JP7736293B2 - Method and apparatus for membrane treatment of solution - Google Patents
Method and apparatus for membrane treatment of solutionInfo
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Description
本発明は、溶液の膜処理方法および装置に関する。 The present invention relates to a method and apparatus for membrane treatment of a solution.
海水等の溶液を膜処理する方法として、特許文献１には、対象溶液を冷却する析出工程を経た対象溶液を半透膜モジュールの高圧室に供給し、高圧室を通過した対象溶液の一部を低圧室に供給することにより、高圧室の対象溶液に含まれる水を半透膜を介して低圧室に移行させ、高圧室の対象溶液を濃縮する方法が開示されている。 Patent Document 1 discloses a membrane treatment method for solutions such as seawater, in which the target solution, which has undergone a precipitation process in which it is cooled, is supplied to a high-pressure chamber of a semipermeable membrane module, and a portion of the target solution that has passed through the high-pressure chamber is supplied to a low-pressure chamber, causing water contained in the target solution in the high-pressure chamber to migrate to the low-pressure chamber via the semipermeable membrane and concentrating the target solution in the high-pressure chamber.
上記の膜処理方法は、析出工程で冷却された対象溶液を加温した後に半透膜モジュールに供給することで、飽和状態の成分が析出して半透膜の目詰まりが生じるのを防止している。 The above membrane treatment method prevents saturated components from precipitating and clogging the semipermeable membrane by heating the target solution cooled in the precipitation process before supplying it to the semipermeable membrane module.
ところが、対象溶液の加温後の温度は、析出工程で冷却する前の温度と同程度であるため、半透膜モジュールにおいて高濃縮を行うためには半透膜の膜面積を大きくする必要があり、半透膜モジュールの大型化および高コスト化を招くおそれがあった。 However, since the temperature of the target solution after heating is approximately the same as the temperature before cooling in the precipitation process, in order to achieve high concentration in the semipermeable membrane module, the membrane area of the semipermeable membrane needs to be increased, which could lead to an increase in the size and cost of the semipermeable membrane module.
そこで、本発明は、溶液の高濃縮を低コストで効率良く行うことができる溶液の膜処理方法および装置の提供を目的とする。 The present invention aims to provide a membrane treatment method and apparatus for a solution that can efficiently and inexpensively concentrate the solution.
本発明の前記目的は、半透膜により仕切られた高圧室および低圧室を有する第１の膜処理ユニットの前記高圧室を通過させた被処理溶液を第１の溶液と第２の溶液とに分流し、第１の溶液を前記低圧室に通過させることにより、前記高圧室の被処理溶液に含まれる水を前記低圧室の第１の溶液に移動させて被処理溶液を濃縮する第１の膜濃縮工程を備える溶液の膜処理方法であって、前記第１の膜濃縮工程が行われる前の被処理溶液を外部熱源により加熱する加熱工程と、前記第１の膜濃縮工程が行われた第１の溶液および第２の溶液の少なくとも一方を、前記加熱工程が行われる前の被処理溶液と熱交換する熱回収工程とを備え、前記第１の膜濃縮工程が行われた第１の溶液を被処理溶液に合流する合流工程と、前記合流工程が行われた被処理溶液を、逆浸透膜を有する第２の膜処理ユニットに供給して逆浸透膜処理を行うことにより濃縮する第２の膜濃縮工程とを更に備え、前記第１の膜濃縮工程は、前記第２の膜濃縮工程で濃縮された被処理溶液に対して行われ、ナノろ過膜を有する前処理ユニットに被処理溶液を供給する前処理工程を更に備え、前記第２の膜濃縮工程は、前記前処理工程において前記ナノろ過膜を透過した被処理溶液に対して行われる溶液の膜処理方法により達成される。
The object of the present invention is to provide a membrane treatment method for a solution, which comprises a first membrane concentration step in which a solution to be treated that has passed through a high-pressure chamber of a first membrane treatment unit having a high-pressure chamber and a low-pressure chamber separated by a semipermeable membrane is divided into a first solution and a second solution, and the first solution is passed through the low-pressure chamber to move water contained in the solution to be treated in the high-pressure chamber to the first solution in the low-pressure chamber, thereby concentrating the solution to be treated, and further comprises a heating step in which the solution to be treated before the first membrane concentration step is heated by an external heat source, and a heating step in which at least one of the first solution and the second solution that have been subjected to the first membrane concentration step is mixed with the solution to be treated before the heating step. The method further comprises a heat recovery process for exchanging heat , a confluence process for converging the first solution that has been subjected to the first membrane concentration process with the solution to be treated, and a second membrane concentration process for supplying the solution to be treated that has been subjected to the confluence process to a second membrane treatment unit having a reverse osmosis membrane and concentrating it by reverse osmosis membrane treatment, wherein the first membrane concentration process is performed on the solution to be treated that has been concentrated in the second membrane concentration process, and further comprises a pretreatment process for supplying the solution to be treated to a pretreatment unit having a nanofiltration membrane, and the second membrane concentration process is achieved by a membrane treatment method for a solution that is performed on the solution to be treated that has permeated the nanofiltration membrane in the pretreatment process .
