JP2018158300A - Water treatment system and work medium - Google Patents
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- JP2018158300A JP2018158300A JP2017057002A JP2017057002A JP2018158300A JP 2018158300 A JP2018158300 A JP 2018158300A JP 2017057002 A JP2017057002 A JP 2017057002A JP 2017057002 A JP2017057002 A JP 2017057002A JP 2018158300 A JP2018158300 A JP 2018158300A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 216
- 238000011282 treatment Methods 0.000 title claims abstract description 49
- 239000012528 membrane Substances 0.000 claims abstract description 96
- 230000003204 osmotic effect Effects 0.000 claims abstract description 91
- 150000001875 compounds Chemical class 0.000 claims abstract description 53
- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphonic acid group Chemical class P(O)(O)=O ABLZXFCXXLZCGV-UHFFFAOYSA-N 0.000 claims abstract description 50
- 150000003839 salts Chemical group 0.000 claims abstract description 48
- 229910052751 metal Inorganic materials 0.000 claims abstract description 34
- 239000002184 metal Substances 0.000 claims abstract description 34
- 150000003863 ammonium salts Chemical group 0.000 claims abstract description 28
- 239000007864 aqueous solution Substances 0.000 claims abstract description 11
- -1 etidronate sodium salt Chemical class 0.000 claims description 16
- 239000002253 acid Substances 0.000 claims description 10
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 claims description 10
- 229940120146 EDTMP Drugs 0.000 claims description 9
- 229940009626 etidronate Drugs 0.000 claims description 8
- 230000001939 inductive effect Effects 0.000 claims description 8
- 229940090960 diethylenetriamine pentamethylene phosphonic acid Drugs 0.000 claims description 7
- DBVJJBKOTRCVKF-UHFFFAOYSA-N Etidronic acid Chemical compound OP(=O)(O)C(O)(C)P(O)(O)=O DBVJJBKOTRCVKF-UHFFFAOYSA-N 0.000 claims description 5
- DUYCTCQXNHFCSJ-UHFFFAOYSA-N dtpmp Chemical compound OP(=O)(O)CN(CP(O)(O)=O)CCN(CP(O)(=O)O)CCN(CP(O)(O)=O)CP(O)(O)=O DUYCTCQXNHFCSJ-UHFFFAOYSA-N 0.000 claims description 4
- 159000000000 sodium salts Chemical class 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- 229910052783 alkali metal Inorganic materials 0.000 claims description 3
- NFDRPXJGHKJRLJ-UHFFFAOYSA-N edtmp Chemical compound OP(O)(=O)CN(CP(O)(O)=O)CCN(CP(O)(O)=O)CP(O)(O)=O NFDRPXJGHKJRLJ-UHFFFAOYSA-N 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 238000000638 solvent extraction Methods 0.000 claims description 3
- 150000001340 alkali metals Chemical class 0.000 claims description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 2
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 2
- 230000005611 electricity Effects 0.000 claims 1
- 230000006698 induction Effects 0.000 claims 1
- 239000000243 solution Substances 0.000 abstract description 18
- 235000002639 sodium chloride Nutrition 0.000 description 30
- 239000011550 stock solution Substances 0.000 description 21
- 238000004821 distillation Methods 0.000 description 19
- 238000010248 power generation Methods 0.000 description 16
- 238000010790 dilution Methods 0.000 description 15
- 239000012895 dilution Substances 0.000 description 15
- 238000001223 reverse osmosis Methods 0.000 description 14
- 239000013535 sea water Substances 0.000 description 14
- 230000018044 dehydration Effects 0.000 description 13
- 238000006297 dehydration reaction Methods 0.000 description 13
- 230000004907 flux Effects 0.000 description 10
- 238000010612 desalination reaction Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 238000011033 desalting Methods 0.000 description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 239000004816 latex Substances 0.000 description 5
- 229920000126 latex Polymers 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 239000010842 industrial wastewater Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000012466 permeate Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 238000009292 forward osmosis Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229910052700 potassium Inorganic materials 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 235000011132 calcium sulphate Nutrition 0.000 description 1
- 125000002843 carboxylic acid group Chemical group 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 235000013681 dietary sucrose Nutrition 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000004811 liquid chromatography Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 235000011147 magnesium chloride Nutrition 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229960004793 sucrose Drugs 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/005—Osmotic agents; Draw solutions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0022—Apparatus therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
- F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
- F03G7/00—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
実施形態は、水処理システム及び作業媒体に関する。 Embodiments relate to a water treatment system and a working medium.
溶質濃度の低い溶液と高い溶液とを浸透膜で隔離すると、低い濃度の溶液の溶媒は浸透膜を透過して高い濃度の溶液側に移動する。この溶媒が移動する現象を利用することにより、海水淡水化などの脱塩を行う脱塩システム、タービンを回して発電する浸透圧発電システムが知られている。また、これを利用した食品、汚泥を濃縮する濃縮システムも知られている。このとき濃度の高い側に使用されるのが作業媒体（ドロー溶液：Draw solution）で、これまで種々のものが提案されている。 When a solution having a low solute concentration and a solution having a high solute concentration are separated from each other by the osmosis membrane, the solvent of the solution having a low concentration passes through the osmosis membrane and moves to the solution side having a high concentration. There are known desalination systems that perform desalination such as seawater desalination by utilizing this phenomenon of solvent movement, and osmotic pressure power generation systems that generate power by turning a turbine. In addition, a concentration system that concentrates food and sludge using the same is also known. At this time, the working medium (Draw solution) is used on the higher concentration side, and various types have been proposed so far.
ドロー溶液の溶質は、一般に食塩が用いられている。有機塩もドロー溶液の溶質として用いられている。しかしながら、有機塩のドロー溶液は水の透過流束が食塩のドロー溶液に比べて劣っている。 As the solute of the draw solution, salt is generally used. Organic salts are also used as solutes in draw solutions. However, organic salt draw solutions have inferior water flux compared to salt draw solutions.
２種以上の溶質を混合したドロー溶液が提案されている。複数の無機塩の混合物は、相乗効果が観測されるが、無機塩とサッカロースの場合には逆効果で浸透膜を通過する流束が下がることもある。 A draw solution in which two or more solutes are mixed has been proposed. In the case of a mixture of a plurality of inorganic salts, a synergistic effect is observed, but in the case of inorganic salts and saccharose, the flux passing through the osmosis membrane may be reduced due to an adverse effect.
実施形態は、低コストで水を分離することができる水処理システム及び作業媒体を提供する。 Embodiments provide a water treatment system and a working medium that can separate water at low cost.
実施形態に係る水処理システムは、被処理水を収容する第１チャンバーと浸透圧を誘起する作業媒体を収容する第２チャンバーとを区画する浸透膜を備える第１処理容器を有し、作業媒体が主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物、又は、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物を溶質として含む水溶液である。 A water treatment system according to an embodiment includes a first treatment container including a permeable membrane that partitions a first chamber that contains water to be treated and a second chamber that contains a working medium that induces osmotic pressure, and the working medium Is a compound having an ammonium salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain, or a compound having a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain Is an aqueous solution containing as a solute.
以下、実施形態の水処理システムと水処理システムに使用される作業媒体を説明する。
（第１実施形態）
第１実施形態に係る水処理システムを図１に示す概略図を参照して説明する。図１に示す第１実施形態に係る水処理システム１００は、被処理水Ａを収容する第１チャンバー１３と作業媒体Ｂを収容する第２チャンバー１４とを区画する浸透膜１２を備える第１処理容器１１を有する浸透圧発生器１において、作業媒体Ｂが浸透圧を誘起する。
Hereinafter, the working medium used for the water treatment system and water treatment system of an embodiment is explained.
(First embodiment)
The water treatment system according to the first embodiment will be described with reference to the schematic diagram shown in FIG. A water treatment system 100 according to the first embodiment shown in FIG. 1 includes a permeable membrane 12 that partitions a first chamber 13 that contains water to be treated A and a second chamber 14 that contains a working medium B. In the osmotic pressure generator 1 having the container 11, the working medium B induces osmotic pressure.
このような水処理システム１００によれば、第１チャンバー１３内の被処理水Ａと第２チャンバー１４内の作業媒体Ｂとの間で生じる浸透圧差により第１チャンバー１３内の被処理水Ａ中の水Ｃが浸透膜１２を透過して第２チャンバー１４内の作業媒体Ｂに移動する。 According to such a water treatment system 100, in the water to be treated A in the first chamber 13 due to the osmotic pressure difference generated between the water to be treated A in the first chamber 13 and the working medium B in the second chamber 14. The water C passes through the osmotic membrane 12 and moves to the working medium B in the second chamber 14.
実施形態の作業媒体Ｂを用いることで、第１チャンバー１３内の被処理水Ａ中の水Ｃを大きな透過流束で浸透膜を透過して第２チャンバー１４内の作業媒体Ｂに移動させることが可能になる点で、実施形態の水処理システムは好ましい。実施形態の作業媒体Ｂは、低コストで運転することができる水処理システム、及び水処理システムに使用される。 By using the working medium B of the embodiment, the water C in the water to be treated A in the first chamber 13 is transferred to the working medium B in the second chamber 14 through the osmotic membrane with a large permeation flux. Therefore, the water treatment system of the embodiment is preferable. The working medium B of the embodiment is used in a water treatment system that can be operated at low cost, and a water treatment system.
第１処理容器１１は、浸透膜１２によって、第１チャンバー１３と第２チャンバー１４とに区画が隔てられている。第１処理容器１１は、第１チャンバー１３に被処理水Ａを収容し、第２チャンバー１４に作業媒体Ｂを収容する樹脂製又は金属製の容器である。 The first processing container 11 is partitioned by a permeable membrane 12 into a first chamber 13 and a second chamber 14. The first treatment container 11 is a resin or metal container in which the water to be treated A is accommodated in the first chamber 13 and the work medium B is accommodated in the second chamber 14.
浸透膜１２は、例えば正浸透膜（Forward Osmosis Membrane:ＦＯ膜）であっても逆浸透膜（Reverse Osmosis Membrane:ＲＯ膜）であってもよい。好ましい浸透膜は、ＦＯ膜である。 For example, the osmosis membrane 12 may be a forward osmosis membrane (FO membrane) or a reverse osmosis membrane (RO membrane). A preferred osmotic membrane is an FO membrane.
浸透膜１２は、例えば酢酸セルロース膜、ポリアミド膜などを用いることができる。浸透膜は、４５μｍ以上２５０μｍ以下の厚さを有することが好ましい。 As the osmotic membrane 12, for example, a cellulose acetate membrane, a polyamide membrane, or the like can be used. The permeable membrane preferably has a thickness of 45 μm or more and 250 μm or less.
第１チャンバー１３は、被処理水Ａを収容する第１処理容器１１内の領域であって、浸透膜１２によって区画が隔てられている。第１チャンバー１３には、被処理水Ａが導入排出される図示しない導入排出経路を設けてもよい。 The first chamber 13 is a region in the first processing container 11 that stores the water to be treated A, and is partitioned by the permeable membrane 12. The first chamber 13 may be provided with an introduction / discharge path (not shown) through which the treated water A is introduced / discharged.
被処理水Ａは、作業媒体よりも溶質濃度の低い液体である。被処理水Ａは、例えば塩水（海水等）、湖水、河川水、沼水、生活排水、産業廃水又はそれらの混合物を挙げることができる。被処理水Ａが塩水の場合、塩水の塩（塩化ナトリウム）濃度は例えば、０．０５％〜８％であればよい。被処理水Ａは、塩化ナトリウム、塩化マグネシウムや硫酸マグネシウム、硫酸カルシウム、塩化カリウムなどの塩や浮遊物質を含み、水以外のものが濃縮される。 The water to be treated A is a liquid having a lower solute concentration than the working medium. The treated water A can include, for example, salt water (seawater, etc.), lake water, river water, marsh water, domestic wastewater, industrial wastewater, or a mixture thereof. When the to-be-processed water A is salt water, the salt (sodium chloride) density | concentration of salt water should just be 0.05%-8%, for example. The water to be treated A contains salts such as sodium chloride, magnesium chloride, magnesium sulfate, calcium sulfate, potassium chloride, and suspended solids, and concentrates other than water.
第２チャンバー１４は、作業媒体Ｂを収容する第１処理容器１１内の領域であって、浸透膜１２によって区画が隔てられている。第２チャンバー１３には、作業媒体Ｂが導入排出される図示しない導入排出経路を設けてもよい。 The second chamber 14 is a region in the first processing container 11 that accommodates the working medium B, and is partitioned by the permeable membrane 12. The second chamber 13 may be provided with an introduction / discharge path (not shown) through which the work medium B is introduced / discharged.
