Patent Application
20110226695
The present invention relates to a method for producing fresh water to obtain freshwater from raw water using a reverse osmosis membrane or nano-filtration membrane (hereinafter, these are collectively called semi-permeable membrane), specifically to a method for producing fresh water capable of preventing performance deterioration of a reverse osmosis membrane and obtaining fresh water efficiently.
Being accompanied by deterioration of a water environment recent years, water treatment techniques have become more important than ever before. In particular, separation membranes have been adopted as a core of water treatment techniques because of their high separation accuracy. Above all, a reverse osmosis membrane and nano-filtration membrane capable of separating and removing ions have been utilized for removing hardness and harmful components of groundwater for producing water suitable for drinking, and have been applied to produce fresh water from seawater, so-called, “seawater desalination.” Ground water has been originally used as a water source clearer than surface water, but it is difficult to remove ion components and harmful chemical substances through clarification action obtained by infiltration in ground, so purification by a nano-filtration membrane or reverse osmosis membrane has been required resulting from environment contamination in recent years.
Meanwhile, seawater desalination has conventionally been in actual use mainly by thermal desalination in the Middle'East region where water resource is extremely few and heat resource of petroleum is very abundant, but in regions other than the Middle East where heat source is not abundant, a reverse osmosis method with high energy efficiency is adopted, and a number of plants have been constructed and actually operated in Caribbean islands and Mediterranean areas. Recently, improvement of reliability and cost-reduction thanks to technical advancement on the reverse osmosis method progress; even in the Middle East, a lot of seawater desalination plants based on the reverse osmosis method have been started in construction.
When seawater is directly passed through a reverse osmosis membrane, ordinarily from invasion of suspended solids, living organisms and the like contained in seawater, there arise troubles that the membrane surface is damaged, the membrane performance (permeability, rejection performance is deteriotated due to attachment on the membrane surface and the channel to the membrane is obstructed. Therefore, after seawater is clarified by various kinds of pre-treatments, it is generally supplied to a reverse osmosis membrane. As the pre-treatment method, there are sand filtration, coagulation sedimentation, dissolved air floatation, microfiltration membrane, ultrafiltration membrane and the like, thereby suspended solids and microbes can be fairly removed. However, since assimilable organic carbon (AOC) which can be foods to microbes cannot be completely removed even by the various kinds of pre-treatments; when operated for a long time, microbes gradually proliferate on the surface of a reverse osmosis membrane based on AOC contained in feed water, causing the foregoing trouble (this is called bio-fouling). Hence, scheduled removal of microbes (washing) becomes necessary.
As this scheduled washing method, intermittent cleaning with sodium hydrogen sulfite and a special bactericide (Non-patent document 1) and the like are listed. The method of sodium hydrogen sulfite has been conventionally adopted, but there is a case that proliferation of microbes is accelerated depending on situations (Non-patent documents 2 and 3). Although these antiseptic washes are carried out at a feed water side, microbes do not essentially permeate into a reverse osmosis membrane, in case where a reverse osmosis membrane is damaged, there is a risk that bactericides etc. leak into a permeate side. Thus, in a plant for an application of drinking water, washing is conducted using acid which does not cause any problem even in case that it is mixed into a permeate side (Non-patent document 1).
Washing using acid has a merit that washing can be carried out without modifying operation conditions during a continuous operation. The concentrate and permeate obtained during acid washing, except that they need to be neutralized to about pH 6 of a dischargeable level or quality of drinking water, do not contain harmful substances, so neutralization treatment with alkali is continuously conducted, thereby to obtain fresh water continuously, which is very efficient.
However, recently in seawater desalination, to satisfy a severe standard of water quality, a reverse osmosis two-step treatment that fresh water once subjected to reverse osmosis treatment is further treated by a low-pressure reverse osmosis membrane has become common; further, to satisfy a standard of water quality on boron, an alkali-adding two-step treatment that alkali is added to feed water in the second step of reverse osmosis membrane is often adopted (Patent document 2). In this case, alkali must be added to permeate of the reverse osmosis membrane in the first step to raise a pH to about 9 to 10 for example. However, in carrying out the foregoing acid washing, permeate of the first step is neutralized, and further alkali must be added by such amount that a pH of feed water in the second step can be raised. Further, since the pH of permeate and concentrate of the second step becomes high, acid needs to neutralize the high pH. Thus, there increase the amounts of acid and alkali necessary for pH adjustment in the first and second steps, respectively, which is not efficient, increasing desalination costs.
An object of the present invention is to provide a practical method for producing fresh water being capable of obtaining fresh water with high water quality efficiently and continuously, removing impure materials in water, particularly boron using a semi-permeable membrane unit.
The present invention to solve the above problems features the following (1) to (8).
20≦a×b≦30, a≧12
Herein, “raw water or pre-treated water obtained by pre-treatment of raw water” means water at an upstream from a first semi-permeable membrane unit, and “feed water” of the first or second permeable membrane unit means water at a time point when it is actually flowed into said semi-permeable Membrane unit. Additionally, it does not matter whether additives such as scale inhibitor are contained or not. In the case where part of feed water is recirculated to upstream from the first semi-permeable membrane unit, a mixed water of the recirculated water and raw water is also called raw water.
According to the present invention, in the case of having a plurality of desalination processes in parallel where raw water or pre-treated water obtained by pre-treatment of raw water is treated by a first semi-permeable membrane unit, and at least part of the resulting permeate of the first semi-permeable membrane unit of which pH is raised is treated in the second semi-permeable membrane unit as feed water of a second semi-permeable membrane unit, temporarily a pH of raw, water or pre-treated water in part of desalination process A to be supplied to a first semi-permeable membrane unit A1 is lowered and made a pH of the resulting permeate of said first semi-permeable membrane unit A1 lower than that of the feed water of a second semi-permeable membrane unit B2 in other desalination process B to be supplied to a second semi-permeable membrane unit A2, and the permeate obtained from the second semi-permeable membrane unit A2 is mixed with the permeate obtained from the second semi-permeable membrane unit B2 in said other desalination process B. Thus permeate with high water quality can be obtained from raw water efficiently and continuously; in particular, it is possible to obtain permeate with high water quality suitable for drinking that boron concentration is decreased from seawater, efficiently and continuously.
First, the basic flow of the method for producing fresh water according to the present invention will be described in reference to a pattern diagram shown in
The apparatus for producing fresh water shown in
At the upstream of the first semi-permeable membrane unit 8 and second semi-permeable membrane unit 15 constituting one desalination process 23, a high-pressure pump 7 and a booster pump 14 used for increasing the pressure of feed water of the respective semi-permeable membrane units are equipped, further, at the upstream of the first semi-permeable membrane unit 8, a dosing device of acid 6 for lowering a pH and at the upstream of the second semi-permeable membrane unit 15, a dosing device of alkali 13 for raising a pH are each equipped. At the concentrate (primary concentrate) 10 side of the first semi-permeable membrane unit 8, an energy recovery device 22 for recovering energy that the primary concentrate 10 has is equipped.