前記加熱工程は、前記第２の膜濃縮工程が行われる前の被処理溶液に対して行うことができ、前記熱回収工程は、前記第２の膜濃縮工程が行われた被処理液の透過水を、前記第２の膜濃縮工程が行われる前の被処理溶液と熱交換する工程を更に備えることができる。
The heating step can be performed on the solution to be treated before the second membrane concentration step is performed, and the heat recovery step can further include a step of heat exchanging the permeate of the solution to be treated that has been subjected to the second membrane concentration step with the solution to be treated before the second membrane concentration step is performed.
前記加熱工程および前記熱回収工程は、前記前処理工程が行われた後、前記第２の膜濃縮工程が行われる前の被処理液に対して行うことができる。あるいは、前記加熱工程は、前記前処理工程が行われる前の被処理液に対して行われ、前記熱回収工程は、前記前処理工程が行われた被処理液の非透過液を、前記前処理工程が行われる前の被処理溶液と熱交換する工程を更に備えることができる。
The heating step and the heat recovery step can be performed on the liquid to be treated after the pretreatment step and before the second membrane concentration step. Alternatively, the heating step can be performed on the liquid to be treated before the pretreatment step, and the heat recovery step can further include a step of exchanging heat between the retentate of the liquid to be treated that has been subjected to the pretreatment step and the liquid to be treated before the pretreatment step.
前記熱回収工程は、前記第１の膜濃縮工程が行われた第１の溶液および第２の溶液の少なくとも一方を、前記第２の膜濃縮工程で濃縮された被処理液と熱交換することができる。
The heat recovery step can exchange heat between at least one of the first solution and the second solution that have been subjected to the first membrane concentration step and the liquid to be treated that has been concentrated in the second membrane concentration step.
また、本発明の前記目的は、半透膜により仕切られた高圧室および低圧室を有する第１の膜処理ユニットを備え、前記高圧室を通過させた被処理溶液を第１の溶液と第２の溶液とに分流し、第１の溶液を前記低圧室に通過させることにより、前記高圧室の被処理溶液に含まれる水を前記低圧室の第１の溶液に移動させて被処理溶液を濃縮する溶液の膜処理装置であって、前記第１の膜処理ユニットに供給される前の被処理溶液を外部熱源により加熱する加熱装置と、前記第１の膜処理ユニットで膜処理が行われた第１の溶液および第２の溶液の少なくとも一方を、前記加熱装置で加熱される前の被処理溶液と熱交換する熱回収器とを備え、逆浸透膜を有する第２の膜処理ユニットを更に備え、前記第２の膜処理ユニットは、前記第１の膜処理ユニットで膜処理が行われた第１の溶液を合流させた被処理溶液を逆浸透膜処理により濃縮し、前記第１の膜処理ユニットは、前記第２の膜処理ユニットで濃縮された被処理溶液を濃縮し、ナノろ過膜を有する前処理ユニットを更に備え、前記第２の膜処理ユニットは、前記前処理ユニットの前記ナノろ過膜を透過した被処理溶液を濃縮する溶液の膜処理装置により達成される。 Another object of the present invention is to provide a membrane treatment device for a solution, which comprises a first membrane treatment unit having a high-pressure chamber and a low-pressure chamber separated by a semipermeable membrane, and which divides a solution to be treated that has passed through the high-pressure chamber into a first solution and a second solution, and passes the first solution through the low-pressure chamber, thereby transferring water contained in the solution to be treated in the high-pressure chamber to the first solution in the low-pressure chamber and concentrating the solution to be treated, and which further comprises a heating device that heats the solution to be treated before being supplied to the first membrane treatment unit by an external heat source, and a heating device that heats at least one of the first solution and the second solution that have been subjected to membrane treatment in the first membrane treatment unit. The system further comprises a second membrane treatment unit having a reverse osmosis membrane, and the second membrane treatment unit concentrates the solution to be treated, which is obtained by combining the first solution that has been membrane-treated in the first membrane treatment unit, by reverse osmosis membrane treatment. The first membrane treatment unit concentrates the solution to be treated concentrated in the second membrane treatment unit. The system further comprises a pretreatment unit having a nanofiltration membrane, and the second membrane treatment unit is achieved by a solution membrane treatment device that concentrates the solution to be treated that has permeated the nanofiltration membrane of the pretreatment unit .