第１実施形態の作業媒体Ｂは、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物、を有する化合物を溶質として含む水溶液である。作業媒体Ｂは、水溶液であるため、水を溶媒として含む。かかる溶質を含む作業媒１４は、高い浸透圧の誘起作用を示すため好ましい。このため、第１チャンバー１１内の被処理水Ａ中の水が浸透膜１５を透過して第２チャンバー１３内の作業媒体Ｂに移動する際、高い透過流束（Ｊｗ Ｌ／ｍ２ｈ）を発生させることができる。 The working medium B according to the first embodiment includes a main chain, a side chain, or a compound having a metal salt structure of a phosphonic acid group in the main chain and the side chain, a main chain, a side chain, or a phosphonic acid group in the main chain and the side chain. An aqueous solution containing a compound having an ammonium salt structure as a solute. Since the working medium B is an aqueous solution, it contains water as a solvent. The working medium 14 containing such a solute is preferable because it exhibits a high osmotic pressure inducing action. For this reason, when the water in the to-be-treated water A in the first chamber 11 permeates the osmotic membrane 15 and moves to the working medium B in the second chamber 13, a high permeation flux (Jw L / m 2 h). Can be generated.
したがって、実施形態では、被処理水Ａの脱塩、濃縮等の処理を効率的に実施し得る、低コストにて運転可能な水処理システムを提供できる。実施形態の水処理システムは、回転体をさらに有し、浸透圧の誘起によって、水流が生じ、水流によって回転体を回転させて発電する水処理システムとして利用することも好ましい。 Therefore, in the embodiment, it is possible to provide a water treatment system that can be operated at a low cost and can efficiently carry out treatments such as desalting and concentration of the water to be treated A. It is also preferable that the water treatment system of the embodiment further includes a rotating body, and a water flow is generated by inducing osmotic pressure, and the water treatment system generates power by rotating the rotating body by the water flow.
作業媒体Ｂに含まれる溶質は浸透膜を介して被処理水Ａ側に漏れ出す現象があり、この溶質の損失が被処理水Ａの水質低下を招き、さらには正浸透システムのランニングコストを上昇させる。かかる現象は、低分子量の溶質で起きやすい。高分子量の溶質では、浸透膜１２の逆透過が起きにくいが、水に対する溶解性が低いため、高分子量の作業媒体Ｂ中の濃度が低いため、高い透過流速を実現するのが難しい。 The solute contained in the working medium B leaks to the treated water A side through the osmosis membrane, and the loss of this solute causes the water quality of the treated water A to deteriorate, and further increases the running cost of the forward osmosis system. Let Such a phenomenon is likely to occur with low molecular weight solutes. With a high molecular weight solute, reverse permeation of the osmotic membrane 12 is unlikely to occur, but since the solubility in water is low, the concentration in the high molecular weight working medium B is low, so it is difficult to achieve a high permeation flow rate.
作業媒体Ｂに含まれる溶質の化合物には、複数のホスホン酸基（金属塩、アンモニウム塩）を含むと溶質逆透過流速（Ｊｓ ｍｍｏｌ／ｍ２ｈ）を小さくできることが分かった。これは、低分子の溶質であっても同様であり、複数のホスホン酸基（金属塩、アンモニウム塩）を含むことによって、溶質の損失が低減されるため好ましい。 It has been found that the solute reverse permeation flow rate (Js mmol / m 2 h) can be reduced when the solute compound contained in the working medium B contains a plurality of phosphonic acid groups (metal salt, ammonium salt). This is the same even for a low-molecular solute, and by including a plurality of phosphonic acid groups (metal salt, ammonium salt), loss of the solute is reduced, which is preferable.
実施形態の主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物と主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物（分子）は、ＣｘＨｙＰｚＯｗＮｒＣｌｓＢｒｔＭｕで表される。Ｍは、金属である。透過流速を高くするため、２≦ｘ≦９、８≦ｙ≦２８、１≦ｚ≦６、３≦ｗ≦１８、０≦ｒ≦３、０≦ｓ≦１、０≦ｔ≦１、２≦ｕ≦１０を満たすことが好ましい。また、溶質逆透過流速を小さくするため、２≦ｘ≦１５、８≦ｙ≦３５、２≦ｚ≦５、７≦ｗ≦１５、０≦ｒ≦５、０≦ｓ≦１、０≦ｔ≦１、２≦ｕ≦１０を満たすことが好ましい。そして、透過流速を高め、かつ、溶質逆透過流速を小さくするため、２≦ｘ≦９、８≦ｙ≦２８、２≦ｚ≦５、７≦ｗ≦１５、０≦ｒ≦３、０≦ｓ≦１、０≦ｔ≦１、２≦ｕ≦１０を満たすことが好ましい。Ｍで表される金属は、ホスホン酸の金属塩の金属である。金属塩の金属は、アルカリ金属又はアルカリ土類金属が好ましい。金属塩の金属は、Ｎａ，Ｋ、Ｃａ、ＡｌとＭｇからなる群のうちのいずれか１種以上が好ましい。実施形態の溶質に含まれる元素又は構造は、液体クロマトグラフィーで分析し、それぞれのピークの化合物を分離し、ＮＭＲ又は有機元素分析装置で求めることができる。 Compound having metal salt structure of phosphonic acid group in main chain, side chain, main chain and side chain of embodiment and compound having ammonium salt structure of phosphonic acid group in main chain, side chain, main chain and side chain (molecules) is represented by C x H y P z O w N r Cl s Br t M u. M is a metal. In order to increase the permeation flow rate, 2 ≦ x ≦ 9, 8 ≦ y ≦ 28, 1 ≦ z ≦ 6, 3 ≦ w ≦ 18, 0 ≦ r ≦ 3, 0 ≦ s ≦ 1, 0 ≦ t ≦ 1, 2. It is preferable to satisfy ≦ u ≦ 10. In order to reduce the reverse flow rate of the solute, 2 ≦ x ≦ 15, 8 ≦ y ≦ 35, 2 ≦ z ≦ 5, 7 ≦ w ≦ 15, 0 ≦ r ≦ 5, 0 ≦ s ≦ 1, 0 ≦ t It is preferable to satisfy ≦ 1, 2 ≦ u ≦ 10. In order to increase the permeation flow rate and reduce the solute reverse permeation flow rate, 2 ≦ x ≦ 9, 8 ≦ y ≦ 28, 2 ≦ z ≦ 5, 7 ≦ w ≦ 15, 0 ≦ r ≦ 3, 0 ≦ It is preferable to satisfy s ≦ 1, 0 ≦ t ≦ 1, 2 ≦ u ≦ 10. The metal represented by M is a metal of a metal salt of phosphonic acid. The metal of the metal salt is preferably an alkali metal or an alkaline earth metal. The metal of the metal salt is preferably one or more members selected from the group consisting of Na, K, Ca, Al and Mg. The element or structure contained in the solute of the embodiment can be analyzed by liquid chromatography, each peak compound can be separated, and determined by NMR or an organic element analyzer.
作業媒体Ｂの主鎖、側鎖、若しくは主鎖及び側鎖に主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物と主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物は、実施形態に係る溶質の化学式を図２に示す。図２の式（１）、（２）、（３）で表される構造を有する化合物のホスホン酸基が金属塩構造又はホスホン酸基がアンモニウム塩構造を有する化合物であることが好ましい。金属塩であれば、ホスホン酸基の一部又は全部がホスホン酸基の金属塩である。アンモニウム塩であれば、ホスホン酸基の一部又は全部がホスホン酸基のアンモニウム塩である。溶質の化合物に含まれる側鎖の一部に塩ではないホスホン酸基が含まれていてもよい。 Main chain, side chain, main chain and side chain of working medium B, compound having main chain, side chain, or ammonium salt structure of phosphonic acid group in main chain and side chain and main chain, side chain, or main chain As for a compound having a metal salt structure of a phosphonic acid group in the side chain, the chemical formula of the solute according to the embodiment is shown in FIG. The compound having a structure represented by the formulas (1), (2), and (3) in FIG. 2 is preferably a compound in which the phosphonic acid group has a metal salt structure or the phosphonic acid group has an ammonium salt structure. In the case of a metal salt, part or all of the phosphonic acid group is a metal salt of a phosphonic acid group. In the case of an ammonium salt, part or all of the phosphonic acid group is an ammonium salt of a phosphonic acid group. A part of the side chain contained in the solute compound may contain a phosphonic acid group that is not a salt.
式（１）のＸ１、Ｘ２とＸ３は、Ｈ、−（ＣＨ２）ｍ１ＰＯ（ＯＨ）２（ｍ１が１から３の整数のいずれか）からなる群から選ばれる１種以上である。Ｘ１、Ｘ２とＸ３のうちの２以上は、−（ＣＨ２）ｍ１ＰＯ（ＯＨ）２（ｍ１が１から３の整数のいずれか）であると溶質損失が少ないため好ましい。図２の式（１）で表される構造を有する化合物としては、ニトロトリス（メチレンホスホン酸）が好ましい。図２の式（１）で表される構造を有する化合物のホスホン酸基が金属塩構造を有している化合物としては、ニトロトリス（メチレンホスホン酸）ナトリウム塩とニトロトリス（メチレンホスホン酸）カリウム塩が挙げられる。図２の式（１）で表される構造を有する化合物のホスホン酸基がアンモニウム塩構造を有している化合物としては、ニトロトリス（メチレンホスホン酸）アンモニウム塩が挙げられる。 X 1 , X 2 and X 3 in formula (1) are one or more selected from the group consisting of H, — (CH 2 ) m1 PO (OH) 2 (m 1 is any one of 1 to 3). It is. Two or more of X 1 , X 2 and X 3 are preferably — (CH 2 ) m 1 PO (OH) 2 (where m 1 is an integer from 1 to 3) because solute loss is small. As the compound having a structure represented by the formula (1) in FIG. 2, nitrotris (methylenephosphonic acid) is preferable. The compound having the structure represented by the formula (1) in FIG. 2 in which the phosphonic acid group has a metal salt structure includes nitrotris (methylenephosphonic acid) sodium salt and nitrotris (methylenephosphonic acid) potassium salt. Can be mentioned. Examples of the compound in which the phosphonic acid group of the compound having the structure represented by the formula (1) in FIG. 2 has an ammonium salt structure include nitrotris (methylenephosphonic acid) ammonium salt.
式（２）のＹ１とＹ２は、ＯＨ、ＣＨ３、Ｃｌ、ＢｒとＣＨ２ＣＨ２ＮＨ２からなる群から選ばれる１種以上である。図２の式（２）で表される構造を有する化合物としては、エチドロン酸が好ましい。図２の式（２）で表される構造を有する化合物のホスホン酸基が金属塩構造を有している化合物としては、エチドロン酸ナトリウム塩とエチドロン酸カリウム塩が挙げられる。図２の式（２）で表される構造を有する化合物のホスホン酸基がアンモニウム塩構造を有している化合物としては、エチドロン酸アンモニウム塩が挙げられる。 Y 1 and Y 2 in the formula (2) are at least one selected from the group consisting of OH, CH 3 , Cl, Br and CH 2 CH 2 NH 2 . Etidronic acid is preferred as the compound having a structure represented by the formula (2) in FIG. Examples of the compound in which the phosphonic acid group of the compound having the structure represented by the formula (2) in FIG. 2 has a metal salt structure include etidronate sodium salt and etidronate potassium salt. Etidronic acid ammonium salt is mentioned as a compound in which the phosphonic acid group of the compound having the structure represented by the formula (2) in FIG. 2 has an ammonium salt structure.
