CN109205944A - A kind of pharmacy waste water divides salt processing method - Google Patents
A kind of pharmacy waste water divides salt processing method Download PDFInfo
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F2103/02—Non-contaminated water, e.g. for industrial water supply
- C02F2103/026—Treating water for medical or cosmetic purposes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
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- Y02A20/131—Reverse-osmosis
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Abstract
Divide salt processing method the present invention provides a kind of pharmacy waste water.Its basic step includes: that pharmacy waste water enters V-type filter tank except SS, the water outlet of V-type filter tank enters the desalination and concentration decrement that level-one DTL counter-infiltration system carries out the first step, level-one DTL reverse osmosis concentrated water is after chemical tendering removes firmly, the concentration decrement of second step is carried out, into second level DTL counter-infiltration system to meet the requirement of the system rate of recovery.The concentrated water of second level DTL counter-infiltration system enters DTNF and realizes NaCl and Na2SO4Separation, the production water of DTNF enters DTRO system and carries out NaCl concentration, final to realize the concentration and separation for carrying out monovalent salt and divalent salts.This method realizes the harmless recycling of resource, while solving the problems, such as that evaporation and crystallization system crystallization is difficult, inferior.
Description
Technical field
The present invention relates to technical field of waste water processing, and in particular to a kind of pharmacy waste water divides salt processing method.
Background technique
For most industries, since the salinity in waste water is complex, only come by simple single vaporization final
Want to realize that " zero solid waste " outlet is very difficult.If not carrying out a point salt treatment, finally obtained solid carnallite base to waste water
This can all be disposed as solid dangerous waste (abbreviation solid dangerous waste).And the cost of current domestic processing solid dangerous waste is basic
At 3000 yuan/ton or more, cost is even concentrated than leading portion film, is concentrated by evaporation, each workshop section's cost summation of evaporative crystallization is taller.
Therefore, in the design of entire high slat-containing wastewater treatment process, if it is possible to it is sold final solid product as product, and
It is handled not as solid dangerous waste, will have very big application value.
To realize waste water salinity resource utilization, current most effective measure carries out a point salt treatment to high-salt wastewater.Institute
Meaning divides salt treatment, that is, utilizes phase diagram theory, and different according to solute solubility each under same temperature in solution carry out salinity separation,
To obtain the process of different product salts.Existing point of salt treatment process is generally thermal method and salt and cold process is divided to be divided to two kinds of salt.Thermal method point
Salt technique is answered in the fields such as " potassium sodium separation (potassium chloride and sodium chloride) ", " salt lake chemical industry solventing-out (sodium chloride and sodium sulphate) "
With the most extensively；Cold process divides salt in " denitration of chemical industry for making chlorine and alkali electrolytic chlorination sodium solution ", " AC foaming agent producing process sodium carbonate is de-
Except " and the fields such as some reaction solutions purification using more.Some certain production procedures not only can divide salt using thermal method, but also can adopt
Divide salt such as " solventing-out " with cold process.
Biochemical pharmaceutical wastewater is high with content of microorganisms, COD is higher, suspension content is high, hardness is high and salt content is higher
Etc. main features.Therefore, it is necessary to which comprehensive actual conditions cautiously select treatment process, to reach optimum efficiency.
In consideration of it, the present invention is specifically proposed.
Summary of the invention
Divide salt processing method the purpose of the present invention is to provide a kind of pharmacy waste water.
To achieve the above object, technical scheme is as follows:
Divide salt processing method the present invention relates to a kind of pharmacy waste water, comprising the following steps:
(1) biochemical treatment and sterilization processing are successively carried out to pharmacy waste water, then waste water introduces V-type filter tank by treated
It is filtered, removes the suspended matter in waste water；
Preferably, the sterilization processing is that NaClO is added into the waste water after the biochemical treatment.
(2) V-type filter tank is produced into water and introduces filter tank production pond, carried out sedimentation in the production pond of the filter tank and pH value is adjusted；
The water outlet that filter tank produces pond enters level-one DTL counter-infiltration system and carries out level-one desalination and concentration；Level-one DTL counter-infiltration system goes out
Water includes concentrated water and production water；
Preferably, the filter tank produces turbidity≤10NTU of water body in pond.