本発明によれば、溶液の高濃縮を低コストで効率良く行うことができる溶液の膜処理方法および装置を提供することができる。 The present invention provides a membrane treatment method and apparatus for a solution that can efficiently and inexpensively concentrate the solution.
図１は、本発明の一実施形態に係る溶液の膜処理装置（以下、単に「膜処理装置」という）の概略構成図である。図１に示す膜処理装置１－１は、第１の膜処理ユニット１０と、加熱装置２０と、熱回収器３０，３１とを備えている。 Figure 1 is a schematic diagram of a membrane treatment device for a solution (hereinafter simply referred to as "membrane treatment device") according to one embodiment of the present invention. The membrane treatment device 1-1 shown in Figure 1 includes a first membrane treatment unit 10, a heating device 20, and heat recovery devices 30 and 31.
第１の膜処理ユニット１０は、室内が半透膜１１で仕切られることにより高圧室１２および低圧室１３が形成されている。高圧室１２には、被処理溶液である原液が導入される。原液は、例えば海水であり、膜処理装置１により濃縮して製塩などを行うことができる。但し、原液は特に限定されるものではなく、海水以外の無機塩の溶液や、有機溶液等であってもよい。 The first membrane treatment unit 10 has a chamber separated by a semipermeable membrane 11, forming a high-pressure chamber 12 and a low-pressure chamber 13. A raw solution, which is the solution to be treated, is introduced into the high-pressure chamber 12. The raw solution is, for example, seawater, and can be concentrated using the membrane treatment device 1 to produce salt, etc. However, the raw solution is not particularly limited and may be a solution of inorganic salts other than seawater, an organic solution, etc.
高圧室１２を通過した原液は、第１の溶液と第２の溶液とに分流されて、第１の溶液が低圧室１３を通過する。高圧室１２の原液は、低圧室１３の第１の溶液よりも高圧であるため、この圧力差によって高圧室１２の原液に含まれる水が低圧室１３の第１の溶液に移動し、第１の膜処理ユニット１０を通過した原液が濃縮される。すなわち、第２の溶液は高濃縮液である一方、低圧室１３を通過した第１の溶液は希釈水となる。 The stock solution that passes through the high-pressure chamber 12 is divided into a first solution and a second solution, and the first solution passes through the low-pressure chamber 13. Because the stock solution in the high-pressure chamber 12 is at a higher pressure than the first solution in the low-pressure chamber 13, this pressure difference causes the water contained in the stock solution in the high-pressure chamber 12 to move into the first solution in the low-pressure chamber 13, concentrating the stock solution that passed through the first membrane treatment unit 10. In other words, the second solution is a highly concentrated solution, while the first solution that passed through the low-pressure chamber 13 becomes diluted water.
加熱装置２０は、第１の膜処理ユニット１０に供給される前の原液を、蒸気等のバックアップ熱源と熱交換する熱交換器であり、流量調整弁２３の開度調整により、加熱量を調整することができる。加熱装置２０は、加熱後の原液の温度を検出する温度センサ２１と、温度センサ２１の検出温度が設定温度になるように流量調整弁２３の開度を制御するコントローラ２２とを備えており、第１の膜処理ユニット１０に供給される原液の温度を、所望の温度に維持することができる。加熱装置２０の構成は、外部熱源により原液を加熱する構成であれば特に限定されず、ヒータ等であってもよい。 The heating device 20 is a heat exchanger that exchanges heat between the raw liquid and a backup heat source such as steam before it is supplied to the first membrane treatment unit 10, and the amount of heat can be adjusted by adjusting the opening of the flow control valve 23. The heating device 20 is equipped with a temperature sensor 21 that detects the temperature of the raw liquid after heating, and a controller 22 that controls the opening of the flow control valve 23 so that the temperature detected by the temperature sensor 21 becomes the set temperature, thereby maintaining the temperature of the raw liquid supplied to the first membrane treatment unit 10 at the desired temperature. The configuration of the heating device 20 is not particularly limited as long as it is configured to heat the raw liquid using an external heat source, and may be a heater, etc.