In such apparatus for producing fresh water, seawater 1, in response to its turbidity, as it is, or after pre-treatment is carried out by a pre-treatment device 2, is supplied to the first semi-permeable membrane unit 8 through the high-pressure pump 7. At this time, according to circumstances, to increase boron rejection factor of the first semi-permeable membrane unit 8, a scale inhibitor and alkali are added by a first dosing device of scale inhibitor 3 and a first dosing device of alkali 4.
In the first semi-permeable membrane unit 8, almost all solutes in seawater can be removed, permeate (primary permeate) 9 that solutes were removed of the first semi-permeable membrane unit 8 is sent to a second semi-permeable membrane unit 15. On the other hand, concentrate (primary concentrate) 10 of the first semi-permeable membrane unit 8 is discharged into sea etc. after pressure energy is recovered by an energy recovery device 22. Here, control of permeate flow volume of the first semi-permeable membrane unit 8 can be conducted by adjusting the output of high-pressure pump 7, and also by a flow volume control valve of concentrate 11. Regarding pressure energy recovery, it is generally applied only to a first semi-permeable membrane unit from the point of cost performance, but it may be no problem to recover energy by which an energy recovery device is equipped at concentrate 17 side to a second semi-permeable membrane unit.
Subsequently, according to circumstances, a scale inhibitor is added to the primary permeate 9 by a second dosing device of scale inhibitor 12; after pH thereof is raised higher than a pH of feed water of the first semi-permeable membrane unit 8 using a second dosing device of alkali 13, the pressure is raised by a booster pump 14 and the permeate is supplied to a second semi-permeable membrane unit 15. In the second semi-permeable membrane unit 15, solutes are further removed from feed water, thereby to obtain a secondary permeate 16 with a very high water quality.
Herein, as a place for adding a scale inhibitor to feed water of the second semi-permeable membrane unit 15 using the second dosing device of scale inhibitor 12, it is preferably at an upstream from a second dosing device of alkali 13 to prevent deposition of scale in the vicinity of an alkali-adding port of a second dosing device of alkali 13.
Additionally, according to need, it is preferable that a mixing tank and an in-line mixer are equipped to promote mixing at the downstream side of dosing of scale inhibitor and alkali.
In the case where water quality of primary permeate 9 is good, as exemplified in
The secondary permeate 16 is alone or mixed with the primary permeate, then, the pH is lowered by a pH adjustment device 19; after a component adjustment such as dosing of lime is conducted by a post-treatment device 20 to adjust components, it is stored in a product water tank 21.
On the other hand, the concentrate (secondary concentrate) 17 of the second semi-permeable membrane unit 15 is discharge into sea etc. In the second semi-permeable membrane unit, since the primary permeate 9 is used as feed water (water to be treated) of the second semi-permeable membrane unit 15, alkali and a scale inhibitor are added to the feed water as needed, suspended solids and the like are sufficiently removed being clear; however, there are many cases that pH becomes high due to dosing of alkali. Therefore, when the secondary concentrate 17 is discharged, it is preferable to be discharged after pH adjustment according to situations. In such case, in the present invention, since concentrate of lines carrying out acid washing is acidic, dosing of acid necessary for pH adjustment is preferably reduced by mixing concentrates discharged from each desalination process and flow them out.
Further, in the present invention, as shown in
As shown in
Here, in the present invention, while a process for producing fresh water have a plurality of desalination processes 23 in parallel treating permeate of a first semi-permeable membrane unit 8 of which a pH is raised with a second semi-permeable membrane unit 15, temporarily, the pH of raw water or pre-treated water for part of desalination processes (for example, 23a) is lowered and supplied to the first semi-permeable membrane unit 8. Thereby, it becomes possible to desalinate continuously while carrying out acid washing of the part of desalination processes (for example, 23a). When the process of this acid washing is conducted sequentially with a suitable delay in the whole desalination processes, it becomes possible to carrying out acid washing of the whole desalination processes while producing fresh water.
In the present invention, while treating by a second semi-permeable membrane unit 15 through raising a pH of permeate of a first semi-permeable membrane unit 8, a pH of permeate of the first semi-permeable membrane unit 8 in the part of processes carrying out acid washing (for example, 23a) is made lower than that of feed water of a second semi-permeable membrane unit 15 in other desalination processes not carrying out acid washing (for example, 23b to 23n), the permeate is supplied to the second semi-permeable membrane unit 15, and also the permeate obtained from the second semi-permeable membrane unit 15 is mixed with the permeates obtained from the second semi-permeable membrane unit 15 in other desalination processes not carrying out acid washing (for example, 23b to 23n). Namely, the acid input for washing in the part of desalination processes (for example, 23a) is used to neutralize the alkali input for removal of boron in other desalination processes (for example, 23b to 23n). Therefore, an acid input for washing in the part of desalination processes (for example, 23a) and an alkali input for removal of boron in other desalination processes (for example, 23b to 23n) are not needed to do be neutralized each independently, so it is efficient because the absolute amount of acid and alkali for a pH adjustment can be greatly reduced.
Hereinafter, regarding a specific flow in washing, the case where washing of desalination process 23a is conducted in
Here, the pH of permeate 9 of the first semi-permeable membrane unit 8 (first semi-permeable membrane unit A1) in the desalination process 23a that acid is being added to raw water is lower than usual. However, in the present invention, when the permeate 9 of the first semi-permeable membrane unit 8 (first semi-permeable membrane unit A1) of which pH became lower than usual is supplied to a second semi-permeable membrane unit 15 (second semi-permeable membrane unit A2), no alkali is added. Namely, in the desalination process 23a carrying out acid washing, the operation of the second dosing device of alkali 13 is stopped. However in the present invention, permeate 16 of the second semi-permeable membrane unit (second semi-permeable membrane unit A2) in the desalination process 23a carrying out acid washing and permeate 16 of a second semi-permeable membrane unit (second semi-permeable membrane unit B2) in other desalination processes 23b to 23n (other desalination process B) carrying out alkali dosing before being supplied to the second semi-permeable membrane unit 15 are mixed; thereafter, according to need, which is adjusted by a pH adjustment device 19 to a pH suitable for product water. As the result, the amount of acid and alkali needed by pH adjustment device 19 can be decreased remarkably.