Preferably, it is produced in pond to the filter tank and sequentially adds NaHSO3And H2SO4, the pH value of the waste water is adjusted to
Then the water outlet that filter tank produces pond is introduced level-one DTL counter-infiltration system by 6.0-7.0.
(3) concentrated water of level-one DTL counter-infiltration system is introduced into highly dense cell system and carries out sofening treatment；Level-one DTL is reverse osmosis
The production water of system introduces intermediate pool；
Preferably, the sofening treatment uses liquid alkaline method, and the reagent of use includes liquid alkaline, PAC and PAM.
Preferably, highly dense pond produces water turbidity≤10NTU, total hardness≤100mg/L.
(4) highly dense pond is produced water introducing sand filter to be filtered, enters sand filtration production pond after removing suspended matter, in the sand
Filter, which produces, carries out sedimentation and pH value adjusting in pond；It is dense that the water outlet that sand filtration produces pond enters second level DTL counter-infiltration system progress second level
Reduction, the water outlet of second level DTL counter-infiltration system include concentrated water and production water；
Preferably, sand filtration produces turbidity of wastewater≤10NTU in pond.
Preferably, it is produced in pond to the sand filtration and H is added2SO4, the pH value of the waste water is adjusted to 6.0-7.0, then will
The water outlet that sand filtration produces pond introduces second level DTL counter-infiltration system.
Preferably, the production water of second level DTL counter-infiltration system is introduced into intermediate pool, the production with level-one DTL counter-infiltration system
Water mixes, and obtains recycle-water after desalting processing.
(5) concentrated water of second level DTL counter-infiltration system enters the nanofiltration of dish tubular type (DTNF) system, carries out a point salt treatment；DTNF
The water outlet of system includes concentrated water and produces water, enters divalent salts evaporated crystallization device after concentrated water purification；
Preferably, DTNF diaphragm uses nanofiltration membrane, operating pressure≤90bar.
Preferably, after the purified processing evaporative crystallization of DTNF concentrated water, obtained divalent salts are Na2SO4, purity >=92%.
(6) the production water of DTNF enters water disc tube reverse osmosis (dt-ro) (DTRO) system of production, carries out concentration；DTRO system goes out
Water includes concentrated water and produces water, enters monovalent salt evaporated crystallization device after concentrated water purification；It produces water and introduces intermediate pool progress reuse.
Preferably, DTRO diaphragm uses seawater film, and operating pressure is 70~80bar.
Preferably, after the purified processing evaporative crystallization of DTRO concentrated water, obtained monovalent salt is NaCl, purity >=98.8.
Beneficial effects of the present invention:
Divide salt processing method the present invention provides a kind of pharmacy waste water, for realizing the recycling of salt in waste water.Its base
This step includes: that pharmacy waste water enters V-type filter tank except SS, and the water outlet of V-type filter tank enters level-one DTL counter-infiltration system and carries out the first step
Desalination and concentration decrement, level-one DTL reverse osmosis concentrated water by chemical tendering except after hard, into second level DTL counter-infiltration system
The concentration decrement of second step is carried out, to meet the requirement of the system rate of recovery.The concentrated water of second level DTL counter-infiltration system enters DTNF reality
Existing NaCl and Na2SO4Separation, the production water of DTNF enters DTRO system and carries out NaCl concentration, and final realize carries out monovalent salt and two
The concentration and separation of valence salt.This method realizes the harmless recycling of resource, while solving evaporation and crystallization system and crystallizing difficult, inferior ask
Topic.
Detailed description of the invention
Fig. 1 is the process flow chart that the pharmacy waste water divides salt processing method.
Specific embodiment
To make the object, technical solutions and advantages of the present invention clearer, technical solution of the present invention will be carried out below
Detailed description.Obviously, described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Base
Embodiment in the present invention, those of ordinary skill in the art are obtained all without making creative work
Other embodiment belongs to the range that the present invention is protected.