熱回収器３０，３１は、いずれも熱交換器であり、加熱装置２０に供給される前の原液の一部が分岐流路２，３により導入され、第１の膜処理ユニット１０で膜処理が行われた第２の溶液および第１の溶液とそれぞれ熱交換される。熱回収器３０，３１で熱回収が行われた原液は、分岐流路２，３の分岐部の下流側で原液の残部に合流され、合流後の原液が加熱装置２０に供給される。分岐流路２，３の分岐箇所および合流箇所は、加熱装置２０の上流側における任意の箇所とすることができる。 Heat recovery devices 30 and 31 are both heat exchangers, into which a portion of the raw liquid before being supplied to heating device 20 is introduced via branch flow paths 2 and 3, and heat is exchanged with the second solution and the first solution, respectively, that have undergone membrane treatment in first membrane treatment unit 10. The raw liquid that has undergone heat recovery in heat recovery devices 30 and 31 is merged with the remainder of the raw liquid downstream of the branch points of branch flow paths 2 and 3, and the merged raw liquid is supplied to heating device 20. The branch points and merge points of branch flow paths 2 and 3 can be any location upstream of heating device 20.
次に、上記の構成を備える膜処理装置１－１を用いた溶液の膜処理方法（以下、単に「膜処理方法」という）を説明する。まず、原液を加熱装置２０により加熱する加熱工程を行った後、第１の膜処理ユニット１０の高圧室１２に供給し、原液を濃縮する第１の膜濃縮工程を行う。濃縮された原液は、一部が第１の溶液として低圧室１３を通過することにより希釈水となる一方、残部が高濃縮液である第２の溶液として製塩工程などの次工程へと送られる。 Next, we will explain a membrane treatment method for a solution (hereinafter simply referred to as the "membrane treatment method") using the membrane treatment device 1-1 configured as described above. First, the stock solution is heated using the heating device 20 in a heating process, and then supplied to the high-pressure chamber 12 of the first membrane treatment unit 10, where a first membrane concentration process is carried out to concentrate the stock solution. A portion of the concentrated stock solution passes through the low-pressure chamber 13 as the first solution and becomes dilution water, while the remainder is sent to the next process, such as a salt production process, as a second solution, which is a highly concentrated liquid.
第１の膜濃縮工程が行われた第１の溶液および第２の溶液は、それぞれ熱回収器３１，３０の通過により、加熱装置２０に供給される前の原液の一部と熱交換する。これにより、第１の溶液および第２の溶液の熱量を回収して原液を昇温する熱回収工程が行われる。 The first solution and second solution that have undergone the first membrane concentration process pass through heat recovery devices 31 and 30, respectively, where they exchange heat with a portion of the raw liquid before being supplied to the heating device 20. This results in a heat recovery process in which the heat of the first solution and second solution is recovered to raise the temperature of the raw liquid.
このように、本実施形態の膜処理装置および膜処理方法によれば、原液を外部熱源により所望の温度に加熱して、第１の膜処理ユニットにより濃縮することができるので、第１の膜処理ユニットにおける濃縮率を高めることができ、半透膜の膜面積を小さくして第１の膜処理ユニットの小型化および低コスト化を図ることができる。また、原液の加熱に要した熱量は、第１の溶液および第２の溶液と原液との熱交換により回収されるので、外部熱源の熱量を抑制することができ、ランニングコストを低減することができる。したがって、原液の高濃縮を低コストで効率良く行うことができる。 As described above, according to the membrane treatment device and membrane treatment method of this embodiment, the stock solution can be heated to a desired temperature using an external heat source and concentrated using the first membrane treatment unit, thereby increasing the concentration rate in the first membrane treatment unit and reducing the membrane area of the semipermeable membrane, thereby enabling the first membrane treatment unit to be made smaller and less expensive. Furthermore, the heat required to heat the stock solution is recovered through heat exchange between the stock solution and the first and second solutions, thereby reducing the heat required from the external heat source and reducing running costs. Therefore, the stock solution can be highly concentrated efficiently and at low cost.