式（３）のＺ１、Ｚ２、Ｚ３とＺ４は、Ｈ、−（ＣＨ２）ｍ２ＰＯ（ＯＨ）２（ｍ２が１から３の整数のいずれか）、−（ＣＨ２）ｍ３Ｎ（（ＣＨ２）ｍ４ＰＯ（ＯＨ）２）２（ｍ３が１から３の整数のいずれか、ｍ４が１から３の整数のいずれか）からなる群から選ばれる１種以上である。図２の式（３）中のｎは２以上１０以下の整数である。図２の式（３）で表される構造を有する化合物としては、エチレンジアミンテトラメチレンホスホン酸とジエチレントリアミンペンタメチレンホスホン酸が好ましい。図２の式（３）で表される構造を有する化合物のホスホン酸基が金属塩構造を有している化合物としては、エチレンジアミンテトラメチレンホスホン酸ナトリウム塩、ジエチレントリアミンペンタメチレンホスホン酸ナトリウム塩、エチレンジアミンテトラメチレンホスホン酸カリウム塩とジエチレントリアミンペンタメチレンホスホン酸カリウム塩が挙げられる。図２の式（３）で表される構造を有する化合物のホスホン酸基がアンモニウム塩構造を有している化合物としては、エチレンジアミンテトラメチレンホスホン酸アンモニウム塩とジエチレントリアミンペンタメチレンホスホン酸アンモニウム塩アンモニウム塩が挙げられる。 Z 1 , Z 2 , Z 3 and Z 4 in the formula (3) are H, — (CH 2 ) m 2 PO (OH) 2 (m 2 is any integer of 1 to 3), — (CH 2 ) in m3 N ((CH 2) m4 PO (OH) 2) 2 (m 3 is any one of 1 to 3 integers, m 4 is any one of 1 to 3 integer) one or more members selected from the group consisting of is there. N in the formula (3) in FIG. 2 is an integer of 2 or more and 10 or less. As the compound having a structure represented by the formula (3) in FIG. 2, ethylenediaminetetramethylenephosphonic acid and diethylenetriaminepentamethylenephosphonic acid are preferable. Examples of the compound in which the phosphonic acid group of the compound represented by the formula (3) in FIG. 2 has a metal salt structure include ethylenediaminetetramethylenephosphonic acid sodium salt, diethylenetriaminepentamethylenephosphonic acid sodium salt, ethylenediaminetetra Examples include potassium methylenephosphonate and potassium diethylenetriaminepentamethylenephosphonate. As the compound in which the phosphonic acid group of the compound having a structure represented by the formula (3) in FIG. 2 has an ammonium salt structure, ethylenediaminetetramethylenephosphonic acid ammonium salt and diethylenetriaminepentamethylenephosphonic acid ammonium salt ammonium salt are Can be mentioned.
したがって、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物は、エチドロン酸ナトリウム塩、エチドロン酸カリウム塩、ニトロトリス（メチレンホスホン酸）ナトリウム塩、ニトロトリス（メチレンホスホン酸）カリウム塩、エチレンジアミンテトラメチレンホスホン酸ナトリウム塩、ジエチレントリアミンペンタメチレンホスホン酸ナトリウム塩、エチレンジアミンテトラメチレンホスホン酸カリウム塩とジエチレントリアミンペンタメチレンホスホン酸カリウム塩からなる群のうちのいずれか１種以上であることが好ましい。 Accordingly, compounds having a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain include etidronate sodium salt, etidronate potassium salt, nitrotris (methylenephosphonic acid) sodium salt, nitrotris (methylenephosphon). Acid) potassium salt, ethylenediaminetetramethylenephosphonic acid sodium salt, diethylenetriaminepentamethylenephosphonic acid sodium salt, ethylenediaminetetramethylenephosphonic acid potassium salt and diethylenetriaminepentamethylenephosphonic acid potassium salt Is preferred.
したがって、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物は、エチドロン酸アンモニウム塩、ニトロトリス（メチレンホスホン酸）アンモニウム塩、エチレンジアミンテトラメチレンホスホン酸アンモニウム塩とジエチレントリアミンペンタメチレンホスホン酸アンモニウム塩からなる群のうちのいずれか１種以上であることが好ましい。 Accordingly, compounds having an ammonium salt structure of phosphonic acid group in the main chain, side chain, or main chain and side chain are etidronate ammonium salt, nitrotris (methylenephosphonic acid) ammonium salt, ethylenediaminetetramethylenephosphonic acid ammonium salt and diethylenetriamine. Any one or more members selected from the group consisting of ammonium pentamethylenephosphonates are preferred.
アルカリ金属塩又はアンモニウム塩の置換数はｐＨによって変化する。例えば、エチドロン酸の２Ｎａ塩は弱酸性であり、４Ｎａ塩はアルカリ性である。ＦＯ膜の耐性の観点から、中性付近の作業媒体Ｂを用いることが望ましいが、浸透圧の観点からは置換数が多いほうが好ましい。そこで、実施形態の作業媒体ＢのｐＨは、２以上１０以下であることが好ましい。作業媒体ＢのｐＨは、堀場製ガラス電極式水素イオン濃度計でマニュアル記載の方法で測定することによって求められる。 The substitution number of the alkali metal salt or ammonium salt varies depending on the pH. For example, the 2Na salt of etidronic acid is weakly acidic and the 4Na salt is alkaline. From the viewpoint of the resistance of the FO film, it is desirable to use the working medium B near neutrality, but from the viewpoint of osmotic pressure, a larger number of substitutions is preferable. Therefore, the pH of the working medium B of the embodiment is preferably 2 or more and 10 or less. The pH of the working medium B is determined by measuring it with a glass electrode type hydrogen ion concentration meter manufactured by Horiba by the method described in the manual.
作業媒体Ｂ中の溶質である主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物と主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物の濃度は、使用されるべき被処理水Ａ中の溶質の濃度、溶質の種類、溶質の特性に基づいて調節することが望ましい。通常、作業媒体Ｂ中の溶質である主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物と主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物の濃度は１０質量％以上７０質量％以下、より好ましくは３０質量％以上７０質量％以下、最も好ましくは５０質量％以上質量％以下にすることが望ましい。ただし、粘度が上がってしまう場合など不都合が起こるときは濃度を下げる方向で調節する。濃度の上限に関してはその物質特有の溶解度に依存する。 A solute in the working medium B, a main chain, a side chain, or a compound having a metal salt structure of a phosphonic acid group in the main chain and the side chain and an ammonium of a phosphonic acid group in the main chain, the side chain, or the main chain and the side chain The concentration of the compound having a salt structure is desirably adjusted based on the concentration of the solute in the water to be treated A to be used, the kind of solute, and the characteristics of the solute. Usually, a compound having a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain, which is a solute in the working medium B, and a phosphonic acid group in the main chain, side chain, or main chain and side chain The concentration of the compound having an ammonium salt structure is preferably 10% by mass to 70% by mass, more preferably 30% by mass to 70% by mass, and most preferably 50% by mass to 70% by mass. However, when inconvenience occurs, such as when the viscosity increases, the concentration is adjusted to decrease. The upper limit of concentration depends on the solubility of the substance.
（第２実施形態）
次に、水処理システムの１つの例である脱塩システムを図３に示す概略図を参照して説明する。第２実施形態において、第１チャンバー１３、被処理水Ａ、第２チャンバー１４、作業媒体Ｂと浸透膜１２は、第１実施形態と共通する。被処理水Ａは、海水などの塩水（塩化ナトリウム水溶液）である。第２実施形態に用いられる作業媒体Ｂは、第１実施形態の作業媒体Ｂである。図３以降では、水処理システム中の被処理水、作業媒体と水の符号は示していないが、これらの符号は、図１の水処理システムと共通する。
(Second Embodiment)
Next, a desalination system as an example of the water treatment system will be described with reference to a schematic diagram shown in FIG. In 2nd Embodiment, the 1st chamber 13, the to-be-processed water A, the 2nd chamber 14, the working medium B, and the permeable membrane 12 are common in 1st Embodiment. The treated water A is salt water (sodium chloride aqueous solution) such as seawater. The working medium B used in the second embodiment is the working medium B of the first embodiment. In FIG. 3 and subsequent figures, reference numerals of the water to be treated, the working medium, and water in the water treatment system are not shown, but these signs are common to the water treatment system of FIG.
脱塩システム２００は、浸透圧発生器１と、希釈作業媒体タンク２と、逆浸透膜分離器３と、濃縮作業媒体タンク４とを備える。浸透圧発生器１、希釈作業媒体タンク２、逆浸透膜分離部３及び濃縮作業媒体タンク４は、この順序で接続されてループを形成している。浸透圧を誘起する作業媒体Ｂ（ドロー溶液）はこのループを循環する。すなわち、作業媒体Ｂは浸透圧発生器１、希釈作業媒体タンク２、逆浸透膜分離器３及び濃縮作業媒体タンク４をこの順番で循環する。なお、上及び下は、図面に表された方向であり、例えば、濃縮作業媒体タンク４は、希釈作業媒体タンク２の上側にあり、浸透圧発生器１は、逆浸透膜分離器３の左側にある。 The desalination system 200 includes an osmotic pressure generator 1, a dilution working medium tank 2, a reverse osmosis membrane separator 3, and a concentration working medium tank 4. The osmotic pressure generator 1, the dilution working medium tank 2, the reverse osmosis membrane separation unit 3, and the concentrated working medium tank 4 are connected in this order to form a loop. The working medium B (draw solution) that induces osmotic pressure circulates in this loop. That is, the working medium B circulates through the osmotic pressure generator 1, the diluted working medium tank 2, the reverse osmosis membrane separator 3 and the concentrated working medium tank 4 in this order. The upper and lower sides are directions shown in the drawing. For example, the concentration working medium tank 4 is above the dilution working medium tank 2, and the osmotic pressure generator 1 is on the left side of the reverse osmosis membrane separator 3. It is in.
被処理水タンク１５は、第１チャンバー１３が位置する処理容器１０の上部にパイプライン１０１ａを通して接続されている。第１ポンプ１６は、パイプライン１０１ａに設けられている。濃縮された被処理水Ａを排出するためのパイプライン１０１ｂは、第１チャンバー１３が位置する第１処理容器１１の下部に接続されている。 The to-be-processed water tank 15 is connected to the upper part of the processing container 10 in which the 1st chamber 13 is located through the pipeline 101a. The first pump 16 is provided in the pipeline 101a. A pipeline 101b for discharging the concentrated water A to be treated is connected to the lower portion of the first treatment container 11 where the first chamber 13 is located.
逆浸透膜分離部３は、例えば気密な第２処理容器２１を備えている。第２処理容器２１は、例えば逆浸透膜（ＲＯ膜）２２により例えば水平方向に区画され、左側に第３チャンバー２３が、右側に第４チャンバー２４がそれぞれ形成されている。 The reverse osmosis membrane separation unit 3 includes, for example, an airtight second processing vessel 21. The second processing vessel 21 is partitioned, for example, in a horizontal direction by, for example, a reverse osmosis membrane (RO membrane) 22, and a third chamber 23 is formed on the left side and a fourth chamber 24 is formed on the right side.
希釈作業媒体タンク２は、第３チャンバー２３が位置する第２処理容器２１の下部にパイプライン１０１ｅを通して接続されている。第３ポンプ２５は、パイプライン１０１ｅに設けられている。第３チャンバー２３が位置する第２処理容器２１の上部は、濃縮作業媒体タンク４にパイプライン１０１ｆを通して接続されている。第４チャンバー２４が位置する第２処理容器２１の下部は、純水タンク２６にパイプライン１０１ｇを通して接続されている。純水タンク２６には、作業媒体Ｂを濃縮する際に逆浸透膜２２を通って、第４チャンバーに移動した水（淡水）が収容される。純水タンク２６には、当該純水タンク２６内の純水を外部に送出して回収するためのパイプライン１０１ｈが接続されている。開閉弁２７は、パイプライン１０１ｈに設けられる。例えば、純水タンク２６内の純水が一定量を超えると開かれる。 The dilution working medium tank 2 is connected to the lower part of the second processing vessel 21 where the third chamber 23 is located through a pipeline 101e. The third pump 25 is provided in the pipeline 101e. The upper part of the second processing vessel 21 in which the third chamber 23 is located is connected to the concentration work medium tank 4 through a pipeline 101f. The lower part of the second processing vessel 21 where the fourth chamber 24 is located is connected to the pure water tank 26 through a pipeline 101g. The pure water tank 26 stores water (fresh water) that has moved through the reverse osmosis membrane 22 and moved to the fourth chamber when the working medium B is concentrated. Connected to the pure water tank 26 is a pipeline 101h for sending and collecting the pure water in the pure water tank 26 to the outside. The on-off valve 27 is provided in the pipeline 101h. For example, it is opened when the pure water in the pure water tank 26 exceeds a certain amount.
濃縮作業媒体タンク４は、第２チャンバー１３が位置する第１処理容器１１の上部にパイプライン１０１ｃを通して接続されている。第２ポンプ１７は、パイプライン１０１ａに設けられている。第２チャンバー１３が位置する処理容器１０の下部は、希釈作業媒体タンク２にパイプライン１０１ｄを通して接続されている。 The concentration working medium tank 4 is connected to the upper part of the first processing container 11 where the second chamber 13 is located through a pipeline 101c. The second pump 17 is provided in the pipeline 101a. The lower part of the processing container 10 in which the second chamber 13 is located is connected to the dilution working medium tank 2 through a pipeline 101d.
次に、図３に示す脱塩システム２００による脱塩操作を説明する。 Next, a desalting operation by the desalting system 200 shown in FIG. 3 will be described.