Divide salt processing method the present invention relates to a kind of pharmacy waste water, comprising the following steps:
(1) biochemical treatment and sterilization processing are successively carried out to pharmacy waste water, then waste water introduces V-type filter tank by treated
It is filtered, removes the suspended matter in waste water.
Wherein, biochemical treatment is the metabolism using microorganism, makes organic dirt in waste water in dissolution and colloidal state
Dye object is converted into innocuous substance, the method to realize purification.Aerobe facture and Anaerobic biotreatment method can be divided into.
In one embodiment of the invention, sterilization processing is that NaClO is added into the waste water after biochemical treatment, makes waste water
In the miscellaneous bacterias such as mould, bacterium and actinomyces content be reduced to it is micro.
V-type filter tank uses constant water level filtering, and ultrasonic level gage automatically controls adjustable solution and is discharged purge valve in pond, and valve can
Opening degree is automatically adjusted according to the height of pool inner water position, to guarantee the constant level in pond.Using homogeneous filtering material, filter area
Greatly, mixing wastewater with air backwashes.Its high degree of automation, control system are mature.
(2) V-type filter tank is produced into water and introduces filter tank production pond, carried out sedimentation in the production pond of filter tank and pH value is adjusted；Filter tank
The water outlet for producing pond enters level-one DTL counter-infiltration system and carries out level-one desalination and concentration；The water outlet packet of level-one DTL counter-infiltration system
It includes concentrated water and produces water.
In one embodiment of the invention, filter tank produces turbidity≤10NTU of water body in pond.
In one embodiment of the invention, it is produced in pond to filter tank and NaHSO is added3, with excessive in reductive water
NaClO reduces the oxidisability of waste water, shown in the chemical equation such as formula (1) of the two reaction:
2NaHSO3+ 2NaClO=Na2SO4+2NaCl+2H2O(1)
Since the pH value of biochemical water is in 8.0-9.0 or so, is next produced in pond to filter tank and H is added2SO4, will wherein give up
The pH value of water is adjusted to 6.0-7.0, then introduces level-one DTL counter-infiltration system.The water outlet of level-one DTL counter-infiltration system is divided into two
Point, permeate (referred to as production water) is discharged into intermediate pool, and concentrate (referred to as concentrated water) is discharged into highly dense cell system and carries out in next step
Processing.
(3) concentrated water of level-one DTL counter-infiltration system is introduced into highly dense cell system and carries out sofening treatment；Level-one DTL is reverse osmosis
The production water of system introduces intermediate pool.
Highly dense cell system full name potassium permanganate composites system is after horizontal sedimentation tank, and inclined plate (pipe) sedimentation basin and machinery add
A kind of New clarifier after fast (pulse) clarifying basin, by dosing, coagulation, flocculation, precipitating and sludge condensation function set in
One.It is divided into mixed zone, flocculation zone, settling zone and pH regulation area.Quick mixer is set in mixed zone, makes the coagulation added
Agent and liquid alkaline rapid dispersion make slightly solubility substance flocculate to form the flocculent deposit of macromolecular, realize mud-water separation.Water outlet is through pH value
Enter next stage processing unit after adjusting.
In one embodiment of the invention, sofening treatment uses liquid alkaline method, i.e., is gone using liquid alkaline remaining temporary in water removal
When hardness and part magnesium hardness.Reagent includes liquid alkaline, PAC and PAM.
Wherein, liquid alkaline is the sodium hydroxide of liquid state.For existing chlor-alkali plant due to the difference of production technology, the concentration of liquid alkaline is logical
Often it is 30%-32% or 40%-42%, the pH of waste water in highly dense cell system is adjusted to 11.0 or so using liquid alkaline.
PAM is polyacrylamide, and PAC is aluminium polychloride.Both it can make sewage or dirt by itself or hydrolysate
Colloid in mud quickly forms precipitating.The present invention makes the settling of floccus in water by adding PAC and PAM.Finally produce highly dense pond
Water turbidity≤10NTU, total hardness≤100mg/L.
(4) highly dense pond is produced water introducing sand filter to be filtered, enters sand filtration production pond after removing suspended matter, is produced in sand filtration
Sedimentation is carried out in pond and pH value is adjusted；The water outlet that sand filtration produces pond enters second level DTL counter-infiltration system progress secondary concentration and subtracts
Amount, the water outlet of second level DTL counter-infiltration system include concentrated water and production water.