本実施形態においては、第１の溶液および第２の溶液の双方を原液と熱交換することにより、熱回収を行っているが、第１の溶液および第２の溶液の少なくとも一方を、加熱装置２０で加熱する前の原液と熱交換する構成であればよい。すなわち、図１に示す熱回収器３０，３１は、いずれか一方のみを備える構成にしてもよく、この点については後述する各実施形態においても同様である。 In this embodiment, heat recovery is performed by exchanging heat between both the first solution and the second solution and the stock solution, but any configuration is possible as long as at least one of the first solution and the second solution is heat exchanged with the stock solution before being heated by the heating device 20. In other words, the heat recovery devices 30 and 31 shown in FIG. 1 may be configured to include only one of them, and this also applies to the other embodiments described below.
以上、本発明の一実施形態について詳述したが、本発明の具体的な態様は上記実施形態に限定されず、種々の変形が可能である。図２は、本発明の他の実施形態に係る溶液の膜処理装置の概略構成図である。図２に示す膜処理装置１－２は、図１に示す膜処理装置１－１において、加熱装置２０と第１の膜処理ユニット１０との間に第２の膜処理ユニット４０を配置したものである。なお、以下の各図において、同様の構成部分には同一の符号を付している。 Although one embodiment of the present invention has been described in detail above, the specific aspects of the present invention are not limited to the above embodiment and various modifications are possible. Figure 2 is a schematic diagram of a membrane treatment device for a solution according to another embodiment of the present invention. The membrane treatment device 1-2 shown in Figure 2 is the membrane treatment device 1-1 shown in Figure 1, with a second membrane treatment unit 40 positioned between the heating device 20 and the first membrane treatment unit 10. Note that in the following figures, similar components are designated by the same reference numerals.
第２の膜処理ユニット４０は、ケーシング内に逆浸透膜４１を備えており、原液を加圧供給して逆浸透膜処理を行うことにより濃縮する。濃縮された原液は、第１の膜処理ユニット１０の高圧室１２に供給される。逆浸透膜４１は、逆浸透膜処理が可能な半透膜であればよく、ＲＯ膜以外にＮＦ膜などであってもよい。第１の膜処理ユニット１０の低圧室１３を通過した希釈水（第１の溶液）は、合流部５において原液に合流される。第２の膜処理ユニット４０は、１段に構成する代わりに複数段に構成してもよい。 The second membrane treatment unit 40 is equipped with a reverse osmosis membrane 41 within a casing, and concentrates the stock solution by supplying it under pressure and performing reverse osmosis membrane treatment. The concentrated stock solution is supplied to the high-pressure chamber 12 of the first membrane treatment unit 10. The reverse osmosis membrane 41 may be any semipermeable membrane capable of reverse osmosis membrane treatment, and may be an NF membrane other than an RO membrane. The diluted water (first solution) that passes through the low-pressure chamber 13 of the first membrane treatment unit 10 is merged with the stock solution at the junction 5. The second membrane treatment unit 40 may be configured as a single stage or multiple stages.
図２に示す膜処理装置１－２は、加熱装置２０に供給される前の原液の一部が、分岐流路２，３により熱回収器３０，３１に供給されて第２の溶液および第１の溶液とそれぞれ熱交換すると共に、分岐流路４により熱交換器３２にも供給されて、第２の膜処理ユニット４０の逆浸透膜４１を透過した透過水と熱交換される。なお、図２においては、分岐流路２，３，４の一部を省略して図示している。 In the membrane treatment device 1-2 shown in Figure 2, a portion of the raw liquid before being supplied to the heating device 20 is supplied to heat recovery devices 30 and 31 via branch flow paths 2 and 3, where it exchanges heat with the second solution and the first solution, respectively, and is also supplied to heat exchanger 32 via branch flow path 4, where it exchanges heat with the permeate that has permeated the reverse osmosis membrane 41 of the second membrane treatment unit 40. Note that some of the branch flow paths 2, 3, and 4 are omitted from Figure 2.
図２に示す膜処理装置１－２による膜処理方法は、図１に示す膜処理装置１－１による膜処理方法において、第１の膜濃縮工程が行われた希釈水（第１の溶液）を合流部５において原液と合流する合流工程と、合流工程が行われた原液を第２の膜処理ユニット４０において濃縮する第２の膜濃縮工程とを更に備えることにより、高濃縮液（第２の溶液）の濃縮率を容易に高めることができる。 The membrane treatment method using membrane treatment device 1-2 shown in Figure 2 is the same as the membrane treatment method using membrane treatment device 1-1 shown in Figure 1, except that it further includes a confluence step in which diluted water (first solution) that has undergone the first membrane concentration step is combined with the stock solution at confluence section 5, and a second membrane concentration step in which the stock solution that has undergone the confluence step is concentrated in second membrane treatment unit 40, thereby easily increasing the concentration rate of the highly concentrated solution (second solution).