Additionally, it is preferable not to conduct pH adjustment by the pH adjustment device 19 as much as possible. Namely, pH fluctuation in post-treatment is taken into consideration, a pH of a mixed water of permeate 16 of the second semi-permeable membrane unit (second semi-permeable membrane unit A2) in the desalination process 23a (part of desalination A) carrying out acid washing and permeate 16 of the second semi-permeable membrane unit (second semi-permeable membrane unit B2) in other desalination processes 23b to 23n (other desalination process B) not carrying out acid washing is preferably set to a target value. Specifically, in the case where a pH rises when a mineral is added in post-treatment, it is preferable that the pH of the mixed water is set to be low by just that much. For example, this can be carried out by adjustment of the total number of desalination processes disposed in parallel, and the amount of acid added (namely, pH adjustment of feed water of the first semi-permeable membrane unit 8, pH adjustment (adjustment of alkali dosing) of feed water of the second semi-permeable membrane unit 15 in an ordinary operation) and like.
Feed water of the second semi-permeable membrane unit 15 (second semi-permeable membrane unit A2) in the desalination process carrying out acid washing (part of desalination process A) is not added with alkali, thus boron rejection factor deteriorates compared to an ordinary operation that alkali is added. Therefore, to make the influence as low as possible, it is preferable for the number (a) of the desalination processes and an operating time (b) for lowering a pH of feed water of the first semi-permeable membrane unit to satisfy the following:.
20≦a×b≦30, a≧12
Additionally, the influence on the quality of product water due to inferior boron rejection performance in the desalination process carrying out acid washing (part of desalination process A), in other words the process that alkali is not added to feed water of the second semi-permeable membrane unit, generally does not often pose a problem because the number of processes carrying out acid washing is few compared to that of the whole desalination processes. However, in the case where it needs to compensate the lowering of the quality of product water during acid washing, the boron rejection factor is increased by increasing the amount of alkali added in an ordinary operation process (other desalination process B) that alkali is added, and by mixing with permeate during carrying out acid shock, it is possible to obtain product water with the same boron concentration as the case not carrying out acid washing.
Meanwhile, as described above, at the upstream of the first semi-permeable membrane unit 8, according to need, there are provided a first dosing device of scale inhibitor 3 that add a scale inhibitor to raw water of the first semi-permeable membrane unit 8 and a first doing device of alkali 4 that add an alkali to raise a pH of raw water of the first semi-permeable membrane unit 8. Also according to, need, at the upstream of the second semi-permeable membrane unit 15, there is provided a second dosing device of scale inhibitor 12 that add a scale inhibitor to feed water of the second semi-permeable membrane unit 15 (primary permeate 9). The first dosing device of alkali 4 is not essential for carrying out the present invention; but for example, when alkali is added to only the second semi-permeable membrane unit 15 for removing boron, in particular, scale tends to precipitate. Therefore, when alkali is added to raw water of the second semi-permeable membrane unit 15 while alkali is added to raw water of the first semi-permeable membrane unit 8, there is an effect that a pH of the second semi-permeable membrane unit 15 can be suppressed relatively low. However, regarding dosing of alkali to the first semi-permeable membrane unit 8, the dosing amount increases because flow volume is large depending on places, which is demerit in cost. Further, in the present invention, acid is added to feed water of part of the first semi-permeable membrane unit 8 by the dosing device of acid 6; and so when alkali is added before that, acid required increases by just that much. Then, in the present invention, there is preferably adopted a method where no alkali is added to feed water of the first semi-permeable membrane unit 8, or as exemplified in
In the present invention, as a method for lowering a pH of feed water of the first semi-permeable membrane unit 8, a method of dosing to a feed water line by a chemical dosing pump is a general one. In the process of the present invention, since mixing is conducted by a high-pressure pump, it is thought that no problem arises in mixing basically. However, it is possible to facilitate mixing by equipping a line mixer at a point after dosing or by equipping a mixing tank at a point of dosing. A method for lowering a pH is not particularly limited, but sulfuric acid is most preferably used from intensity of acid and easy handling. When seawater is used as raw water, it is preferable to set a pH of feed water of the first semi-permeable membrane unit 8 to be 4 or less capable of killing most fungi. The pH of permeate 9 of the first semi-permeable membrane unit 8 tends to be higher by about 1 than a pH of feed water in an acidic region. Also, as described below, in a desalination process where an ordinary operation is conducted without acid washing (other desalination process B), it is preferable to set a pH of feed water of the second semi-permeable membrane unit 15 to be 8 or more for improving boron rejection performance, 9 or more for obtaining further high effects. From considering these, it is preferable to set a pH of feed water of the first semi-permeable membrane unit 8 to be 4 or less based on the intention of the present invention that sequences of alkali dosing are neutralized by sequences of acid dosing.
Operation for lowering a pH is preferably 0.5 hours or more, 2.5 hours or less per day in one desalination process because it can suppress proliferation of microbes efficiently. When it is 0.5 hours or more, proliferation of microbes can be sufficiently suppressed, whereas when more than 2.5 hours, the proliferation suppressing effect reaches the limit. Therefore, when it is set to 2.5 hours or less, proliferation of microbes is prevented while preventing the lowering of quality of product water, and chemical costs for acid dosing can also be suppressed.
On the other hand, as a pH of feed water of the second semi-permeable membrane unit 15 in the desalination process where acid washing is not conducted (other desalination process B), it is preferably set to 8 or more for improving born rejection performance. To exhibit this effect further sufficiently, it is preferably set to 9 or more. Thereby it is possible to improve a rejection factor of a reverse osmosis membrane by ionizing boron that is not generally dissociated in seawater.
Operation for lowering a pH easily makes the water quality of product water stable over time by always conducting in the desalination processes which is changed sequentially, but an ordinary operation supplying raw water or pre-treated water to the first semi-permeable membrane unit 8 as it is without lowering the pH in all desalination processes may be carried out temporarily.
In the case of carrying out an ordinary operation that raw water or pre-treated water is supplied to the first semi-permeable membrane unit 8 as it is without lowering the pH in all desalination processes temporarily, during which acid washing is carried out in part of desalination processes (desalination process A), it is preferable to set for a pH of feed water of the second semi-permeable membrane unit 15 in the desalination process that acid washing is not conducted (other desalination process B) to be higher than a pH of feed water of the second semi-permeable membrane unit 15 in the ordinary operation (other desalination process B2). By so doing, it is possible to make boron concentration of the permeate obtained from the desalination process that acid washing is not conducted (other desalination process B) low; and by mixing the permeate having a high boron concentration obtained from the desalination processes carrying out acid washing (desalination process A) with the permeate having a low boron concentration, it is possible to maintain the boron concentration without deteriorating the boron concentration of permeate after mixing. In this time, a desalination process for raising a pH of feed water of the second semi-permeable membrane unit 15 may be the whole of desalination processes that acid washing is not carried out, or may be part thereof.
