primary demineralized water reservoir

13: 1st demineralized water transfer pump 14: magnetization apparatus

15: AC high voltage generator 15a: variable resistor

15b: Primary winding 15c: Core

15d: secondary winding 15e: output terminal

15f: Insulation terminal 15g: Earth

16: Sterilization tank 17: High voltage application electrode

18: ground electrode 19: ground

N: N pole of magnet S: S pole of magnet

Ⓢ: Solenoid Valve

BIS: Baume's hydrometer indicating switch

ECIS: Electric conductivity indicating switch

Claims

In the production of beverages from deep sea or surface sea water,

A pretreatment step of acquiring the deep seawater or surface seawater, and obtaining at least one kind of pretreatment filtration from warming treatment, adsorption process of organic matter and sand filtration, microfiltration or ultrafilter,

When the pre-filtered seawater is supplied to the seawater storage tank (1), between the positive electrode (5) and the negative electrode (6) installed in the salt extraction chamber (3), the negative electrode (6) side is a positive ion exchange membrane (8), the positive electrode (5) The seawater of the seawater storage tank (1) is a seawater transfer pump (2) in the primary desalination process by electric extraction consisting of anion exchange membrane (7) and an isolated desalination chamber (4). Is supplied to the salt extraction chamber 3 and the desalination chamber 4, to the desalination chamber 4, and aerated air from the air blower 10 through the diffuser 11, and direct current from the rectifier. The cation contained in the seawater of the desalting chamber 4 by applying electricity passes through the cation exchange diaphragm 8 on the negative electrode 6 side and moves to the salt extraction chamber 3, and the anion is the positive electrode 5 In the salt extraction chamber 3, the concentrated brine is discharged, and the desalting chamber 4 is contained in the sea water as it moves to the salt extraction chamber 3 through the anion exchange diaphragm 7 of the side). And primary desalting step for obtaining a primary desalinated water the salinity primary desalting,

The primary demineralized water is magnetized by one type of magnetizer, either a solenoid type magnetizer or a magnetizer provided with permanent magnets, and then a high voltage is applied to the sterilization tank 16 to apply an AC high voltage. The alternating current is applied to the high voltage applying electrode 17 of the sterilization process by an alternating current high voltage in which the applying electrode 17 and the ground electrode 18 connected to the ground 19 on the ground are installed alternately. A sterilization step of sterilizing while applying an AC high voltage from the output terminal 15e of the high voltage generator 15 to obtain sterilization water;

Secondary desalination treatment in which the sterilized water was sent to the pH adjusting step, and the pH 9 to 11 was sent to the nano filtration step, and the filtered filtrate was sent to the reverse osmosis filtration step to filter and demineralize the salts contained in the water to obtain secondary demineralized water. Steps,

The secondary demineralized water is sent to the neutralization treatment and hardness adjustment process to neutralize the pH in the range of 5.8 to 8.5, which is the standard for drinking water, while supplying a mineral modifier to adjust the hardness, filling the container, inspecting and packing the beverage Method for producing a beverage from deep sea water or superficial sea water, characterized in that consisting of the steps of producing.

The method of claim 1, wherein the sterilized water is sent to a nanofiltration process, the filtered filtrate is supplied to a reverse osmosis filtration process to supply a mineral modifier to the filtered secondary demineralized water to adjust the hardness, and then filled into a container, and then packed after inspection. To produce beverages from deep ocean or surface seawater producing beverages.

The method of claim 1, wherein the sterilized water is supplied to a reverse osmosis filtration process to supply a mineral modifier to the filtered secondary demineralized water to adjust the hardness, filling the container, filling the container, packaging after inspection to produce a drinking water Process for producing beverages from deep or superficial seawater.

The sterilized water was sent to the pH adjusting process, and the pH 9-11 was adjusted to the reverse osmosis filtration process, and the second demineralized water obtained by filtering the salt in the reverse osmosis filtration was sent to the neutralization treatment and the hardness adjustment process, and the pH was adjusted to the drinking water standard value of 5.8 to A method of producing beverages from deep sea or superficial seawater which neutralizes in the range of 8.5, adjusts the hardness by supplying mineral modifiers, fills them into containers, inspects and packages them to produce beverages.