また、加熱装置２０による加熱工程が第２の膜濃縮工程が行われる前の原液に対して行われ、熱回収工程は、原液の加熱に要した熱量を、熱回収器３０，３１で回収すると共に、熱回収器３２においても回収するため、原液の濃縮を低コストで効率よく行うことができる。特に、第２の膜処理ユニット４０の逆浸透膜４１がＲＯ膜である場合には、逆浸透膜４１の透過水の流量が多くなるため、熱回収器３２での熱回収がより効果的である。 In addition, the heating process using the heating device 20 is performed on the raw liquid before the second membrane concentration process is performed, and the heat recovery process recovers the heat required to heat the raw liquid in the heat recovery devices 30 and 31, as well as in the heat recovery device 32, allowing the raw liquid to be concentrated efficiently and at low cost. In particular, when the reverse osmosis membrane 41 of the second membrane treatment unit 40 is an RO membrane, the flow rate of the permeate through the reverse osmosis membrane 41 is high, making heat recovery in the heat recovery device 32 more effective.
図３は、本発明の更に他の実施形態に係る溶液の膜処理装置の概略構成図である。図３に示す膜処理装置１－３は、図２に示す膜処理装置１－２において、加熱装置２０を、第２の膜処理ユニット４０の上流側に配置する代わりに、第２の膜処理ユニット４０と第１の膜処理ユニット１０との間に配置したものであり、第２の膜処理ユニット４０で濃縮後の原液により、熱回収器３０，３１における熱回収工程が行われる。図３に示す膜処理装置１－３は、加熱装置２０により加熱された原液が、第２の膜処理ユニット４０に直接供給されないため、第２の膜処理ユニット４０の加熱が不要な場合や加熱を望まない場合などに有効である。 Figure 3 is a schematic diagram of a membrane treatment device for a solution according to yet another embodiment of the present invention. The membrane treatment device 1-3 shown in Figure 3 is similar to the membrane treatment device 1-2 shown in Figure 2, except that instead of locating the heating device 20 upstream of the second membrane treatment unit 40, it is located between the second membrane treatment unit 40 and the first membrane treatment unit 10. The heat recovery process in the heat recovery devices 30, 31 is performed using the stock solution concentrated in the second membrane treatment unit 40. The membrane treatment device 1-3 shown in Figure 3 is effective when heating the second membrane treatment unit 40 is not necessary or desired, because the stock solution heated by the heating device 20 is not directly supplied to the second membrane treatment unit 40.
図４に示す膜処理装置１－４は、図３に示す膜処理装置１－３において、第２の膜処理ユニット４０に供給される前の原液の前処理を行う前処理ユニット５０を更に備えるものであり、第２の膜濃縮工程の前に、前処理ユニット５０による前処理工程を行うことができる。前処理ユニット５０は、ケーシング内にＮＦ膜５１を備えており、原液をＮＦ膜５１に通水することにより、海水のスケール成分等がブライン（非透過液）として外部に排出される。図４に示す構成においては、第２の膜処理ユニット４０の逆浸透膜はＲＯ膜であることが好ましい。前処理ユニット５０は、１段に構成する代わりに複数段に構成してもよい。図４に示す膜処理装置１－４は、第２の膜処理ユニット４０および前処理ユニット５０を、加熱装置２０による加熱対象外とすることができる。 The membrane treatment device 1-4 shown in Figure 4 is the membrane treatment device 1-3 shown in Figure 3, further equipped with a pretreatment unit 50 that pretreats the raw liquid before it is supplied to the second membrane treatment unit 40. The pretreatment unit 50 can perform a pretreatment process before the second membrane concentration process. The pretreatment unit 50 has an NF membrane 51 inside a casing. By passing the raw liquid through the NF membrane 51, scale components of seawater and the like are discharged to the outside as brine (non-permeated liquid). In the configuration shown in Figure 4, the reverse osmosis membrane of the second membrane treatment unit 40 is preferably an RO membrane. The pretreatment unit 50 may be configured in multiple stages instead of a single stage. In the membrane treatment device 1-4 shown in Figure 4, the second membrane treatment unit 40 and the pretreatment unit 50 can be excluded from the heating device 20.