Sand filter entitled shallow media filter (Shallow medium filter) entirely is a kind of to utilize filter medium
Go water removal in various suspended matters, microorganism and other subparticles, be finally reached reduce water turbidity, purify water effect
A kind of High-cfficiency Filtration equipment.Common filtrate has quartz sand, activated carbon, anthracite, manganese sand etc..It is handled in the present invention using sand filter
The water outlet in highly dense pond reduces the suspended matter in water, to meet the subsequent water inlet requirement into second level DTL counter-infiltration system, reduces
The blocking of core filter.
In one embodiment of the invention, handled by sand filter, into sand filtration produce pond in turbidity of wastewater≤
10NTU。
After waste water enters sand filtration production pond, is produced in pond to sand filtration and H is added2SO4, the pH value of waste water is adjusted to 6.0-7.0,
Then the water outlet that sand filtration produces pond is introduced into second level DTL counter-infiltration system.Similar with level-one DTL counter-infiltration system, second level DTL is anti-
The water outlet of osmosis system is also classified into permeate (referred to as production water) and concentrate (referred to as concentrated water) two parts.
In one embodiment of the invention, the production water of second level DTL counter-infiltration system is introduced into intermediate pool, with level-one
The production water of DTL counter-infiltration system mixes, and recycle-water is obtained after desalting processing.
(5) concentrated water of second level DTL counter-infiltration system enters the nanofiltration of dish tubular type (DTNF) system, carries out a point salt treatment；DTNF
The water outlet of system includes concentrated water and produces water, enters divalent salts evaporated crystallization device after concentrated water purification.
In one embodiment of the invention, DTNF system uses dish tubular nanofiltration membrane technology to divide salt technique for core.
Consider variation of water, DTNF is set as can achieve 90bar pressure rating membranous system.It mainly utilizes the spy of nanofiltration membrane
Property, most of organic matter and divalent salts (predominantly sulfate) are trapped in concentrate end, and to monovalent salt (predominantly chlorination
Sodium) there is permeability, monovalent salt and divalent salts can be effectively separated in this way.
After the purified processing evaporative crystallization of DTNF isolated concentrated water, obtained divalent salts are mainly Na2SO4, purity
>=92%.
(6) the production water of DTNF enters water disc tube reverse osmosis (dt-ro) (DTRO) system of production, carries out concentration；DTRO system goes out
Water includes concentrated water and produces water, enters monovalent salt evaporated crystallization device after concentrated water purification；It produces water and introduces intermediate pool progress reuse.
In one embodiment of the invention, DTRO system is strong using contamination resistance, high voltage bearing dish tubular type membrane technology.
DTRO diaphragm uses the operating pressure form membrane of 90bar, and operating pressure is 70~80bar, salt content can be concentrated and be improved
To 60000mg/L or more, again into evaporation and crystallization system after concentrate purification.
After the purified processing evaporative crystallization of DTRO isolated concentrated water, obtained monovalent salt is mainly NaCl, purity
≥98.8。
Embodiment
By taking certain company's Treated sewage reusing construction-operation-transfer (BOT) project as an example, the day yield of the said firm's pharmacy waste water
For 12000m3/d.Do not use present invention process technology before, by the said firm sewage disposal system directly to pharmacy waste water into
Row processing, obtained former bio-chemical effluent are directly entered mechanical steam recompression system (abbreviation MVR) and are evaporated crystallization.Due to
COD in waste water is higher, suspension content is high, hardness is high, so that MVR needs frequent clean, MVR whole system is caused to handle energy
The 80% of designed capacity is not achieved in power, and energy consumption is high.
After present invention process, membranous system concentrate enters divide salt system after pretreatment, realizes NaCl in waste water
And Na2SO4Concentration and separation, provide a kind of possibility to further realize resource reclaim harmless treatment, while solving evaporation
Crystal system crystallization is difficult, inferior problem.