第１ポンプ１６を駆動して被処理水Ａ（例えば海水）を被処理水タンク１５から浸透圧発生器１の第１チャンバー１３内にパイプライン１０１ａを通して供給する。海水の供給と前後して第２ポンプ１７を駆動して濃縮作業媒体Ｂを濃縮作業媒体タンク４から浸透圧発生器１の第２チャンバー１４内にパイプライン１０１ｃを通して供給する。このとき、第２チャンバー１４に供給された濃縮作業媒体Ｂの溶質濃度は、第１チャンバー１３に供給された海水の塩濃度に比べて高濃度である。このため、第１チャンバー１３内の海水と第２チャンバー１４内の濃縮作業媒体Ｂとの間で浸透圧差が生じ、海水中の水が浸透膜１２を透過して第２チャンバー１４内に移動する。第２チャンバー１４内の濃縮作業媒体Ｂは、第１実施形態の溶質を含む水溶液で、高い浸透圧誘起作用を示す。このため、第１チャンバー１３内の海水中の水が浸透膜１２を透過して第２チャンバー１４内の濃縮作業媒体Ｂに移動する際、高い透過流束を発生する。その結果、第１チャンバー１３内の海水中の多くの水を第２チャンバー１４の濃縮作業媒体Ｂに移動でき、塩水から水（純水）を取り出す高効率の脱塩処理を実行できる。 The first pump 16 is driven to supply the treated water A (for example, seawater) from the treated water tank 15 into the first chamber 13 of the osmotic pressure generator 1 through the pipeline 101a. Before and after the supply of seawater, the second pump 17 is driven to supply the concentrated working medium B from the concentrated working medium tank 4 into the second chamber 14 of the osmotic pressure generator 1 through the pipeline 101c. At this time, the solute concentration of the concentrated working medium B supplied to the second chamber 14 is higher than the salt concentration of seawater supplied to the first chamber 13. For this reason, an osmotic pressure difference is generated between the seawater in the first chamber 13 and the concentrated working medium B in the second chamber 14, and the water in the seawater passes through the osmotic membrane 12 and moves into the second chamber 14. . The concentrated working medium B in the second chamber 14 is an aqueous solution containing the solute of the first embodiment and exhibits a high osmotic pressure inducing action. For this reason, when the water in the seawater in the first chamber 13 permeates the osmotic membrane 12 and moves to the concentration working medium B in the second chamber 14, a high permeation flux is generated. As a result, a large amount of water in the seawater in the first chamber 13 can be moved to the concentration working medium B in the second chamber 14, and a highly efficient desalting process for extracting water (pure water) from the salt water can be performed.
浸透圧発生器１において、海水中の水が第１チャンバー１３から第２チャンバー１４内の濃縮作業媒体Ｂに移動することにより、海水は濃縮海水として第１チャンバー１３からパイプライン１０１ｂを通して排出され、濃縮作業媒体Ｂは移動した水で希釈される。 In the osmotic pressure generator 1, when the water in the seawater moves from the first chamber 13 to the concentration working medium B in the second chamber 14, the seawater is discharged as concentrated seawater from the first chamber 13 through the pipeline 101b, The concentrated working medium B is diluted with the transferred water.
第２チャンバー１４の希釈作業媒体Ｂは、希釈作業媒体タンク２にパイプライン１０１ｄを通して送出され、貯留される。希釈作業媒体Ｂが希釈作業媒体タンク２内に所定の水位まで貯まると、第３ポンプ２５を駆動して希釈作業媒体タンク２内の希釈作業媒体Ｂを逆浸透膜分離部３の第２処理容器２１の第３チャンバー２３にパイプライン１０１ｅを通して所望の圧力で供給する。所望の圧力で第３チャンバー２３に供給された希釈作業媒体Ｂ中の水は、逆浸透膜（ＲＯ膜）２２を強制的に透過して第４チャンバー２４に移動する。第３チャンバー２３内の希釈作業媒体Ｂは、水を第４チャンバー２４に移動することにより濃縮される。濃縮作業媒体Ｂは、第３チャンバー２３から濃縮作業媒体タンク４に送出される。濃縮作業媒体タンク４内の濃縮作業媒体Ｂは、第２ポンプ１７を駆動することにより浸透圧発生器１の第２チャンバー１４内に供給され、前述したように塩水から水（純水）を取り出す脱塩処理に利用される。 The diluted working medium B in the second chamber 14 is sent to the diluted working medium tank 2 through the pipeline 101d and stored. When the diluted working medium B is stored in the diluted working medium tank 2 up to a predetermined water level, the third pump 25 is driven to move the diluted working medium B in the diluted working medium tank 2 to the second processing container of the reverse osmosis membrane separation unit 3. The third chamber 23 is supplied at a desired pressure through the pipeline 101e. The water in the diluted working medium B supplied to the third chamber 23 at a desired pressure is forced to permeate the reverse osmosis membrane (RO membrane) 22 and move to the fourth chamber 24. The diluted working medium B in the third chamber 23 is concentrated by moving water to the fourth chamber 24. The concentrated working medium B is sent from the third chamber 23 to the concentrated working medium tank 4. The concentrated working medium B in the concentrated working medium tank 4 is supplied into the second chamber 14 of the osmotic pressure generator 1 by driving the second pump 17 and takes out water (pure water) from the salt water as described above. Used for desalting.
他方、第４チャンバー２４に移動した水（純水）は、パイプライン１０１ｇを通して純水タンク２６に送出される。純水タンク２６内の水が一定量を超えると、開閉弁２７を開き、パイプライン１０１ｈを通して外部に送出して水を回収する。 On the other hand, the water (pure water) moved to the fourth chamber 24 is sent to the pure water tank 26 through the pipeline 101g. When the amount of water in the pure water tank 26 exceeds a certain amount, the on-off valve 27 is opened and sent to the outside through the pipeline 101h to collect the water.
したがって、海水の脱塩処理（純水の回収）を効率的に実施し得る、低コストにて運転可能な脱塩システムを提供できる。 Therefore, it is possible to provide a desalting system that can efficiently operate seawater desalination (recovery of pure water) and can be operated at low cost.
なお、図３に示す脱塩システム２００において、浸透圧発生器は第１処理容器１１を浸透膜により水平方向に区画して第１チャンバー１３、第２チャンバー１４を形成したが、第１処理容器を浸透膜により上下に区画して第１チャンバー１３を、第２チャンバー１４を形成してもよい。 In the desalination system 200 shown in FIG. 3, the osmotic pressure generator forms the first chamber 13 and the second chamber 14 by partitioning the first processing vessel 11 horizontally by the osmosis membrane. The first chamber 13 and the second chamber 14 may be formed by dividing the upper and lower sides by a permeable membrane.
脱塩処理を行うことにより、作業媒体Ｂの溶質濃度が低下した場合は、濃縮作業媒体タンク４などにおいて、溶質の添加を行うことが好ましい。 When the solute concentration of the working medium B is reduced by performing the desalting treatment, it is preferable to add the solute in the concentrated working medium tank 4 or the like.
図３に示す脱塩システム２００において、希釈作業媒体Ｂの濃縮は逆浸透膜（ＲＯ膜）を備える逆浸透膜分離部で行なう場合に限らず、希釈作業媒体Ｂの水を除去するものであれば如何なる装置で行なってもよい。 In the desalination system 200 shown in FIG. 3, the concentration of the diluted working medium B is not limited to being performed in a reverse osmosis membrane separation unit including a reverse osmosis membrane (RO membrane), but may be used to remove water from the diluted working medium B. Any apparatus may be used.
（第３実施形態）
次に、水処理システムの１つの例である濃縮システム３００を図４に示す概略図を参照して説明する。第３実施形態に用いられる作業媒体Ｂは、第１実施形態の作業媒体Ｂである。
(Third embodiment)
Next, a concentration system 300 as an example of the water treatment system will be described with reference to a schematic diagram shown in FIG. The working medium B used in the third embodiment is the working medium B of the first embodiment.
濃縮システム３００は、浸透圧発生器３１と、希釈作業媒体タンク３２と、膜蒸留分離器３３と、濃縮作業媒体タンク３４とを備える。浸透圧発生器３１、希釈作業媒体タンク３２、膜蒸留分離器３３及び濃縮作業媒体タンク３４は、この順序で接続されてループを形成している。作業媒体Ｂ（ドロー溶液）はこのループを循環する。すなわち、作業媒体Ｂは浸透圧発生器３１、希釈作業媒体タンク３２、膜蒸留分離器３３及び濃縮作業媒体タンク３４をこの順番で循環する。 The concentration system 300 includes an osmotic pressure generator 31, a dilution working medium tank 32, a membrane distillation separator 33, and a concentration working medium tank 34. The osmotic pressure generator 31, the dilution working medium tank 32, the membrane distillation separator 33, and the concentration working medium tank 34 are connected in this order to form a loop. The working medium B (draw solution) circulates in this loop. That is, the working medium B circulates through the osmotic pressure generator 31, the diluted working medium tank 32, the membrane distillation separator 33, and the concentrated working medium tank 34 in this order.
浸透圧発生器３１は、例えば気密な第１処理容器４１を備えている。第１処理容器４１は、浸透膜４２（例えば正浸透膜：ＦＯ膜）により例えば水平方向に区画され、左側に第１チャンバー４３が、右側に第２チャンバー４４がそれぞれ形成されている。被処理水Ａ、例えば産業廃水等の原液を収容した被処理水タンク４５は、第１チャンバー４３が位置する第１処理容器４１の上部にパイプライン２０１ａを通して接続されている。第１ポンプ４６は、パイプライン２０１ａに設けられている。第１チャンバー４３が位置する第１処理容器４１の下部には、当該第１チャンバー４３内の濃縮した原液を外部に排出するためのパイプライン２０１ｂが接続されている。 The osmotic pressure generator 31 includes, for example, an airtight first processing container 41. The first processing container 41 is partitioned, for example, in a horizontal direction by a osmotic membrane 42 (for example, a normal osmosis membrane: FO membrane), and a first chamber 43 is formed on the left side and a second chamber 44 is formed on the right side. A to-be-treated water tank 45 containing a to-be-treated water A, for example, an undiluted solution such as industrial wastewater, is connected to the upper portion of the first treatment container 41 where the first chamber 43 is located through a pipeline 201a. The first pump 46 is provided in the pipeline 201a. A pipeline 201b for discharging the concentrated stock solution in the first chamber 43 to the outside is connected to the lower portion of the first processing container 41 where the first chamber 43 is located.
濃縮作業媒体タンク３４は、第２チャンバー４４が位置する第１処理容器４１の上部にパイプライン２０１ｃを通して接続されている。第２ポンプ４７は、パイプライン２０１ｃに設けられている。第２チャンバー４４が位置する第１処理容器１１の下部は、希釈作業媒体タンク３２にパイプライン２０１ｄを通して接続されている。 The concentration working medium tank 34 is connected to the upper part of the first processing container 41 where the second chamber 44 is located through a pipeline 201c. The second pump 47 is provided in the pipeline 201c. The lower part of the first processing container 11 where the second chamber 44 is located is connected to the dilution working medium tank 32 through a pipeline 201d.
膜蒸留分離器３３は、例えば気密な第２処理容器５１を備えている。第２処理容器５１は、例えば多孔質ラテックス膜からなる脱水膜５２により例えば水平方向に区画され、左側に第３チャンバー５３が、右側に第４チャンバー５４がそれぞれ形成されている。 The membrane distillation separator 33 includes, for example, an airtight second processing vessel 51. The second processing container 51 is partitioned, for example, in a horizontal direction by a dehydration film 52 made of, for example, a porous latex film, and a third chamber 53 is formed on the left side and a fourth chamber 54 is formed on the right side.
前記希釈作業媒体タンク３２は、第３チャンバー５３が位置する第２処理容器５１の下部にパイプライン２０１ｅを通して接続されている。第１開閉弁６１、熱交換器６２及び第３ポンプ６３は、パイプライン２０１ｅに作業媒体Ｂの流れ方向に沿ってこの順序で設けられている。熱交換器６２には、例えば排熱ガスのパイプライン２０１ｆが交差され、パイプライン２０１ｅを流れる作業媒体Ｂが排熱ガスと熱交換して当該作業媒体Ｂを加熱する。第３チャンバー５３が位置する第２処理容器５１の上部は、循環タンク６４の上部にパイプライン２０１ｇを通して接続されている。循環タンク６４は、第１開閉弁６１と熱交換器６２の間に位置するパイプライン２０１ｅの部位にパイプライン２０１ｈを通して接続されている。第２開閉弁６５は、パイプライン２０１ｈに設けられている。 The dilution working medium tank 32 is connected through a pipeline 201e to the lower part of the second processing vessel 51 where the third chamber 53 is located. The first on-off valve 61, the heat exchanger 62, and the third pump 63 are provided in this order along the flow direction of the working medium B in the pipeline 201e. For example, a waste heat gas pipeline 201f intersects the heat exchanger 62, and the work medium B flowing through the pipeline 201e exchanges heat with the exhaust heat gas to heat the work medium B. The upper part of the second processing vessel 51 where the third chamber 53 is located is connected to the upper part of the circulation tank 64 through a pipeline 201g. The circulation tank 64 is connected to a portion of the pipeline 201e located between the first on-off valve 61 and the heat exchanger 62 through the pipeline 201h. The second on-off valve 65 is provided in the pipeline 201h.