As exemplified in
As alkali added in a first dosing device of alkali 4 and a second dosing device of alkali 13, sodium hydroxide, calcium hydroxide, potassium hydroxide, sodium bicarbonate, ammonium hydroxide and the like can be exemplified, which is not particularly restricted. However, to prevent an increase in scale component into seawater, it is better not to use calcium or magnesium. The acceptable range of alkali dosing herein is suitably set depending on the alkali resistance of semi-permeable Membrane or an acceptable range till the generation of scale by adding alkali.
Additionally, being not shown in the figure, it is preferable that an in-line mixer is equipped right after the first dosing device of alkali 4 and the second dosing device of alkali 13, or a dosing port of alkali is directly contacted to the flow of seawater, thereby to prevent precipitation of scale at the dosing port. As a matter of course, it is also preferable to add a scale inhibitor to seawater before adding alkali as described above. The amount (concentration) of scale inhibitor added in the first semi-permeable membrane unit 8 and the second semi-permeable membrane unit 15 is generally determined by a condition where feed water of the semi-permeable membrane unit that scale most easily precipitates is most concentrated, namely, salt concentration, composition, temperature, pH, etc. in concentrate.
As a scale inhibitor added from a first dosing device of scale inhibitor 3 and a second dosing device of scale inhibitor 12, it may be the one that forms a complex with a metal, a metal ion or the like in solution to solubilize the metal or metal salt, and organic or inorganic ionic-polymers or monomers can be used. As the organic ionic polymer, there can be used synthetic polymers such as polyacrylic acid, sulfonated polystyrene, polyacrylamide and polyarylamine, natural polymers such as carboxymethyl cellulose, chitosan and alginic acid; and as monomers, ethylenediaminetetraacetate (EDTA) and the like. As the inorganic scale inhibitor, polyphosphate and the like can be used.
Among these scale inhibitors, polyphosphate and ethylenediaminetetraacetate are preferably used from the points of easy availability and easy handling such as solubility and price. Polyphosphate, being typified by sodium hexametaphosphate, is a polymerized inorganic phosphoric acid type substance that has two or more phosphor atoms in a molecule, an alkali metal and an alkaline metal are bonded with atoms of phosphoric acid, etc. As a typical polyphosphate, sodium tetrapyrophoshate, sodium dipyrophosphate, sodium tripolyphosphate, sodium tetrapolyphosphate, sodium heptapolyphosphate, sodium decapolyphosphate, sodium metaphosphate, sodium hexametaphosphate, and their potassium salts.
In the present invention, quality of feed water supplied to the first semi-permeable membrane unit 8 is preferably clean and has few deposition of fouling on a semi-permeable membrane. For this, first, water quality at an intake point is preferably good. When surface water is contaminated, percolating water such as groundwater is preferably used as raw water. Depending on water quality of raw water, it is preferable to conduct pre-treatment of raw water such as removal of suspended solid components and sterilization. By these treatments, it is possible to prevent the lowering of performance in the first semi-permeable membrane unit 8 and the second semi-permeable membrane unit 15, further subsequent processes, and to carry out a stable operation for a long period of time in treatment apparatus. A specific treatment may be suitably selected on the basis of a state of raw water such as seawater.
In the case where suspended solids need to be removed from raw water, applications of sand filtration, microfiltration membrane and ultrafiltration membrane are effective. In this case, when there are lots of microbes such as bacteria and fungi, disinfectant is preferably added. It is preferable to use chlorine to sterilize; for example, chlorine gas or sodium hypochlorite may be added to raw water in a range of 1 to 5 mg/l as free chlorine. In this case, there is a case that a specific disinfectant has no chemical durability depending on semi-permeable membranes; in such case, it is added preferably at an upstream side in the flow direction of feed water as possible, further it is preferable to invalidate the disinfectant in the vicinity at the inlet of raw water of the first semi-permeable membrane unit 8. For example, in sterilizing with free chlorine, the sterilization effect is exhibited by its oxidizing power. However, since it is known that free chlorine also oxidatively decomposes polymer substances constituting a semi-permeable membrane, it is preferable to invalidate the residual free chlorine not contributing to sterilization with a reducing agent (namely markedly weakening oxidizing power). Specifically, the concentration of free chlorine is measured, based on this measurement, the dosing amount of chlorine gas or sodium hypochlorite may be controlled, or a reducing agent such as sodium hydrogen sulfate may be added.
In the case where bacteria, proteins, natural organic components and the like are contained other than suspended solids, it is also effective to add an aggregating agent such as aluminum polychloride, aluminum sulfate and iron (III) chloride. The aggregated feed water is thereafter precipitated on a tilt board etc., followed by sand filtration or filtration by microfiltration membrane and ultrafiltration membrane that a plurality of hollow fiber membranes were bundled, thereby to be able to obtain feed water suitable for passing through a semi-permeable membrane in subsequent steps. In particular, in adding an aggregating agent, it is preferable to adjust pH for easy aggregation, generally; the pH is 5 or more, less than 8, and preferably less than 7.
Additionally, when pH is lowered in adding an aggregating agent, regarding a desalination process not carrying out acid washing (other desalination process B), boron rejection factor is lowered when pH is not raised before the first semi-permeable membrane unit 8; and so alkali is preferably added before the first semi-permeable membrane unit 8 for raising pH. In this manner, as a solute that varies the rejection performance by a pH change in the semi-permeable membrane unit, there is listed the one such as carbonic acid, nitric acid and silica whose dissociation degree changes by pH. By raising pH for these solutes, there rises the rejection ratio [%] (=100×(1-permeate concentration)/feed water concentration). Hence, to maintain the permeate concentration below a target concentration such as standard of water quality, alkali is preferably added as needed.
On the other hand, in the case where a lot of organic substances soluble in seawater are contained, the organic substances can be decomposed by adding chlorine gas or sodium hypochlorite, and they can also be removed by dissolved air floatation or activated carbon filtration. In the case where a lot of soluble inorganic substances are contained, a chelating agent such as organic polymer electrolyte and sodium hexametaphosphate may be added, or they may be exchanged with soluble ions using an ion exchange resin. When iron and manganese are present in a soluble state, it is preferable to use aeration oxidation filtration, contact oxidation filtration and the like.
Meantime, as raw water in the present invention, it is not particularly limited, including seawater, brine, river water, groundwater, drainage and their treated water. However, a two-step method for raising pH by adding alkali in the second step is in great need for removing high-concentration salts highly or removing boron highly. Therefore, water containing high-concentration salts such as seawater or treated water of seawater is preferably used as raw water in the present invention as well. Additionally, it is often said that seawater generally has the total salt concentration of 3% or more by weight, but there are cases that it is easily mixed with fresh water near the river mouth, and it becomes 4% or more by weight in seawater in the Middle East or an accumulated seawater, so it is not limited by the total salt concentration.