As shown in Figure 1, pharmacy waste water provided by the invention divide salt processing method the following steps are included:
(1) after carrying out biochemical treatment to pharmacy waste water, NaClO is added and carries out sterilization processing, obtains biochemical water.Biochemistry comes
Water is introduced into collecting-tank, squeezes into V-type filter tank by elevator pump and is filtered, removes the suspended matter in water.V-type filter tank is due to filter
The bed of material is thicker, and dirt-carrying amount is big, and the delivery turbidity of water after filter is generally less than 10.0NTU.V-type filter tank needs periodically to carry out air water anti-
It washes, backwash water drains into biochemical system.
(2) V-type filter tank produced into water introduce filter tank and produce pond, produce in pond and settled in filter tank, make the turbidity of water body≤
10NTU.Then NaHSO is added3And H2SO4, the pH value of waste water is adjusted to 6.0-7.0.The water outlet that filter tank produces pond enters level-one
DTL counter-infiltration system carries out level-one desalination and concentration.Level-one DTL counter-infiltration system uses bitter film, and operation maximum pressure is
The rate of recovery of level-one DTL counter-infiltration system is designed as 80% by 75bar.The water outlet of level-one DTL counter-infiltration system is divided into two
Point, permeate (referred to as production water) is discharged into intermediate pool, and concentrate (referred to as concentrated water) is discharged into highly dense cell system and carries out in next step
Processing.
In certain operating condition, the influent COD of level-one DTL counter-infiltration system is 626mg/L, and production water COD is 23mg/L, removal rate
97%.
(3) since after the processing of level-one DTL counter-infiltration system, the salt content in concentrated water is 4-5 times of biochemical water,
Therefore the scale-forming ion concentration in concentrated water is very high.Need to introduce the concentrated water of level-one DTL counter-infiltration system highly dense cell system into
Row sofening treatment, subsequently into the processing of second level DTL counter-infiltration system.The production water of level-one DTL counter-infiltration system introduces intermediate pool.
Sofening treatment carries out in highly dense cell system, using liquid alkaline method.Softening be added medicament be mainly liquid alkaline, PAC and
PAM, softening water outlet enter softening and produce pond.Softening sludge removes sludge-tank, and the mud cake and biochemistry generated by sludge dewatering system is dirty
Mud is disposed together, and filter press filtrate again returns to chemical tendering system.
In certain operating condition, before sofening treatment, the total hardness of level-one DTL counter-infiltration system concentrated water is 1256.3mg/L, softening
Total hardness that treated is 90.1mg/L.
(4) highly dense pond is produced into water, i.e. H is used in softening water outlet2SO4After pH value is adjusted to 6.0-7.0, carried out into sand filter
Filter enters sand filtration production pond after removing SS.Sand filtration produces pond by the way of air water backwash, and anti-scouring water is that sand filtration produces water, instead
It washes and drains back biochemical system.Sand filtration produce pond water outlet by promoted be pumped into second level DTL counter-infiltration system carry out secondary concentration subtract
Amount.Second level DTL counter-infiltration system uses seawater film, and operation maximum pressure is 90bar.
The water outlet of second level DTL counter-infiltration system includes concentrated water and production water.During the production water of second level DTL counter-infiltration system is introduced into
Between pond, mixed with the production water of level-one DTL counter-infiltration system, recycle-water obtained after desalting processing.
(5) concentrated water of second level DTL counter-infiltration system enters the nanofiltration of dish tubular type (DTNF) system, carries out a point salt treatment；DTNF
The water outlet of system includes concentrated water and produces water, enters divalent salts evaporated crystallization device after concentrated water purification.DTNF diaphragm uses nanofiltration membrane
Form, operating pressure≤90bar.
In certain operating condition, after the purified processing evaporative crystallization of DTNF concentrated water, the obtained Na in divalent salts2SO4Purity >=
92%.
(6) the production water of DTNF enters water disc tube reverse osmosis (dt-ro) (DTRO) system of production, carries out concentration；DTRO system goes out
Water includes concentrated water and produces water, enters monovalent salt evaporated crystallization device after concentrated water purification；It produces water and introduces intermediate pool progress reuse.