このような構成により膜蒸留分離器３３の第３チャンバー５３、循環タンク６４及びこれらの部材を接続するパイプライン２０１ｅ、２０１ｇ、２０１ｈによるループが形成される。すなわち、後述する第３チャンバー５３で脱水処理され、循環タンク６４に貯留された希釈作業媒体Ｂは第２開閉弁６５を開き、第３ポンプ６３を駆動することにより、パイプライン２０１ｈ、パイプライン２０１ｅ、第３チャンバー５３及びパイプライン２０１ｇを循環する、希釈作業媒体循環系を形成している。なお、希釈作業媒体Ｂの循環において、第１開閉弁６１を閉じることにより希釈作業媒体循環系は希釈作業媒体タンク３２と隔絶される。 With such a configuration, a loop is formed by the third chamber 53 of the membrane distillation separator 33, the circulation tank 64, and pipelines 201e, 201g, and 201h that connect these members. That is, the diluted working medium B dehydrated in the third chamber 53 described later and stored in the circulation tank 64 opens the second on-off valve 65 and drives the third pump 63, whereby the pipeline 201h and the pipeline 201e. A dilution working medium circulation system is circulated through the third chamber 53 and the pipeline 201g. In the circulation of the diluted working medium B, the diluted working medium circulation system is isolated from the diluted working medium tank 32 by closing the first on-off valve 61.
循環タンク６４は、濃縮作業媒体タンク３４にパイプライン２０１ｉを通して接続されている。第４ポンプ６６は、パイプライン２０１ｉに設けられている。 The circulation tank 64 is connected to the concentration work medium tank 34 through a pipeline 201i. The fourth pump 66 is provided in the pipeline 201i.
第１純水タンク７１は、第４チャンバー５４が位置する第２処理容器５１の上部にパイプライン２０１ｊを通して接続されている。第４チャンバー５４が位置する第２処理容器５１の下部は、第２純水タンク７２にパイプライン２０１ｋを通して接続されている。第３開閉弁７３は、パイプライン２０１ｋに設けられ、純水の非循環時に閉じて純水を第４チャンバー５４内に滞留する。第２純水タンク７２は、第１純水タンク７１にパイプライン２０１ｍを通して接続されている。第５ポンプ７４は、パイプライン２０１ｍに設けられている。このような構成により第１純水タンク７１、膜蒸留分離器３３の第４チャンバー５４、第２純水タンク７２及びこれらの部材を接続するパイプライン２０１ｊ，２０１ｋ，２０１ｍによるループが形成される。すなわち、第２純水タンク７２内の純水は第３開閉弁７３を開き、第５ポンプ７４を駆動することにより、パイプライン２０１ｍ、第１純水タンク７１、パイプライン２０１ｊ、第４チャンバー５４及びパイプライン２０１ｋを循環する、純水循環冷却系を形成している。 The first pure water tank 71 is connected to the upper part of the second processing vessel 51 where the fourth chamber 54 is located through a pipeline 201j. The lower part of the second processing vessel 51 where the fourth chamber 54 is located is connected to the second pure water tank 72 through a pipeline 201k. The third on-off valve 73 is provided in the pipeline 201k and closes when the pure water is not circulated so that the pure water stays in the fourth chamber 54. The second pure water tank 72 is connected to the first pure water tank 71 through a pipeline 201m. The fifth pump 74 is provided in the pipeline 201m. With such a configuration, a loop is formed by the first pure water tank 71, the fourth chamber 54 of the membrane distillation separator 33, the second pure water tank 72, and pipelines 201j, 201k, 201m connecting these members. That is, the pure water in the second pure water tank 72 opens the third on-off valve 73 and drives the fifth pump 74, thereby causing the pipeline 201 m, the first pure water tank 71, the pipeline 201 j, and the fourth chamber 54. And the pure water circulation cooling system which circulates through the pipeline 201k is formed.
第２純水タンク７２には、当該第２純水タンク７２内の純水を外部に送出して回収するためのパイプライン２０１ｎが接続されている。第４開閉弁７５は、パイプライン２０１ｎに設けられている。第４開閉弁７５は、前述した純水の循環時に閉じられ、第２純水タンク７５内の純水が一定量を超えると開かれる。 Connected to the second pure water tank 72 is a pipeline 201n for sending out and collecting the pure water in the second pure water tank 72 to the outside. The fourth on-off valve 75 is provided in the pipeline 201n. The fourth on-off valve 75 is closed when the pure water is circulated as described above, and is opened when the pure water in the second pure water tank 75 exceeds a certain amount.
次に、図４に示す濃縮システム３００による濃縮操作を説明する。 Next, the concentration operation by the concentration system 300 shown in FIG. 4 will be described.
第１ポンプ４６を駆動して被処理水Ａである原液（例えば産業廃水）を被処理水タンク４５から浸透圧発生器３１の第１チャンバー４３内にパイプライン２０１ａを通して供給する。原液の供給と前後して第２ポンプ４７を駆動して濃縮作業媒体Ｂを濃縮作業媒体タンク３４から浸透圧発生器３１の第２チャンバー４４内にパイプライン２０１ｃを通して供給する。第２チャンバー４４に供給された濃縮作業媒体Ｂは第１チャンバー４３に供給された原液の濃度に比べて高濃度である。このため、第１チャンバー４３内の原液と第２チャンバー４４内の濃縮作業媒体Ｂとの間で浸透圧差が生じ、原液中の水が浸透膜４２を透過して第２チャンバー４４内に移動する。このとき、第２チャンバー４４内の濃縮作業媒体Ｂは、実施形態の溶質を含む水溶液で、高い浸透圧の誘起作用を示す。このため、第１チャンバー４３内の原液中の水が浸透膜３２を透過して第２チャンバー４４内の作業媒体Ｂに移動する際、高い透過流束を発生する。その結果、第１チャンバー４３内の原液中の多くの水を第２チャンバー４４の作業媒体Ｂに移動でき、原液の濃縮処理が高効率になされる。 The first pump 46 is driven to supply a raw solution (for example, industrial wastewater) as the water to be treated A from the water tank 45 to be treated into the first chamber 43 of the osmotic pressure generator 31 through the pipeline 201a. Before and after the supply of the stock solution, the second pump 47 is driven to supply the concentrated working medium B from the concentrated working medium tank 34 into the second chamber 44 of the osmotic pressure generator 31 through the pipeline 201c. The concentrated working medium B supplied to the second chamber 44 has a higher concentration than the concentration of the stock solution supplied to the first chamber 43. For this reason, an osmotic pressure difference is generated between the stock solution in the first chamber 43 and the concentrated working medium B in the second chamber 44, and the water in the stock solution passes through the osmotic membrane 42 and moves into the second chamber 44. . At this time, the concentrated working medium B in the second chamber 44 is an aqueous solution containing the solute of the embodiment, and exhibits a high osmotic pressure inducing action. For this reason, when the water in the undiluted solution in the first chamber 43 passes through the osmotic membrane 32 and moves to the working medium B in the second chamber 44, a high permeation flux is generated. As a result, a large amount of water in the stock solution in the first chamber 43 can be moved to the working medium B in the second chamber 44, and the concentration process of the stock solution is made highly efficient.
浸透圧発生器３１において、原液中の水が第１チャンバー４３から第２チャンバー４４内の濃縮作業媒体Ｂに移動することにより、原液は濃縮原液として第１チャンバー４３からパイプライン２０１ｂを通して排出され、回収される。濃縮作業媒体Ｂは、移動した水により希釈される。 In the osmotic pressure generator 31, the water in the stock solution moves from the first chamber 43 to the concentration working medium B in the second chamber 44, whereby the stock solution is discharged from the first chamber 43 through the pipeline 201b as a concentrated stock solution. Collected. The concentrated working medium B is diluted with the moved water.
第２チャンバー４４の希釈作業媒体Ｂは、希釈作業媒体タンク３２にパイプライン２０１ｄを通して送出され、貯留される。希釈作業媒体Ｂが希釈作業媒体タンク３２内に所定量まで貯留されると、パイプライン２０１ｅに設けた第１開閉弁６１を開き、パイプライン２０１ｈに設けた第２開閉弁６５を閉じ、第３ポンプ６３を駆動する。これにより希釈作業媒体タンク３２内の希釈作業媒体Ｂを膜蒸留分離器３３の第２処理容器５１の第３チャンバー５３にパイプライン２０１ｅを通して供給する。希釈作業媒体Ｂが第３チャンバー５３に供給される間、パイプライン２０１ｅを流通する希釈作業媒体Ｂはパイプライン２０１ｆが交差する熱交換器６２で当該パイプライン２０１ｆを流通する排熱ガスと熱交換されて加熱される。また、第２純水タンク７２内の純水を第３開閉弁７３を開き、第５ポンプ７４を駆動することにより、純水をパイプライン２０１ｍ、第１純水タンク７１、パイプライン２０１ｊ、第４チャンバー５４及びパイプライン２０１ｋに循環させて、膜蒸留分離器３３の多孔質ラテックス膜からなる脱水膜５２を第４チャンバー５４側から純水で冷却する。すなわち、純水循環冷却系により第４チャンバー５４側の脱水膜５２を冷却する。 The diluted working medium B in the second chamber 44 is sent to the diluted working medium tank 32 through the pipeline 201d and stored. When the diluted working medium B is stored up to a predetermined amount in the diluted working medium tank 32, the first on-off valve 61 provided on the pipeline 201e is opened, the second on-off valve 65 provided on the pipeline 201h is closed, and the third The pump 63 is driven. As a result, the diluted working medium B in the diluted working medium tank 32 is supplied to the third chamber 53 of the second processing container 51 of the membrane distillation separator 33 through the pipeline 201e. While the diluted working medium B is supplied to the third chamber 53, the diluted working medium B flowing through the pipeline 201e exchanges heat with the exhaust heat gas flowing through the pipeline 201f in the heat exchanger 62 where the pipeline 201f intersects. And heated. Also, the pure water in the second pure water tank 72 is opened by opening the third on-off valve 73 and driving the fifth pump 74, whereby pure water is supplied to the pipeline 201m, the first pure water tank 71, the pipeline 201j, The dehydration membrane 52 made of the porous latex membrane of the membrane distillation separator 33 is cooled with pure water from the fourth chamber 54 side by circulating through the four chambers 54 and the pipeline 201k. That is, the dehydration film 52 on the fourth chamber 54 side is cooled by the pure water circulation cooling system.
このように加熱した希釈作業媒体Ｂを通して膜蒸留分離器３３の第３チャンバー５３にパイプライン２０１ｅを供給しながら、膜蒸留分離器３３の脱水膜５２を第４チャンバー５４内の循環する純水で冷却することによって、第３チャンバー５３内で希釈作業媒体Ｂ中の水が蒸発し、その蒸気は多孔質ラテックス膜からなる脱水膜５２を透過して第４チャンバー５４に移動し、循環する純水により冷却、凝縮してその中に取込まれる。すなわち、希釈作業媒体Ｂは第３チャンバー５３内で脱水処理される。第３チャンバー５３内の脱水処理された希釈作業媒体Ｂは、パイプライン２０１ｇを通して循環タンク６４に送出され、貯留される。循環タンク６４に貯留された希釈作業媒体Ｂは、前記脱水処理により、ある濃度まで濃縮される。 While supplying the pipeline 201e to the third chamber 53 of the membrane distillation separator 33 through the diluted working medium B thus heated, the dehydrated membrane 52 of the membrane distillation separator 33 is made of pure water circulating in the fourth chamber 54. By cooling, the water in the dilution working medium B evaporates in the third chamber 53, and the vapor passes through the dehydration film 52 made of a porous latex film and moves to the fourth chamber 54 to circulate pure water. It is cooled, condensed and taken into it. That is, the diluted working medium B is dehydrated in the third chamber 53. The dehydrated diluted working medium B in the third chamber 53 is sent to the circulation tank 64 through the pipeline 201g and stored. The diluted working medium B stored in the circulation tank 64 is concentrated to a certain concentration by the dehydration process.