The high-pressure pump 4 is not particularly limited, and it can be suitably chosen depending on a necessary output. However, in the present invention, it is necessary to give feed water a pressure more than osmotic pressure; thus, in the case of seawater, it is preferably the one capable of providing a pressure of 3 MPa or more, further preferably 5 MPa or more. On the other hand, when a pressure markedly higher than osmotic pressure of raw water 1 to be supplied is given, it is not preferable because permeation flux at the inlet part of a first semi-permeable membrane becomes too large, and organic substances infinitesimally present in raw water precipitate and attach on the membrane surface, deteriorating membrane performances. Therefore, it is preferable to provide a pressure such that a differential permeation flux in the inlet part becomes 1 m3/m2·day or less, preferably 0.5 m3/m2·day or less. Additionally, the differential permeation flux can be obtained on the basis of the calculation formula described below.
Booster pump 13 is not particularly limited. Since it aims at supplying permeate of a first semi-permeable membrane and osmotic pressure hardly needs to be considered, it may be a low pressure and low flow volume compared to the high-pressure pump 5. As a specific pressure, it is preferably one capable of loading a maximum pressure of 2 MPa.
As a first semi-permeable membrane unit 8 and a second semi-permeable membrane unit 15, a fluid separation device (element) that a hollow fiber membrane or a flat sheet membrane is accommodated in a casing for easy handling can be used. In the case where this element is formed by a flat sheet membrane, as shown in
As a material for the semi-permeable membrane 30, there can be used polymer materials such as cellulose acetate type polymer, polyamide, polyester, polyimide and vinyl polymer. The membrane structure may be either an asymmetric membrane having a dense layer on at least one surface of the membrane, and micro-pores with gradually larger pore diameter toward the inside of the membrane or the other surface from the dense layer, or a composite membrane having a very thin functional layer formed by a different material on the dense layer of asymmetric membrane.
However, above all, a composite membrane composed of a functional layer made of polyamide having high pressure resistance and high permeability as well as a high solute rejection performance and an excellent potential is preferable. In, particular, when seawater is used as raw water, it is necessary to load a pressure higher than the osmotic pressure in the first semi-permeable membrane unit, and substantially an operation pressure of at least 5 MPa is often loaded. For maintaining high permeability and rejection performance against this pressure, suitable is a structure that polyamide is used as a functional layer, which is held by a support consisting of a porous membrane and unwoven cloth. As the polyamide semi-permeable membrane, it is suitably a composite semi-permeable membrane having a functional layer of crosslinked polyamide obtained by a polycondensation reaction of a multifunctional amine with a multifunctional acid halide as a support.
The functional layer is preferably the one which is made of crosslinked polyamide with a high chemical stability to acid or alkali, or consisting mainly of crosslinked polyamide. The crosslinked polyamide is formed by polycondensation of a multifunctional amine and a multifunctional acid halide, and it is preferable to contain a compound having a trifunctional group or more in at least one of the multifunctional amine and multifunctional acid halide components
Herein, a multifunctional amine means an amine having at least two primary and/or secondary amino groups in a molecule; for example, there can be listed aromatic multifunctional amines that two amino groups are bonded with benzene at any one of ortho, meta and para positional relations, such as phenylenediamine, xylenediamine; 1,3,5-triaminobenzene, 1,2,4-triaminobenzene and 3,5-diaminobenzoic acid; aliphatic amines such as ethylenediamine and propylenediamine; alicyclic multifunctional amines such as 1,2-diaminocyclohexane, 1,4-diaminocyclohexane, piperazine, 1,3-bispiperidylpropane and 4-aminomethylpiperazine, and the like. Above all, taking selective isolation, permeability of membrane and heat resistance into accounts, aromatic multifunctional amines are preferable, and as such aromatic multifunctional amines, m-phenylenediamine, p-phenylenediamine and 1,3,5-triaminobenze are preferably used. Further, from easy availability and easy handling, m-phenylenediamine (hereinafter denoted as m-PDA) is more preferably used. These multifunctional amines may be used alone or in a mixture thereof.
A multifunctional acid halide is an acid halide having at least two carbonyl halide groups in a molecule. For example, as a trifunctional halide, there can be listed trimesic acid chloride, 1,3,5-cyclohexane tricarboxylic acid chloride, 1,2,4-cyclobutane tricarboxylic acid chloride, and the like; as a difunctional halide, there can be listed aromatic difunctional acid halides such as biphenyldicarboxylic acid chloride, biphenylne carboxylic acid chloride, azobenzene dicarboxylic acid chloride, terephthalic acid chloride, isophthalic acid chloride and naphthalene dicarboxylic acid chloride; aliphatic difunctional acid halides such as adipoyl chloride and sebacoyl chloride; and alicyclic difunctional acid chlorides such as cyclopentane dicarboxylic acid dichloride, cyclohexane dicarboxylic acid dichloride, and tetrahydrofuran dicarboxylic acid dichloride. Taking reactivity with multifunctional amines into accounts, multifunctional acid halides are preferably multifunctional acid chlorides, and taking selective isolation of membrane and heat resistance into accounts, multifunctional aromatic acid chlorides are preferable. Above all, from the viewpoints of easy availability and easy handling, trimesic acid chloride is more preferably used. These multifunctional acid halides may be used alone or in a mixture thereof.
In the present invention, a semi-permeable membrane used in the first semi-permeable membrane unit 8 can desirably remove solutes such as ions and others in seawater highly. Particularly, in regard to boron whose rejection factor is low compared with other components, it is preferable to have a high boron rejection performance. Specifically, as a semi-permeable membrane used in the first semi-permeable membrane unit 8, fresh water with high quality of water can be obtained from seawater by adopting the one capable of exhibiting such performance that pure water permeability coefficient Lp, is 3×10−12 m3/m2·Pa·s or more and boron permeability coefficient Pb is 400×10−9 m/s or less when an artificial seawater having the total salt concentration of 3.5% by weight, pH of 7.0 and temperature of 25° C. is supplied by an operation pressure of 5.5 MPa.
Herein, artificial seawater having the total salt concentration of 3.5% by weight is the one prepared in a composition: NaCl=23.926 g/l, Na2SO4=4.006 g/l, KCl=0.738 g/l, NaHCO3=0.196 g/l, MgCl2=5.072 g/l, CaCl2=1.147 g/l, and H3BO3=0.0286 g/l.