DTRO diaphragm uses operating pressure form membrane, and operating pressure is 70~80bar.
In certain operating condition, after the purified processing evaporative crystallization of DTRO concentrated water, the obtained NaCl purity in monovalent salt >=
98.8。
Wherein, table 1 is the Inlet and outlet water water analysis data of DTNF under certain operating condition.Table 2 be certain operating condition under DTNF and
The operation data of DTRO system.
Table 1
| Sample is other | TDS/% | Cl-Concentration (mg/L) | SO4 2-Concentration (mg/L) | COD concentration (mg/L) |
| DTNF water inlet | 5.47 | 7351.46 | 25799.73 | 5870 |
| DTNF produces water | 2.2 | 8037.36 | 105.77 | 2272.5 |
| DTNF concentrated water | 10.47 | 5543.5 | 70762.68 | 10724 |
Table 2
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (10)
1. a kind of pharmacy waste water divides salt processing method, which comprises the following steps:
(1) biochemical treatment and sterilization processing are successively carried out to pharmacy waste water, then waste water introduces the progress of V-type filter tank by treated
Filtering removes the suspended matter in waste water；
(2) V-type filter tank is produced into water and introduces filter tank production pond, carried out sedimentation in the production pond of the filter tank and pH value is adjusted；Filter tank
The water outlet for producing pond enters level-one DTL counter-infiltration system and carries out level-one desalination and concentration；The water outlet packet of level-one DTL counter-infiltration system
It includes concentrated water and produces water；
(3) concentrated water of level-one DTL counter-infiltration system is introduced into highly dense cell system and carries out sofening treatment；Level-one DTL counter-infiltration system
Production water introduce intermediate pool；
(4) highly dense pond is produced water introducing sand filter to be filtered, enters sand filtration production pond after removing suspended matter, is produced in the sand filtration
Sedimentation is carried out in pond and pH value is adjusted；The water outlet that sand filtration produces pond enters second level DTL counter-infiltration system progress secondary concentration and subtracts
Amount, the water outlet of second level DTL counter-infiltration system include concentrated water and production water；
(5) concentrated water of second level DTL counter-infiltration system enters DTNF system, carries out a point salt treatment；The water outlet of DTNF system includes dense
Water and production water, enter divalent salts evaporated crystallization device after concentrated water purification；
(6) the production water of DTNF enters DTRO system, carries out concentration；The water outlet of DTRO system includes concentrated water and production water, concentrated water
Enter monovalent salt evaporated crystallization device after purification；It produces water and introduces intermediate pool progress reuse.
2. the method according to claim 1, wherein the sterilization processing is at the biochemistry in step (1)
NaClO is added in waste water after reason.
3. the method according to claim 1, wherein producing in pond and sequentially adding to the filter tank in step (2)
NaHSO3And H2SO4, the pH value of the waste water is adjusted to 6.0-7.0, it is anti-that the water outlet that filter tank produces pond is then introduced level-one DTL
Osmosis system.
4. being adopted the method according to claim 1, wherein the sofening treatment uses liquid alkaline method in step (3)
Reagent includes liquid alkaline, PAC and PAM.
5. the method according to claim 1, wherein highly dense pond produces water turbidity≤10NTU, total hard in step (3)
Degree≤100mg/L.
6. the method according to claim 1, wherein producing in pond and being added to the sand filtration in step (4)
H2SO4, the pH value of the waste water is adjusted to 6.0-7.0, the water outlet that sand filtration produces pond is then introduced into second level DTL counter-infiltration system.
7. the method according to claim 1, wherein DTNF diaphragm uses nanofiltration membrane, operation in step (5)
Pressure≤90bar.
8. the method according to claim 1, wherein in step (5), the purified processing evaporative crystallization of DTNF concentrated water
Afterwards, the divalent salts obtained are Na2SO4, purity >=92%.
9. the method according to claim 1, wherein DTRO diaphragm uses seawater film, operation in step (6)
Pressure is 70~80bar.
10. the method according to claim 1, wherein the purified processing evaporation of DTRO concentrated water is tied in step (6)
After crystalline substance, obtained monovalent salt is NaCl, purity >=98.8.
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