図５に示す膜処理装置１－５は、図４に示す膜処理装置１－４において、加熱装置２０を、第２の膜処理ユニット４０と第１の膜処理ユニット１０との間に配置する代わりに、前処理ユニット５０と第２の膜処理ユニット４０との間に配置したものであり、前処理工程が行われた後、第２の膜濃縮工程が行われる前の原液に対して、加熱工程および熱回収工程が行われる。この膜処理装置１－５は、第２の膜処理ユニット４０の透過水の熱量を、熱回収器３２により回収することができる。 The membrane treatment device 1-5 shown in Figure 5 is the same as the membrane treatment device 1-4 shown in Figure 4, except that instead of placing the heating device 20 between the second membrane treatment unit 40 and the first membrane treatment unit 10, it is placed between the pretreatment unit 50 and the second membrane treatment unit 40. After the pretreatment process, the raw liquid is subjected to a heating process and a heat recovery process before being subjected to the second membrane concentration process. This membrane treatment device 1-5 can recover the heat of the permeate from the second membrane treatment unit 40 using the heat recovery device 32.
図６に示す膜処理装置１－６は、図５に示す膜処理装置１－５において、加熱装置２０を、前処理ユニット５０と第２の膜処理ユニット４０との間に配置する代わりに、前処理ユニット５０の上流側に配置したものである。図６に示す膜処理装置１－６は、加熱装置２０に供給される前の原液の一部が、分岐流路５により熱交換器３３にも供給されて、前処理ユニット５０のブライン（非透過液）と熱交換されるため、熱回収工程において、原液の加熱に要した熱量を、熱回収器３０，３２で回収すると共に、熱回収器３３においても回収することができる。 The membrane treatment device 1-6 shown in Figure 6 is the same as the membrane treatment device 1-5 shown in Figure 5, except that instead of locating the heating device 20 between the pretreatment unit 50 and the second membrane treatment unit 40, it is located upstream of the pretreatment unit 50. In the membrane treatment device 1-6 shown in Figure 6, a portion of the raw liquid before being supplied to the heating device 20 is also supplied to the heat exchanger 33 via the branch flow path 5, where it exchanges heat with the brine (non-permeated liquid) from the pretreatment unit 50. Therefore, in the heat recovery process, the heat required to heat the raw liquid can be recovered in the heat recovery devices 30 and 32, as well as in the heat recovery device 33.
１ 膜処理装置
１０ 第１の膜処理ユニット
１１ 半透膜
１２ 高圧室
１３ 低圧室
２０ 加熱装置
３０，３１，３２，３３ 熱回収器
４０ 第２の膜処理ユニット
４１ 逆浸透膜
５０ 前処理ユニット
５１ ナノろ過膜
1 Membrane treatment device 10 First membrane treatment unit 11 Semipermeable membrane 12 High pressure chamber 13 Low pressure chamber 20 Heating device 30, 31, 32, 33 Heat recovery device 40 Second membrane treatment unit 41 Reverse osmosis membrane 50 Pretreatment unit 51 Nanofiltration membrane
Claims (6)
前記第１の膜濃縮工程が行われる前の被処理溶液を外部熱源により加熱する加熱工程と、
前記第１の膜濃縮工程が行われた第１の溶液および第２の溶液の少なくとも一方を、前記加熱工程が行われる前の被処理溶液と熱交換する熱回収工程とを備え、
前記第１の膜濃縮工程が行われた第１の溶液を被処理溶液に合流する合流工程と、
前記合流工程が行われた被処理溶液を、逆浸透膜を有する第２の膜処理ユニットに供給して逆浸透膜処理を行うことにより濃縮する第２の膜濃縮工程とを更に備え、
前記第１の膜濃縮工程は、前記第２の膜濃縮工程で濃縮された被処理溶液に対して行われ、
ナノろ過膜を有する前処理ユニットに被処理溶液を供給する前処理工程を更に備え、
前記第２の膜濃縮工程は、前記前処理工程において前記ナノろ過膜を透過した被処理溶液に対して行われる溶液の膜処理方法。 A membrane treatment method for a solution, comprising a first membrane concentration step of dividing a solution to be treated that has passed through a high-pressure chamber of a first membrane treatment unit having a high-pressure chamber and a low-pressure chamber separated by a semipermeable membrane into a first solution and a second solution, and passing the first solution through the low-pressure chamber, thereby transferring water contained in the solution to be treated in the high-pressure chamber to the first solution in the low-pressure chamber, thereby concentrating the solution to be treated,
a heating step of heating the solution to be treated by an external heat source before the first membrane concentration step is performed;
a heat recovery step of exchanging heat between at least one of the first solution and the second solution that has been subjected to the first membrane concentration step and the solution to be treated before the heating step ,
a confluence step of converging the first solution that has been subjected to the first membrane concentration step with the solution to be treated;
a second membrane concentration step of supplying the solution to be treated that has been subjected to the joining step to a second membrane treatment unit having a reverse osmosis membrane and concentrating the solution by reverse osmosis membrane treatment,
the first membrane concentration step is performed on the solution to be treated that has been concentrated in the second membrane concentration step;
A pretreatment step of supplying the solution to be treated to a pretreatment unit having a nanofiltration membrane is further provided,
The second membrane concentration step is a membrane treatment method for a solution, which is performed on the solution to be treated that has permeated the nanofiltration membrane in the pretreatment step .