The pure water permeability coefficient Lp and boron permeability coefficient Pb can be obtained by the following method taking into consideration a concentration polarization phenomenon occurring on the membrane surface. For example, when measured using a flat membrane, by means of a flat membrane cell shown in a document by M. Taniguchi et al. (Journal of Membrane Science, vol. No. 183, p 259-267, 2000 (hereinafter referred to Reference 1)), permeation flux Jv and TDS permeate concentration Cp of artificial seawater are measured, and Lp, Pb are calculated by the following formula.
J
v
=L
p(ΔP−Δπ)
L
s
=P(Cm−Cp)
J
sb
=P
b(Cmb−Cpb)
Δπ=π(Cm)−π(Cp)
(Cm−Cp)/(Cf−Cp)=exp(Jv/k)
(Cmb−Cp)/(Cfb−Cpb)=exp(Jv/kb)
Here, osmotic pressure it can be known by a so-called “Miyake's formula” shown in a document by M. Taniguchi et al. (AIChE Journal, vol. No. 46, p 1967-1973, 2000 (hereinafter referred to Reference 2)). TDS mass-transfer coefficient k is a value determined by an evaluation cell, but can be obtained by an osmotic method or flow velocity variation method shown in Reference 2 as a function of membrane surface flow volume Q [m3/s] or membrane flow rate u [m/s].
In the case of flat membrane cell shown in Reference 1,
k=1.63×10−3·Q0.4053
Subsequently, boron mass-transfer coefficient kb can be calculated as shown in the same document.
k/k
b=(D/Db)0.75
Hence, unknown quantities Lp, P, Pb, Cm and Cmb can be calculated from the above formulas. In the case of a membrane element, as shown in Reference 2, Lp and P can be calculated by fitting while integrating in the longitudinal direction of the membrane element.
The foregoing differential permeation flux is also explained. First, “differential” means a specific position in the longitudinal direction of this membrane element; by fitting in the above-described integration calculation, it can be precisely obtained by the profile in the longitudinal direction of this membrane element finally obtained. Here, in the case where a semi-permeable membrane having a sufficient rejection factor of 99% or more in salt rejection performance is used, TDS permeate concentration Cp is very small compared with TDS raw water bulk concentration Cf, and osmotic pressure π (Cp) can be neglected; thus, it can be calculated in the following manner.
Namely, the differential permeation flux Jv,IN can be obtained by solving a simultaneous equation of Jv,IN and Cm,IN using:
J
v,IN
=L
p(ΔPIN−ΔπIN)
Js,IN≈P(Cm,IN)
Δπ≈π(Cm)
C
m,IN
/C
f,IN=exp(Jv,IN/k)
To obtain a composite semi-permeable membrane suitable for the first semi-permeable membrane unit 8 having such a high boron rejection performance, for example, a method that an aliphatic acyl group is made present inside or on the surface can be mentioned. Specifically, for example, a functional layer substantially having separation performance of ions etc. is provided on the micro-porous support membrane substantially having no separation performance, and an aliphatic acyl group is made present inside the functional layer and/or on the surface of the functional layer. The aliphatic acyl group may be present in the functional layer or on the surface of the functional layer by bonding.
The method making an aliphatic acyl group present in the functional layer is not particularly limited. For example, an aliphatic acid halide solution is contacted with the surface of the functional layer formed by an interfacial polycondensation of a multifunctional amine and a multifunctional acid halide, or an aliphatic acid halide is concomitantly present in an interfacial polycondensation of a multifunctional amine and a multifunctional acid halide, thereby to make the group present in the functional layer through covalent bonding. Namely, in forming a polyamide functional layer on a micro-porous support membrane, a multifunctional amine aqueous solution, an organic solvent solution of an aliphatic acid halide, and an organic solvent solution of an aliphatic acid halide having carbon numbers of 1 to 4 different from this may be contacted on a micro-porous support membrane to be subjected to an interfacial polycondensation; or a multifunctional amine aqueous solution, a multifunctional acid halide, and an organic solvent solution containing an aliphatic acid halide having carbon numbers of 1 to 4 different from this may be contacted on a micro-porous support membrane to be subjected to an interfacial polycondensation.
An aliphatic acid halide preferably has carbon numbers of 1 to 4, and further preferably carbon numbers of 2 to 4. As the carbon number is larger, reactivity of an aliphatic acid halide becomes lower due to steric hindrance, access of a multifunctional acid halide to a reaction point becomes difficult, preventing a smooth membrane formation; thus, the performance of membrane deteriorates. As such aliphatic acid halide, there are listed methanesulfonyl chloride, acetyl chloride, propionyl chloride, butyryl chloride, oxalyl chloride, malonic acid dichloride, succinic acid dichloride, maleic acid dichloride, fumaric acid dichloride, chlorosulfonylacetyl chloride, N,N-dimethylaminocarbonyl chloride and the like. These may be used alone, or in 2 kinds or more at the same time; in order to have a balance that a membrane is made into a dense structure and permeability is not so lowered, it is preferable to consist mainly of oxalyl chloride.
The support containing a micro-porous support membrane is a layer which substantially has no separation performance, and provided to give a mechanical strength to a functional layer of crosslinkedpolyamide substantially having a separation performance. The one that a micro-porous support membrane is formed on a base material such as cloth or unwoven cloth is used.
The micro-porous support membrane is a layer which substantially has no separation performance, and provided to give a mechanical strength to a functional layer substantially having a separation performance. It has a uniform micro-pore or a gradually larger micro-pore from one surface to the other surface, and it is preferably a support membrane with a structure that the size of the micro-pore is 100 nm or less on the surface of one side.
The above-described support can be selected from various commercial materials such as “Millipore filter VSWP” (product name) manufactured by Millipore Corporation and “Ultrafilter UK10” (product name) manufactured by Toyo Roshi Co., Ltd.; but it can be generally produced in accordance with a method described in “Office of Saline Water Research and Development Progress Report” No. 359 (1968). As the material, there are ordinarily used homopolymers such as polysulfone, polyamide, polyester, cellulose acetate, cellulose nitrate and polyvinylchloride and their blend, but it is preferable to use polysulfone with high chemical, mechanical and thermal stabilities.
For example, a micro-porous support membrane having a micro-pore of several 10 nm or less in diameter on almost all surface is obtained as follows: a dimethylformamide (DMF) solution of the foregoing polysulfone is cast in a constant thickness onto a polyester cloth tightly woven or unwoven cloth, which is subjected to wet coagulation in an aqueous solution containing sodium dodecylsulfate of 0.5% by weight and DMF of 2% by weight. As the material of micro-porous support membrane, polyamide and polyester are also preferably used other than polysulfone.
The total dissolved solids concentration (TDS concentration) of permeate or feed water was obtained by measuring electric conductivity of each liquid by an electric conductivity meter (SC82 manufactured by Yokokawa Denki Co., Ltd.) and by the relationship between the concentration and electric conductivity of artificial seawater previously measured with an artificial seawater. pH measurement was measured using PH82 manufactured by Yokokawa Denki Co., Ltd.