しかしながら、この程度の濃縮では濃度が低く、前述した濃縮作業媒体Ｂとして使用するには適切ではない。このため、脱水処理された希釈作業媒体Ｂが循環タンク６４に一定量貯留された時点で、第２開閉弁６５を開き、当該タンク６４内の脱水処理された希釈作業媒体Ｂをパイプライン２０１ｈに流出する。同時に、第１開閉弁６１を閉じ、循環タンク６４、パイプライン２０１ｈ、パイプライン２０１ｅ、第３チャンバー５３及びパイプライン２０１ｇからなる希釈作業媒体循環系を希釈作業媒体タンク３２と隔絶する。 However, this level of concentration is low in concentration and is not suitable for use as the above-described concentrated working medium B. Therefore, when the dehydrated diluted working medium B is stored in the circulation tank 64 in a certain amount, the second on-off valve 65 is opened, and the dehydrated diluted working medium B in the tank 64 is put into the pipeline 201h. leak. At the same time, the first on-off valve 61 is closed, and the diluted working medium circulation system including the circulation tank 64, the pipeline 201h, the pipeline 201e, the third chamber 53, and the pipeline 201g is isolated from the diluted working medium tank 32.
このような希釈作業媒体循環系及び純水循環冷却系において、前述した第３チャンバー５３内での希釈作業媒体Ｂの水の蒸発、蒸気の脱水膜５２の透過、第４チャンバー５４への移動、及び第４チャンバー５４側での循環する純水による冷却、凝縮、をなす脱水処理を複数回繰り返すことによって、希釈作業媒体Ｂを濃縮作業媒体Ｂとして使用し得る濃度にする。このような希釈作業媒体Ｂの循環、脱水処理後に第２開閉弁６５を閉じて、濃縮作業媒体Ｂを循環タンク６４に貯留する。第４チャンバー５４に移動した水（純水）は、パイプライン２０１ｋを通して第２純水タンク７２に循環する純水と共に送出される。 In such a dilution work medium circulation system and pure water circulation cooling system, the evaporation of water of the dilution work medium B in the third chamber 53, the permeation of the vapor dehydration film 52, the movement to the fourth chamber 54, And the dilution work medium B is made a concentration that can be used as the concentrated work medium B by repeating the dehydration process of cooling and condensing with the pure water circulating on the fourth chamber 54 side a plurality of times. After such circulation and dehydration of the diluted working medium B, the second on-off valve 65 is closed and the concentrated working medium B is stored in the circulation tank 64. The water (pure water) moved to the fourth chamber 54 is sent out together with the pure water circulating to the second pure water tank 72 through the pipeline 201k.
濃縮作業媒体Ｂとして使用し得る濃度の濃縮作業媒体Ｂを循環タンク６４に貯留した後は、第５ポンプ７４の駆動を停止し、第４チャンバー５４への純水の循環を停止した後、第３開閉弁７３を閉じる。なお、第２純水タンク７２内の純水が一定量を超えると、第１開閉弁７５を開き、パイプライン２０１ｎを通して外部に送出して回収される。 After the concentrated working medium B having a concentration that can be used as the concentrated working medium B is stored in the circulation tank 64, the driving of the fifth pump 74 is stopped, and the circulation of pure water to the fourth chamber 54 is stopped, 3. Close the on-off valve 73. When the pure water in the second pure water tank 72 exceeds a certain amount, the first on-off valve 75 is opened and sent to the outside through the pipeline 201n to be collected.
第４ポンプ６４を駆動して循環タンク６４内の濃縮作業媒体Ｂを濃縮作業媒体タンク３４にパイプライン２０１ｉを通して送出する。濃縮作業媒体タンク３４内の濃縮作業媒体Ｂは、前述したように原液の濃縮処理に利用するために第２ポンプ４７を駆動して浸透圧発生器３１の第２チャンバー４４内に供給される。 The fourth pump 64 is driven to send the concentrated working medium B in the circulation tank 64 to the concentrated working medium tank 34 through the pipeline 201i. As described above, the concentrated working medium B in the concentrated working medium tank 34 is supplied to the second chamber 44 of the osmotic pressure generator 31 by driving the second pump 47 so as to be used for the concentration process of the stock solution.
したがって、浸透圧発生器３１において、第１チャンバー４３に原液を供給し、第２チャンバー４４に濃縮作業媒体Ｂを供給し、原液中の水を第１チャンバー４３から第２チャンバー４４内の濃縮作業媒体Ｂに移動させて、原液を濃縮して第１チャンバー４３からパイプライン２０１ｂを通して排出され、回収する。濃縮作業媒体Ｂは、移動した水により希釈され、その希釈作業媒体Ｂは希釈作業媒体タンク３２に送出され、貯留される。 Therefore, in the osmotic pressure generator 31, the stock solution is supplied to the first chamber 43, the concentration working medium B is supplied to the second chamber 44, and the water in the stock solution is concentrated from the first chamber 43 to the second chamber 44. The stock solution is moved to the medium B, concentrated, discharged from the first chamber 43 through the pipeline 201b, and collected. The concentrated working medium B is diluted with the moved water, and the diluted working medium B is sent to the diluted working medium tank 32 and stored.
浸透圧発生器３１による原液の濃縮操作の間、希釈作業媒体タンク３２に貯留された希釈作業媒体Ｂは膜蒸留分離器３３の第３チャンバー５３を含む希釈作業媒体循環系及び膜蒸留分離器３３の第４チャンバー５４を含む純水循環冷却系により濃縮操作がなされ、濃縮作業媒体タンク３４に送出され、第４チャンバー５４に移動した水（純水）は第２純水タンク７２から送出、回収される。すなわち、浸透圧発生器３１による原液の濃縮操作及び膜蒸留分離器３３による希釈作業媒体Ｂの濃縮を連続的に実行できる。 During the concentration operation of the stock solution by the osmotic pressure generator 31, the diluted working medium B stored in the diluted working medium tank 32 is diluted with the diluted working medium circulation system including the third chamber 53 of the membrane distilled separator 33 and the membrane distilled separator 33. Concentration operation is performed by the pure water circulation cooling system including the fourth chamber 54, and the water (pure water) sent to the concentration working medium tank 34 and moved to the fourth chamber 54 is sent out from the second pure water tank 72 and collected. Is done. That is, the concentration operation of the stock solution by the osmotic pressure generator 31 and the concentration of the diluted working medium B by the membrane distillation separator 33 can be executed continuously.
それ故、産業廃水等の原液（被処理水Ａ）の濃縮処理及び水の回収を効率的に実施し得る、低コストにて運転可能な濃縮システム３００を提供できる。 Therefore, it is possible to provide a concentration system 300 that can be operated at a low cost and can efficiently perform a concentration process of a stock solution (treated water A) such as industrial wastewater and a recovery of water.
なお、図４に示す濃縮システム３００において、浸透圧発生器は第１処理容器４１を浸透膜により水平方向に区画して第１チャンバー４３、第２チャンバー４４を形成したが、第１処理容器を浸透膜により上下に区画して第１チャンバー４３、第２チャンバー４４を形成してもよい。 In the concentration system 300 shown in FIG. 4, the osmotic pressure generator forms the first chamber 43 and the second chamber 44 by partitioning the first processing container 41 in the horizontal direction by the osmosis membrane. The first chamber 43 and the second chamber 44 may be formed by dividing them vertically with a permeable membrane.
図４に示す濃縮システム３００において、浸透圧発生器３１の第１チャンバー４３内の濃縮された被処理水Ａ（例えば原液）をパイプライン２０１ｂを通して外部に送出、回収したが、より高濃度に濃縮された原液を得る場合には、パイプライン２０１ｂを被処理水タンク４５に接続して被処理水タンク４５、パイプライン２０１ａ、浸透圧発生器３１の第１チャンバー４３及びパイプライン２０１ｂのループを作ってもよい。この場合、浸透圧発生器３１における濃縮された原液と濃縮作業媒体Ｂの間の浸透圧差を考慮して原液の濃縮度合を決定することが望ましい。 In the concentration system 300 shown in FIG. 4, the concentrated water to be treated A (for example, a stock solution) in the first chamber 43 of the osmotic pressure generator 31 is sent out and recovered through the pipeline 201b, but is concentrated to a higher concentration. When the obtained stock solution is obtained, the pipeline 201b is connected to the water tank 45 to be treated to form a loop of the water tank 45, the pipeline 201a, the first chamber 43 of the osmotic pressure generator 31, and the pipeline 201b. May be. In this case, it is desirable to determine the concentration degree of the stock solution in consideration of the osmotic pressure difference between the concentrated stock solution and the concentrated working medium B in the osmotic pressure generator 31.
図４に示す濃縮システム３００において、膜蒸留分離器３３の脱水膜５２は多孔質ラテックス膜に限らず、蒸気を透過する機能を有するものであれば如何なるものでもよい。 In the concentration system 300 shown in FIG. 4, the dehydration membrane 52 of the membrane distillation separator 33 is not limited to the porous latex membrane, and may be any device as long as it has a function of transmitting vapor.
図４に示す濃縮システム３００において、希釈作業媒体Ｂの濃縮は脱水膜５２を備える膜蒸留分離器３３で行なう場合に限らず、希釈作業媒体Ｂの水を除去するものであれば如何なる装置で行なってもよい。 In the concentration system 300 shown in FIG. 4, the concentration of the diluted working medium B is not limited to being performed by the membrane distillation separator 33 including the dehydrating membrane 52, but may be performed by any apparatus that can remove the water of the diluted working medium B. May be.
（第４実施形態）
次に、第４実施形態に係る水処理システムの１つの例である循環型浸透圧発電システム４００を図５に示す概略図を参照して説明する。なお、図５において図４と同様な部材は同符号を付して説明を省略する。第４実施形態に用いられる作業媒体は、第１実施形態の作業媒体Ｂである。
(Fourth embodiment)
Next, a circulation type osmotic pressure power generation system 400 as an example of the water treatment system according to the fourth embodiment will be described with reference to a schematic diagram shown in FIG. In FIG. 5, the same members as those in FIG. The working medium used in the fourth embodiment is the working medium B of the first embodiment.
第４実施形態に係る水処理システムは、循環型浸透圧発電システムである。循環型浸透圧発電システム４００は、水流を発生させる浸透圧発生器３１と、浸透圧発生器３１で発生した水流で発電を行う回転体８２を備える。 The water treatment system according to the fourth embodiment is a circulation type osmotic pressure power generation system. The circulatory osmotic pressure power generation system 400 includes an osmotic pressure generator 31 that generates a water flow, and a rotating body 82 that generates power using the water flow generated by the osmotic pressure generator 31.
循環型浸透圧発電システム４００は、水を収容する第１チャンバー４３と、浸透圧を誘起する作業媒体Ｂ（ドロー溶液）を収容する第２チャンバー４４と、第１チャンバーと第２チャンバーとを区画する浸透膜４２と、第２チャンバー４４に接続された圧力交換器８１と、圧力交換器８１に接続された回転体８２とを備える。このような水処理システムによれば、第１チャンバー４３内の水と第２チャンバー４４内の作業媒体Ｂとの間で生じる浸透圧差により第１チャンバー４４内の水が浸透膜４２を透過して第２チャンバー４４内の作業媒体Ｂに移動する。水が作業媒体Ｂに移動することに伴う水流により回転体８２を回して発電する。 The circulation type osmotic pressure power generation system 400 divides a first chamber 43 for containing water, a second chamber 44 for containing a working medium B (draw solution) for inducing osmotic pressure, and a first chamber and a second chamber. And a pressure exchanger 81 connected to the second chamber 44, and a rotating body 82 connected to the pressure exchanger 81. According to such a water treatment system, the water in the first chamber 44 permeates the osmotic membrane 42 due to the osmotic pressure difference generated between the water in the first chamber 43 and the working medium B in the second chamber 44. Move to the working medium B in the second chamber 44. The rotating body 82 is rotated by the water flow accompanying the movement of the water to the working medium B to generate electric power.
第４実施形態は、作業媒体Ｂが実施形態の溶質を含む水溶液で、高い浸透圧の誘起作用を示す。このため、第１チャンバー４３内の水が浸透膜４２を透過して第２チャンバー４４内の作業媒体Ｂに移動する際、高い透過流束を発生させることができる。その結果、水が移動された作業媒体Ｂは高い圧力を持つ水流になるため、回転体８２をより高い速度で回して発電することができる。したがって、回転体８２を効率的に回転して発電し得る、低コストにて運転可能な水処理システムを提供できる。 In the fourth embodiment, the working medium B is an aqueous solution containing the solute of the embodiment, and exhibits a high osmotic pressure inducing action. For this reason, when the water in the first chamber 43 passes through the osmotic membrane 42 and moves to the working medium B in the second chamber 44, a high permeation flux can be generated. As a result, since the working medium B to which the water has been moved becomes a water stream having a high pressure, the rotating body 82 can be rotated at a higher speed to generate electric power. Therefore, it is possible to provide a water treatment system that can efficiently operate by rotating the rotating body 82 and can be operated at a low cost.
回転体８２は、例えばタービン、水車を用いることができる。 As the rotating body 82, for example, a turbine or a water turbine can be used.