前記熱回収工程は、前記第２の膜濃縮工程が行われた被処理液の透過水を、前記第２の膜濃縮工程が行われる前の被処理溶液と熱交換する工程を更に備える請求項１に記載の溶液の膜処理方法。 the heating step is performed on the solution to be treated before the second membrane concentration step is performed,
2. The membrane treatment method for a solution according to claim 1, wherein the heat recovery step further comprises a step of exchanging heat between the permeate of the solution to be treated that has been subjected to the second membrane concentration step and the solution to be treated that has not yet been subjected to the second membrane concentration step.
前記熱回収工程は、前記前処理工程が行われた被処理液の非透過液を、前記前処理工程が行われる前の被処理溶液と熱交換する工程を更に備える請求項１に記載の溶液の膜処理方法。 The heating step is performed on the liquid to be treated before the pretreatment step is performed,
2. The membrane treatment method for a solution according to claim 1 , wherein the heat recovery step further comprises a step of exchanging heat between the non-permeated liquid of the solution to be treated that has been subjected to the pretreatment step and the solution to be treated that has not yet been subjected to the pretreatment step.
前記第１の膜処理ユニットに供給される前の被処理溶液を外部熱源により加熱する加熱装置と、
前記第１の膜処理ユニットで膜処理が行われた第１の溶液および第２の溶液の少なくとも一方を、前記加熱装置で加熱される前の被処理溶液と熱交換する熱回収器とを備え、
逆浸透膜を有する第２の膜処理ユニットを更に備え、
前記第２の膜処理ユニットは、前記第１の膜処理ユニットで膜処理が行われた第１の溶液を合流させた被処理溶液を逆浸透膜処理により濃縮し、
前記第１の膜処理ユニットは、前記第２の膜処理ユニットで濃縮された被処理溶液を濃縮し、
ナノろ過膜を有する前処理ユニットを更に備え、
前記第２の膜処理ユニットは、前記前処理ユニットの前記ナノろ過膜を透過した被処理溶液を濃縮する溶液の膜処理装置。 A membrane treatment device for a solution, comprising a first membrane treatment unit having a high-pressure chamber and a low-pressure chamber separated by a semipermeable membrane, wherein a solution to be treated that has passed through the high-pressure chamber is divided into a first solution and a second solution, and the first solution is passed through the low-pressure chamber, thereby transferring water contained in the solution to be treated in the high-pressure chamber to the first solution in the low-pressure chamber, thereby concentrating the solution to be treated,
a heating device that heats the solution to be treated by an external heat source before being supplied to the first membrane treatment unit;
a heat recovery device that exchanges heat between at least one of the first solution and the second solution that has been subjected to membrane treatment in the first membrane treatment unit and the solution to be treated before being heated by the heating device;
a second membrane treatment unit having a reverse osmosis membrane;
the second membrane treatment unit concentrates the solution to be treated, which is obtained by joining the first solution that has been subjected to membrane treatment in the first membrane treatment unit, by reverse osmosis membrane treatment;
the first membrane treatment unit concentrates the solution to be treated that has been concentrated in the second membrane treatment unit;
further comprising a pretreatment unit having a nanofiltration membrane;
The second membrane treatment unit is a membrane treatment device for a solution that concentrates the solution to be treated that has permeated the nanofiltration membrane of the pretreatment unit .
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