Evaluation apparatus of flow (hereinafter referred to apparatus X) shown in
Apparatus X was constituted by a feed water tank 38, high-pressure pump 7, a first semi-permeable membrane unit 8, booster pump 14 and a second semi-permeable membrane unit 15. The high-pressure pump 8 is output-controlled by an inverter, the output of booster pump 14 is non-regulated, but pressure loaded in feed water of the second semi-permeable membrane unit 15 was substantially controlled by a pressure adjustment valve 45. The flow volume of permeate 9 of the first semi-permeable membrane unit 8 was made controllable by a flow control valve 11 of concentrate of first semi-permeable membrane unit 11, and the flow volume of permeate of the second semi-permeable membrane unit was made controllable by a pressure adjustment valve 45, valve 18 and back-pressure valve 47. As shown in
As an ordinary operation, seawater near an Ehime factory of Toray Industries Inc. was pre-treated by sand filtration to remove suspended solids, and the pre-treated seawater (TDS concentration 3.4% by weight, water temperature 22° C., pH=7.5) was treated by flow volume 80 m3/day using apparatus X. As a membrane element of a first semi-permeable membrane unit, SU-810 manufactured by Toray Industries Inc. was used; as a membrane element of a second semi-permeable membrane unit, SU-710 manufactured by Toray Industries Inc. was used. The operation was done by a recovery factor of 30% in the first semi-permeable membrane unit, and a recovery factor of 75% in the second semi-permeable membrane unit. Additionally, there was no dosing of scale inhibitor by a first dosing device of scale inhibitor 3, no dosing of alkali by a first dosing device of alkali 4, and no dosing of acid by a dosing device of acid 6. However, to improve boron rejection performance in the second semi-permeable membrane unit, NaOH was added by a second dosing device of alkali 13, and a pH of feed water of the second semi-permeable membrane unit 15 was set to 9.0. Further, scale inhibitor (SHMP, sodium hexametaphosphate) of 3 mg/l was added by a second dosing device of scale inhibitor 12, thereby to prevent the generation of scale due to alkali dosing. As a result of operation under this condition, the permeate flow volume was 18 m3/day, permeate TDS concentration was 1.1 mg/l, boron concentration was 0.19 mg/l, and pH of permeate was 9.2. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 0 g/hr, and the dosing amount of NaOH in the second dosing device of alkali 13 was 25 g/hr.
As a washing operation, the operation was done in the same condition as in Reference example 1 except that sulfuric acid was added by a dosing device of acid 6 before a first semi-permeable membrane unit 8, pH of feed water to the first semi-permeable membrane unit 8 was set to 3.0, there was no dosing of scale inhibitor by a second dosing device of scale inhibitor 12 before a second semi-permeable membrane unit 15, and no dosing of alkali by a second dosing device of alkali 13. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 1.5 mg/l, boron concentration was 0.25 mg/l, and pH of permeate was 4.5. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 530 g/hr, and the dosing amount of NaOH in the second dosing device of alkali was 0 g/day.
As a washing operation, the operation was done in the same condition as in Reference example 1 except that sulfuric acid was added by a dosing device of acid 6 before a first semi-permeable membrane unit 8, pH of feed water to the first semi-permeable membrane unit 8 was set to 3.0. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 1.1 mg/l, boron concentration was 0.19 mg/l, and pH of permeate was 9.2. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 530 g/hr, and the dosing amount of NaOH in the second dosing device of alkali was 120 g/hr.
As an ordinary operation, the operation was done in the same condition as in Reference example 1 except that pH of feed water of the second semi-permeable membrane unit 15 was set to 9.06. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 1.1 mg/l, boron concentration was. 0.184 mg/l, and pH of permeate was 9.26. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 0 g/hr, and the dosing amount of NaOH in the second dosing device of alkali 13 was 25.4 g/hr.
After a continuous operation for 3 months in the condition of Reference example 1, the operation was done in the same condition as in Reference example 1 except that as the pre-treated seawater at high temperature (TDS concentration 3.4% by weight, water temperature 27° C., pH=7.5), and pH of feed water of the second semi-permeable membrane unit 15 was set to 9.2. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.6 mg/l, boron concentration was 0.47 mg/l, and pH of permeate was 9.3. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 0 g/hr, and the dosing amount of NaOH in the second dosing device of alkali 13 was 26 g/hr.
As a washing operation, the operation was done in the same condition as in Reference example 5 except that sulfuric acid was added by a dosing device of acid 6 before a first semi-permeable membrane unit 8, and pH of feed water to the first semi-permeable membrane unit 8 was set to 3.0; there was no dosing of scale inhibitor by a second dosing device of scale inhibitor 12 before a second semi-permeable membrane unit 15, and no dosing of alkali by a second dosing device of alkali 13. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.9 mg/l, boron concentration was 0.67 mg/l, and pH of permeate was 4.6. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 520 g/hr, and the dosing amount of NaOH in the second dosing device of alkali was 0 g/day.
As a washing operation, the operation was done in the same condition as in Reference example 5 except that sulfuric acid was added by a dosing device of acid 6 before a first semi-permeable membrane unit 8, and pH of feed water to the first semi-permeable membrane unit 8 was set to 3.0. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.8 mg/l, boron concentration was 0.47 mg/l, and pH of permeate was 9.3. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 520 g/hr, and the dosing amount of NaOH in the second dosing device of alkali was 125 g/hr.
As an ordinary operation, the operation was done in the same condition as in Reference example 5 except that a pH of feed water of the second semi-permeable membrane unit 15 was set to 9.26. As a result, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.7 mg/l, boron concentration was 0.45 mg/l, and pH of permeate was 9.41. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 0 g/hr, and the dosing amount of NaOH in the second dosing device of alkali 13 was 27 g/hr.
As an ordinary operation, the operation was done in the same condition as in Reference example 8 except that 22 m3/day of the permeate flow volume of a first semi-permeable membrane unit of 24 m3/day was allotted to feed water of a second semi-permeable membrane unit 15, and a recovery factor was set to 72.7% so that the permeate flow volume of the second semi-permeable membrane unit was 16 m3/day. As a result, it was shown in the permeate of the second semi-permeable membrane unit that the TDS concentration was 2.6 mg/l, boron concentration was 0.44 mg/l, and pH of permeate was 9.41. With this permeate, 2 m3/day of the permeate of the first semi-permeable membrane unit (permeate TDS concentration 196 mg/l, boron concentration 1.0 mg/l, and pH=6.13) was mixed; as a result, the total water volume of mixed water was 18 m3/day, permeate TDS concentration was 24.0 mg/l, boron concentration was 0.50 mg/l, and pH was 8.7. In this case, the dosing amount of sulfuric acid in the dosing device of acid 6 was 0 g/hr, and the dosing amount of NaOH in the second dosing device of alkali 13 was 24.8 g/hr.