循環型浸透圧発電システム４００は、浸透圧発生器３１の第２チャンバー４４が位置する第１処理容器４１の下部（作業媒体Ｂ出口側）に接続したパイプライン２０１ｂにおいて、圧力交換器８１及び回転体８２が作業媒体Ｂの流れ方向に沿ってこの順序で設けられている。また、第２チャンバー４４が位置する第１処理容器４１の上部と濃縮作業媒体タンク３４とを接続するパイプライン２０１ｃにおいて、第２ポンプ４７より作業媒体Ｂの流れ方向の下流側のパイプライン２０１ｃ部分が圧力交換器８１を経由して第２チャンバー４４が位置する第１処理容器４１の上部に接続されている。すなわち、浸透圧発生器３１において水が第１チャンバー４３から浸透膜４２を透過して第２チャンバー４４に移動したときに発生した流束を有する希釈作業媒体Ｂは、第２チャンバー４４が位置する第１処理容器４１の下部から圧力交換器８１が設けられたパイプライン２０１ｂを通して流出される。この間、濃縮作業媒体タンク３４から流出した濃縮作業媒体Ｂが流通するパイプライン２０１ｃは圧力交換器８１を経由する。このため、当該濃縮作業媒体Ｂは、圧力交換器８１で第２チャンバー４４から流出する希釈作業媒体Ｂと圧力交換され、希釈作業媒体Ｂは圧力を下げ、濃縮作業媒体Ｂは圧力を上昇する。 The circulation type osmotic pressure power generation system 400 includes a pressure exchanger 81 and a rotation in a pipeline 201b connected to a lower portion (working medium B outlet side) of the first processing container 41 where the second chamber 44 of the osmotic pressure generator 31 is located. The body 82 is provided in this order along the flow direction of the working medium B. Further, in the pipeline 201c that connects the upper part of the first processing vessel 41 where the second chamber 44 is located and the concentrated working medium tank 34, the pipeline 201c portion on the downstream side in the flow direction of the working medium B from the second pump 47 Is connected to the upper part of the first processing vessel 41 where the second chamber 44 is located via a pressure exchanger 81. That is, in the osmotic pressure generator 31, the second chamber 44 is located in the diluted working medium B having a flux generated when water passes from the first chamber 43 through the osmotic membrane 42 and moves to the second chamber 44. It flows out from the lower part of the 1st processing container 41 through the pipeline 201b in which the pressure exchanger 81 was provided. During this time, the pipeline 201 c through which the concentrated working medium B flowing out from the concentrated working medium tank 34 passes through the pressure exchanger 81. For this reason, the concentrated working medium B is pressure-exchanged with the diluted working medium B flowing out from the second chamber 44 by the pressure exchanger 81, the diluted working medium B decreases the pressure, and the concentrated working medium B increases the pressure.
なお、循環型浸透圧発電システム４００において、被処理水タンク４５内には水が収容される。 In the circulation type osmotic pressure power generation system 400, water is accommodated in the water tank 45 to be treated.
次に、図５に示す循環型浸透圧発電システム４００による発電操作を説明する。
第１ポンプ４６を駆動して水を被処理水タンク４５から浸透圧発生器３１の第１チャンバー４３内にパイプライン２０１ａを通して供給する。水の供給と前後して第２ポンプ４７を駆動して濃縮作業媒体Ｂを濃縮作業媒体タンク３４から浸透圧発生器３１の第２チャンバー４４内にパイプライン２０１ｃを通して供給する。第２チャンバー４４に供給された濃縮作業媒体Ｂは、第１チャンバー４３に供給された溶媒のみの水に対して十分に高濃度である。このため、第１チャンバー４３内の水と第２チャンバー４４内の濃縮作業媒体Ｂとの間で浸透圧差が生じ、水が浸透膜４２を透過して第２チャンバー４４内に移動する。このとき、第２チャンバー４４内の作業媒体Ｂは、実施形態の溶質を含む水溶液で、高い浸透圧の誘起作用を示す。このため、第１チャンバー４３内の水が浸透膜３２を透過して第２チャンバー４４内の作業媒体Ｂに移動する際、高い透過流束を発生する。その結果、第１チャンバー４３内の多くの水を第２チャンバー４４の濃縮作業媒体Ｂに移動でき、水により希釈された高い圧力を持つ希釈作業媒体Ｂが生成される。なお、第１チャンバー４３内の水はパイプライン２０１ｂを通して排出される。
Next, power generation operation by the circulation type osmotic pressure power generation system 400 shown in FIG. 5 will be described.
The first pump 46 is driven to supply water from the treated water tank 45 into the first chamber 43 of the osmotic pressure generator 31 through the pipeline 201a. Before and after the supply of water, the second pump 47 is driven to supply the concentrated working medium B from the concentrated working medium tank 34 into the second chamber 44 of the osmotic pressure generator 31 through the pipeline 201c. The concentrated working medium B supplied to the second chamber 44 has a sufficiently high concentration relative to the water of only the solvent supplied to the first chamber 43. For this reason, an osmotic pressure difference is generated between the water in the first chamber 43 and the concentrated working medium B in the second chamber 44, and the water passes through the osmotic membrane 42 and moves into the second chamber 44. At this time, the working medium B in the second chamber 44 is an aqueous solution containing the solute of the embodiment, and exhibits a high osmotic pressure inducing action. For this reason, when the water in the first chamber 43 passes through the osmotic membrane 32 and moves to the working medium B in the second chamber 44, a high permeation flux is generated. As a result, a large amount of water in the first chamber 43 can be moved to the concentrated working medium B in the second chamber 44, and a diluted working medium B having a high pressure diluted with water is generated. The water in the first chamber 43 is discharged through the pipeline 201b.
第２チャンバー４４の高い圧力を持つ希釈作業媒体Ｂは、希釈作業媒体タンク３２にパイプライン２０１ｄを通して送出され、貯留される。圧力交換器８１及び回転体８２がパイプライン２０１ｄに作業媒体Ｂの流れ方向に沿ってこの順序で設けられている。 The diluted working medium B having a high pressure in the second chamber 44 is sent to the diluted working medium tank 32 through the pipeline 201d and stored. The pressure exchanger 81 and the rotating body 82 are provided in this order along the flow direction of the working medium B in the pipeline 201d.
このため、前述したように圧力交換器８１では濃縮作業媒体タンク３４からパイプライン２０１ｃを通して流れる濃縮作業媒体Ｂと第２チャンバー４４から（回転体８２を通って）パイプライン２０１ｄを通して流れる高い圧力を持つ希釈作業媒体Ｂとの間で圧力交換がなされ、希釈作業媒体Ｂの圧力を下げ、濃縮作業媒体Ｂの圧力を上昇させる。圧力交換により適正な圧力を持つ希釈作業媒体Ｂは回転体８２に流れ、それを効率的に回転させて発電する。また、圧力交換により適正な圧力を持つ濃縮作業媒体Ｂは第２チャンバー４４に供給される。 For this reason, as described above, the pressure exchanger 81 has the concentrated work medium B flowing from the concentrated work medium tank 34 through the pipeline 201c and the high pressure flowing from the second chamber 44 (through the rotating body 82) through the pipeline 201d. The pressure is exchanged with the diluted working medium B, the pressure of the diluted working medium B is lowered, and the pressure of the concentrated working medium B is raised. The diluted working medium B having an appropriate pressure by pressure exchange flows into the rotating body 82 and efficiently rotates it to generate electric power. Further, the concentrated working medium B having an appropriate pressure is supplied to the second chamber 44 by pressure exchange.
希釈作業媒体タンク３２に貯留された希釈作業媒体Ｂは、前述した図４に示す濃縮システム３００と同様に膜蒸留分離器３３の第３チャンバー５３を含む希釈作業媒体循環系及び膜蒸留分離器３３の第４チャンバー５４を含む純水循環冷却系によって濃縮される。すなわち、第３チャンバー５３内で希釈作業媒体Ｂの水の蒸発、蒸気の脱水膜５２の透過、第４チャンバー５４への移動、及び第４チャンバー５４側での循環する純水による冷却、凝縮をなす脱水処理を複数回繰り返すことによって、希釈作業媒体Ｂを濃縮作業媒体Ｂとして使用し得る濃度の作業媒体Ｂ（濃縮作業媒体Ｂ）として循環タンク６４に貯留し、当該濃縮作業媒体Ｂを濃縮作業媒体タンク３４に戻す。濃縮作業媒体タンク３４内の濃縮作業媒体Ｂは、前述したように回転体８２を回転させて発電するために第２ポンプ４７を駆動して浸透圧発生器３１の第２チャンバー４４内に供給される。 The diluted working medium B stored in the diluted working medium tank 32 is diluted with the diluted working medium circulation system including the third chamber 53 of the membrane distillation separator 33 and the membrane distillation separator 33 in the same manner as the concentration system 300 shown in FIG. The pure water circulation cooling system including the fourth chamber 54 is concentrated. That is, evaporation of water of the diluted working medium B in the third chamber 53, permeation of the vapor dehydration film 52, movement to the fourth chamber 54, and cooling and condensation by circulating pure water on the fourth chamber 54 side. By repeating the dehydration process to be performed a plurality of times, the diluted working medium B is stored in the circulation tank 64 as a working medium B having a concentration that can be used as the concentrated working medium B (concentrated working medium B), and the concentrated working medium B is concentrated. Return to media tank 34. As described above, the concentrated working medium B in the concentrated working medium tank 34 is supplied into the second chamber 44 of the osmotic pressure generator 31 by driving the second pump 47 in order to generate electric power by rotating the rotating body 82. The
従って、浸透圧発生器３１による回転体８２の回転による発電操作及び膜蒸留分離器３３による希釈作業媒体Ｂの濃縮を連続的に実行できる。それ故、タービンなどの回転体８２を効率的に回転して発電し得る、低コストにて運転可能な循環型浸透圧発電システム４００を提供できる。 Therefore, the power generation operation by the rotation of the rotating body 82 by the osmotic pressure generator 31 and the concentration of the diluted working medium B by the membrane distillation separator 33 can be executed continuously. Therefore, it is possible to provide a circulation type osmotic pressure power generation system 400 that can efficiently generate power by rotating a rotating body 82 such as a turbine and that can be operated at low cost.
なお、図５に示す循環型浸透圧発電システム４００において、浸透圧発生器は第１処理容器を浸透膜により水平方向に区画して第１チャンバー４３、第２チャンバー４４を形成したが、第１処理容器を浸透膜により上下に区画して第１チャンバー４３、第２チャンバー４４を形成してもよい。 In the circulation type osmotic pressure power generation system 400 shown in FIG. 5, the osmotic pressure generator forms the first chamber 43 and the second chamber 44 by dividing the first processing container horizontally by the osmotic membrane. The first chamber 43 and the second chamber 44 may be formed by dividing the processing container up and down with a permeable membrane.
図５に示す循環型浸透圧発電システム４００において、浸透圧発生器３１の第１チャンバー４３内の水をパイプライン２０１ｂを通して外部に送出したが、パイプライン２０１ｂを被処理水タンク４５に接続して被処理水タンク４５、パイプライン２０１ａ、浸透圧発生器３１の第１チャンバー４３、パイプライン２０１ｂのループを作ってもよい。 In the circulation type osmotic pressure power generation system 400 shown in FIG. 5, the water in the first chamber 43 of the osmotic pressure generator 31 is sent to the outside through the pipeline 201b, and the pipeline 201b is connected to the water tank 45 to be treated. You may make the loop of the to-be-processed water tank 45, the pipeline 201a, the 1st chamber 43 of the osmotic pressure generator 31, and the pipeline 201b.
図５に示す循環型浸透圧発電システム４００において、膜蒸留分離器３３の脱水膜５２は多孔質ラテックス膜に限らず、蒸気を透過する機能を有するものであれば如何なるものでもよい。 In the circulatory osmotic pressure power generation system 400 shown in FIG. 5, the dehydration membrane 52 of the membrane distillation separator 33 is not limited to the porous latex membrane, and may be anything as long as it has a function of permeating vapor.
図５に示す循環型浸透圧発電システム４００において、希釈作業媒体Ｂの濃縮は脱水膜を備える膜蒸留分離器３３で行なう場合に限らず、希釈作業媒体Ｂの水を除去するものであれば如何なる装置で行なってもよい。 In the circulatory osmotic pressure power generation system 400 shown in FIG. 5, the concentration of the diluted working medium B is not limited to being performed by the membrane distillation separator 33 provided with a dehydrating membrane, and any method can be used as long as it removes water from the diluted working medium B. You may carry out with an apparatus.
以下、実施例を説明する。 Examples will be described below.
正浸透試験は以下の通り行った。ＦＯセルにＨＴＩ社製ＣＴＡ−ＥＳ膜をセットし、膜の活性面側に被処理水として純水を入れ、その後、支持層側に作業媒体を入れた。作業媒体を入れ終わった時間を０分とし、２０分静置した。試験後、活性面側の液体の重量を測定し、液体の比重を１として試験前後の差分から透過流束（Ｊｗ）を算出した。また、試験後の活性面側の液体中の全有機炭素濃度を全有機炭素計で、陽イオン濃度をイオンクロマトグラフで測定し、溶質の損失（Ｊｓ）を算出した。作業媒体に含まれる溶質とその濃度及び実験結果を表１に示す。 The forward osmosis test was conducted as follows. A CTA-ES membrane manufactured by HTI was set in the FO cell, pure water was added as treated water to the active surface side of the membrane, and then a working medium was placed on the support layer side. The time when the working medium was put in was set to 0 minutes, and allowed to stand for 20 minutes. After the test, the weight of the liquid on the active surface side was measured, and the permeation flux (Jw) was calculated from the difference before and after the test with the specific gravity of the liquid being 1. Further, the total organic carbon concentration in the liquid on the active surface side after the test was measured with a total organic carbon meter, the cation concentration was measured with an ion chromatograph, and the solute loss (Js) was calculated. Table 1 shows the solute contained in the working medium, its concentration, and the experimental results.
表１から明らかなように複数のホスホン酸基を含む化合物をドロー溶液に用いた実施例１〜７は一般に用いられる無機塩に対して溶質の損失が非常に小さい。また、カルボン酸基を有するナトリウム塩を溶質に用いた比較例では、Js/Jwが実施例に対して劣っている。かかる特性を有する作業媒体を使用することで、浸透圧を利用した水処理システムのランニングコストを小さくすることができる。また、これらの浸透圧作用によって生じる水流を用いて発電することで、低コストに発電をすることができる。
明細書中、一部の元素は、元素記号のみで表している。
As is apparent from Table 1, Examples 1 to 7 using a compound containing a plurality of phosphonic acid groups in the draw solution have a very small loss of solute with respect to generally used inorganic salts. Moreover, in the comparative example using the sodium salt which has a carboxylic acid group as a solute, Js / Jw is inferior to an Example. By using a working medium having such characteristics, the running cost of the water treatment system using osmotic pressure can be reduced. Moreover, it can generate electric power at low cost by generating electric power using the water flow produced by these osmotic pressure actions.
In the specification, some elements are represented only by element symbols.
本発明のいくつかの実施形態を説明したが、これらの実施形態は、例として提示したものであり、発明の範囲を限定することは意図していない。これら新規な実施形態は、その他の種々の形態で実施されることが可能であり、発明の要旨を逸脱しない範囲で、種々の省略、置き換え、変更を行うことができる。これら実施形態やその変形は、発明の範囲や要旨に含まれるとともに、特許請求の範囲に記載された発明とその均等の範囲に含まれる。 Although several embodiments of the present invention have been described, these embodiments are presented by way of example and are not intended to limit the scope of the invention. These novel embodiments can be implemented in various other forms, and various omissions, replacements, and changes can be made without departing from the scope of the invention. These embodiments and modifications thereof are included in the scope and gist of the invention, and are included in the invention described in the claims and the equivalents thereof.
Ａ…被処理水、
Ｂ…作業媒体、
Ｃ…水
１、３１…浸透圧発生器、
２、３２…希釈作業媒体タンク、
３…逆浸透膜分離器、
４、３４…濃縮作業媒体タンク、
１１、４１…第１処理容器、
１２、４２…浸透膜、
１３、４３…第１チャンバー、
１４、４４…第２チャンバー、
１５、４５…被処理水タンク、
１６…第１ポンプ、
１７…第２ポンプ、
２１、５１…第２処理容器、
２２…逆浸透膜（ＲＯ膜）、
２３、５３…第３チャンバー、
２４、５４…第４チャンバー、
２５…第３ポンプ、
２６…純水タンク、
２７…開閉弁、
３３…膜蒸留分離器、
５２…脱水膜、
６１…第１開閉弁、
６２…熱交換器、
６４…循環タンク、
６５…第２開閉弁、
６６…第４ポンプ、
７１…第１純水タンク、
７２…第２純水タンク、
７３…第３開閉弁、
７４…第５ポンプ、
７５…第４開閉弁、
８１…圧力交換器、
８２…回転体、
１００…水処理システム、
１０１…パイプライン、
２００…脱塩システム、
２０１…パイプライン、
３００…濃縮システム３００、
４００…循環型浸透圧発電システム
A ... treated water,
B ... Working medium,
C ... water 1, 31 ... osmotic pressure generator,
2, 32 ... Dilution working medium tank,
3 ... Reverse osmosis membrane separator,
4, 34 ... Concentrated working medium tank,
11, 41 ... 1st processing container,
12, 42 ... osmotic membrane,
13, 43 ... first chamber,
14, 44 ... second chamber,
15, 45 ... treated water tank,
16 ... first pump,
17 ... second pump,
21, 51 ... second processing vessel,
22 ... Reverse osmosis membrane (RO membrane),
23, 53 ... the third chamber,
24, 54 ... the fourth chamber,
25 ... the third pump,
26 ... pure water tank,
27: On-off valve,
33 ... Membrane distillation separator,
52 ... dehydration membrane,
61 ... 1st on-off valve,
62 ... heat exchanger,
64 ... circulation tank,
65 ... second on-off valve,
66 ... Fourth pump,
71 ... the first pure water tank,
72 ... the second pure water tank,
73 ... third on-off valve,
74 ... Fifth pump,
75 ... Fourth on-off valve,
81 ... pressure exchanger,
82 ... Rotating body,
100 ... water treatment system,
101 ... Pipeline,
200 ... desalination system,
201 ... pipeline,
300 ... Concentration system 300,
400 ... Circulation type osmotic pressure power generation system
Claims (10)
前記作業媒体が主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基のアンモニウム塩構造を有する化合物、又は、主鎖、側鎖、若しくは主鎖及び側鎖にホスホン酸基の金属塩構造を有する化合物を溶質として含む水溶液である水処理システム。 A first treatment container having a osmosis membrane for partitioning a first chamber containing water to be treated and a second chamber containing a working medium for inducing osmotic pressure;
The working medium is a main chain, a side chain, or a compound having an ammonium salt structure of a phosphonic acid group in the main chain and side chain, or a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain The water treatment system which is the aqueous solution which contains the compound which has this as a solute.
前記Ｍは、アルカリ金属又はアルカリ土類金属であり、ｘ、ｙ、ｚ、ｗ、ｒ、ｓ、ｔとｕは、２≦ｘ≦９、８≦ｙ≦２８、１≦ｚ≦６、３≦ｗ≦１８、０≦ｒ≦３、０≦ｓ≦１、０≦ｔ≦１、２≦ｕ≦１０を満たす請求項１に記載の水処理システム。 A compound having a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain, and a compound having an ammonium salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain, is represented by C x H y P z O w N r Cl s Br t M u,
M is an alkali metal or alkaline earth metal, and x, y, z, w, r, s, t, and u are 2 ≦ x ≦ 9, 8 ≦ y ≦ 28, 1 ≦ z ≦ 6, 3 The water treatment system according to claim 1 satisfying ≦ w ≦ 18, 0 ≦ r ≦ 3, 0 ≦ s ≦ 1, 0 ≦ t ≦ 1, 2 ≦ u ≦ 10.
前記式（１）のＸ１、Ｘ２とＸ３は、Ｈ、−（ＣＨ２）ｍ１ＰＯ（ＯＨ）２（ｍ１が１から３の整数のいずれか）からなる群から選ばれる１種以上であり、
前記式（２）のＹ１とＹ２は、ＯＨ、ＣＨ３、Ｃｌ、ＢｒとＣＨ２ＣＨ２ＮＨ２からなる群から選ばれる１種以上であり、
前記式（３）のＺ１、Ｚ２、Ｚ３とＺ４は、Ｈ、−（ＣＨ２）ｍ２ＰＯ（ＯＨ）２（ｍ２が１から３の整数のいずれか）、−（ＣＨ２）ｍ３Ｎ（（ＣＨ２）ｍ４ＰＯ（ＯＨ）２）２（ｍ３が１から３の整数のいずれか、ｍ４が１から３の整数のいずれか）からなる群から選ばれる１種以上である請求項１ないし３のいずれか１項に記載の水処理システム。
X 1 , X 2 and X 3 in the formula (1) are one selected from the group consisting of H, — (CH 2 ) m1 PO (OH) 2 (m 1 is any one of 1 to 3). That's it,
Y 1 and Y 2 in the formula (2) are at least one selected from the group consisting of OH, CH 3 , Cl, Br and CH 2 CH 2 NH 2 ;
Z 1 , Z 2 , Z 3 and Z 4 in the formula (3) are H, — (CH 2 ) m 2 PO (OH) 2 (m 2 is any integer of 1 to 3), — (CH 2 ) M3 N ((CH 2 ) m4 PO (OH) 2 ) 2 (one or more selected from the group consisting of m 3 is any integer from 1 to 3, and m 4 is any integer from 1 to 3) The water treatment system according to any one of claims 1 to 3.
前記浸透圧の誘起によって、水流が生じ、
前記水流によって前記回転体を回転させて発電する水処理システム。 The water treatment system according to any one of claims 1 to 6, further comprising a rotating body,
Due to the induction of the osmotic pressure, a water flow is generated,
A water treatment system for generating electricity by rotating the rotating body by the water flow.
前記式（１）のＸ１、Ｘ２とＸ３は、Ｈ、−（ＣＨ２）ｍ１ＰＯ（ＯＨ）２（ｍ１が１から３の整数のいずれか）からなる群から選ばれる１種以上であり、
前記式（２）のＹ１とＹ２は、ＯＨ、ＣＨ３、Ｃｌ、ＢｒとＣＨ２ＣＨ２ＮＨ２からなる群から選ばれる１種以上であり、
前記式（３）のＺ１、Ｚ２、Ｚ３とＺ４は、Ｈ、−（ＣＨ２）ｍ２ＰＯ（ＯＨ）２（ｍ２が１から３の整数のいずれか）、−（ＣＨ２）ｍ３Ｎ（（ＣＨ２）ｍ４ＰＯ（ＯＨ）２）２（ｍ３が１から３の整数のいずれか、ｍ４が１から３の整数のいずれか）からなる群から選ばれる１種以上である請求項９に記載の作業媒体。
A compound having a metal salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain, and a compound having an ammonium salt structure of a phosphonic acid group in the main chain, side chain, or main chain and side chain are The compound having the structure represented by formula (1), (2) or (3) is a compound in which the phosphonic acid group has an ammonium salt structure or the phosphonic acid group has a metal salt structure,
X 1 , X 2 and X 3 in the formula (1) are one selected from the group consisting of H, — (CH 2 ) m1 PO (OH) 2 (m 1 is any one of 1 to 3). That's it,
Y 1 and Y 2 in the formula (2) are at least one selected from the group consisting of OH, CH 3 , Cl, Br and CH 2 CH 2 NH 2 ;
Z 1 , Z 2 , Z 3 and Z 4 in the formula (3) are H, — (CH 2 ) m 2 PO (OH) 2 (m 2 is any integer of 1 to 3), — (CH 2 ) M3 N ((CH 2 ) m4 PO (OH) 2 ) 2 (one or more selected from the group consisting of m 3 is any integer from 1 to 3, and m 4 is any integer from 1 to 3) The working medium according to claim 9.
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| WO2016072461A1 (en) * | 2014-11-07 | 2016-05-12 | 株式会社 東芝 | Water treatment method, water treatment system, and water treatment device |
| CN105597540A (en) * | 2016-02-02 | 2016-05-25 | 华中科技大学 | Forward permeating absorbing fluid, application thereof, organic phosphine compound applied to forward permeating absorbing fluid and preparation method thereof |
| US20160288053A1 (en) * | 2013-07-01 | 2016-10-06 | Samsung Electronics Co., Ltd. | Draw solutes including phosphonate ionic oligomers, forward osmotic water treating apparatus, and methods using the same |
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| US20160288053A1 (en) * | 2013-07-01 | 2016-10-06 | Samsung Electronics Co., Ltd. | Draw solutes including phosphonate ionic oligomers, forward osmotic water treating apparatus, and methods using the same |
| WO2016072461A1 (en) * | 2014-11-07 | 2016-05-12 | 株式会社 東芝 | Water treatment method, water treatment system, and water treatment device |
| CN105597540A (en) * | 2016-02-02 | 2016-05-25 | 华中科技大学 | Forward permeating absorbing fluid, application thereof, organic phosphine compound applied to forward permeating absorbing fluid and preparation method thereof |
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