Assuming twelve machines shown in
It was calculated in the same condition as in Example 1 except that each desalination process undergoes the washing operation condition for lowering a pH explained in Reference example 3. As a result, the raw water volume summed up twelve desalination processes was calculated to be 960 m3/day and the permeate flow volume to be 216 m3/day, and as a result of that permeates of Reference example 1 and Reference example 3 were mixed by 11:1 as an average permeate in the twelve desalination processes, the permeate TDS concentration was 1.1 mg/l, and boron concentration was 0.190 mg/l, giving the almost same water quality as Example 1. In this case, it was calculated that the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 3 was 1060 g/day, and the dosing amount of NaOH in the second dosing device of alkali was 790 g/day, resulting in a consumption amount 1.4 times that in Example 1.
It was calculated in the same condition as in Example 1 except that Reference example 4 was adopted as an ordinary operation condition for permeate boron concentration after mixing to be the same as Comparative Example 1. As a result, the raw water volume summed up twelve desalination processes was calculated to be 960 m3/day and the permeate flow volume to be 216 m3/day, and as a result of that permeates of Reference example 4 and Reference example 2 were mixed by 11:1 as an average permeate in the twelve desalination processes, the permeate TDS concentration was 1.13 mg/l, and boron concentration was 0.190 mg/l, giving the same boron concentration as in Example 1. In this case, it was calculated that the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 1060 g/day, and the dosing amount of NaOH in the second dosing device of alkali was 559 g/day, resulting in the same consumption amount as in Example 1.
In assuming the same operation condition as in Example 1 except that Reference example 5 and Reference example 6 were adopted in place of Reference example 1 and Reference example 2. The raw water volume summed up twelve desalination processes was calculated to be 960 m3/day and the permeate flow volume to be 216 m3/day, and the average permeate TDS concentration of twelve desalination processes was as sufficiently low as 2.63 mg/l, and the average boron concentration was 0.488 mg/l. This result satisfied the WHO quality standard of drinking water (boron concentration of 0.5 mg/l). In this case, it was calculated that the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 1040 g/day, and the dosing amount of NaOH in the second dosing device of alkali was 572 g/day.
It was calculated in the same condition as in Example 3 except that the washing operation condition for lowering a pH explained in Reference example 7 was adopted in place of Reference example 6. As a result, the raw water volume summed up twelve desalination processes was calculated to be 960 m3/day and the permeate flow volume to be 216 m3/day; the average permeate TDS concentration of twelve desalination processes was 2.63 mg/l, and the boron concentration was 0.470 mg/l. In this case, it was calculated that the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 3 was 1040 g/day, and the dosing amount of NaOH in the second dosing device of alkali was 822 g/day, resulting in a consumption amount 1.4 times that in Example 3.
It was calculated in the same condition as in Example 3 except that Reference example 8 was adopted as an ordinary operation condition for permeate boron concentration after mixing to be the same as Comparative Example 2. As a result, the raw water volume summed up twelve desalination processes was calculated to be 960 m3/day and the permeate flow volume to be 216 m3/day; the average permeate TDS concentration of the twelve desalination processes was 2.72 mg/l, and the boron concentration was 0.470 mg/l. In this case, it was calculated that the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 1040 g/day, and the dosing amount of NaOH in the second dosing device of alkali was 594 g/day.
There was assumed a case that the number of desalination processes was 12, and acid washing time was 1 hour. In this case, the calculation was done assuming an operation that an ordinary operation without washing in all desalination processes was carried out for 12 hours in a day and one desalination process was subjected to acid washing in rotation for the residual 12 hours. Here, it was assumed that when all was in the ordinary operation, it was operated in the condition of Reference example 5 (namely, pH of feed water of the second semi-permeable membrane unit 15 was 9.2), and when washing was carried out in any one of desalination processes, it was operated in the condition of Reference example 4 (namely, pH of feed water of the second semi-permeable membrane unit 15 in an ordinary operation was raised to 9.26). As a result, through a day, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.6 to 2.72, and boron concentration was constant at 0.470 mg/l. It was able to obtain permeate with a constant boron concentration even during which washing was carried out in any one of desalination processes. In this case, the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 520 g/day, and the dosing amount of NaOH in the second dosing condition of alkali was 609 g/hr.
The calculation was done assuming an operation in the same condition as in Example 5 (namely, pH of feed water of the second semi-permeable membrane unit 15 was 9.2) except by operating in the same condition as in Comparative Example 2 during which acid washing was carried out in any one of desalination processes. As a result, through a day, the permeate flow volume was 18 m3/day, permeate TDS concentration was 2.6 to 2.8, and boron concentration was constant at 0.470 mg/l. It was able to maintain a constant boron concentration even during which washing was carried out in any one of desalination processes, in this case, the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 520 g/day, and the dosing amount of NaOH in the second dosing condition of alkali was 723 g/hr, which was larger than that of Example 5 by 19%.
There was assumed a case that the number of desalination processes was 12, and acid washing time was 1 hour. In this case, the calculation was done assuming an operation that an ordinary operation without washing in all desalination processes was carried out for 12 hours in a day and one desalination process was subjected to acid washing in rotation for the residual 12 hours. Here, the calculation was done assuming an operation that when all was in the ordinary operation, it was operated in the condition of Reference example 9 (namely, feed water volume of the second semi-permeable membrane unit 15 was 22 m3/day, bypass flow volume was 2 m3/day), and when it was operated during which washing was carried out in any one of desalination processes, in the condition of Reference example 9 for six lines of desalination processes carrying out an ordinary operation, in the condition of Reference example 8 for five lines (without bypassing), and in the condition of Reference example 6 for an acid washing line (without bypassing). As a result, through a day, it was shown in the total permeate that the flow volume was 18 m3/day, permeate TDS concentration was 13.4 to 24 mg/l, and boron concentration was almost constant at 0.495 to 0.50 mg/l. It was able to maintain a constant boron concentration satisfying the WHO water quality standard even during which washing was carried out in any one of desalination processes. In this case, the dosing amount of sulfuric acid per one desalination process in the dosing device of acid 6 was 520 g/day, and the dosing amount of NaOH in the second dosing condition of alkali was 581 g/hr.
Additionally, Table 1 shows the condition and result in Reference examples 1 to 9, and Table 2 shows the condition and result in Examples 1 to 6, and Comparative Examples 1 to 3.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2006-129875 | May 2006 | JP | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/JP2007/058233 | 4/16/2007 | WO | 00 | 6/10/2011 |
