JP5526093B2 - Seawater desalination method and seawater desalination apparatus - Google Patents

Seawater desalination method and seawater desalination apparatus Download PDF

Info

Publication number
JP5526093B2
JP5526093B2 JP2011197406A JP2011197406A JP5526093B2 JP 5526093 B2 JP5526093 B2 JP 5526093B2 JP 2011197406 A JP2011197406 A JP 2011197406A JP 2011197406 A JP2011197406 A JP 2011197406A JP 5526093 B2 JP5526093 B2 JP 5526093B2
Authority
JP
Japan
Prior art keywords
water
seawater
concentration
salt
reverse osmosis
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
JP2011197406A
Other languages
Japanese (ja)
Other versions
JP2013056320A (en
Inventor
雅彦 三浦
光重 島田
紘史 丸野
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shinko Pantec Co Ltd
Original Assignee
Kobelco Eco Solutions Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Kobelco Eco Solutions Co Ltd filed Critical Kobelco Eco Solutions Co Ltd
Priority to JP2011197406A priority Critical patent/JP5526093B2/en
Priority to PCT/JP2012/064517 priority patent/WO2013035397A1/en
Publication of JP2013056320A publication Critical patent/JP2013056320A/en
Application granted granted Critical
Publication of JP5526093B2 publication Critical patent/JP5526093B2/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2649—Filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2688—Biological processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/06—Submerged-type; Immersion type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/04—Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Nanotechnology (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Activated Sludge Processes (AREA)

Description

本発明は、海水淡水化方法および海水淡水化装置に関し、例えば、逆浸透膜を用いた逆浸透膜装置によるろ過によって海水を淡水化する海水淡水化方法および海水淡水化装置に関する。   The present invention relates to a seawater desalination method and a seawater desalination apparatus, for example, a seawater desalination method and a seawater desalination apparatus that desalinate seawater by filtration using a reverse osmosis membrane apparatus using a reverse osmosis membrane.

近年、地球温暖化等により雨が局所的に若しくは短時間に降ってしまい水資源が地理的若しくは時間的に偏在してしまうことや、林業衰退や森林伐採等により山間部の保水力が低下してしまうこと等により、水資源を安定的に確保することが難しいという問題がある。   In recent years, rain has fallen locally or in a short time due to global warming, etc., and water resources are unevenly distributed geographically or temporally, and the water retention capacity of mountainous areas has declined due to forestry decline or deforestation. As a result, there is a problem that it is difficult to stably secure water resources.

水資源を安定的に確保すべく、例えば、臨海地域では、逆浸透膜装置を用いたろ過処理によって海水を淡水化する方法及び設備が提案されている（例えば、特許文献１）。   In order to secure water resources stably, for example, in a coastal area, a method and equipment for desalinating seawater by filtration using a reverse osmosis membrane device have been proposed (for example, Patent Document 1).

しかし、上記特許文献１に記載の海水淡水化方法及び海水淡水化設備では、海水を逆浸透膜装置でろ過処理するのに海水を加圧してポンプ等で逆浸透膜装置に圧送する必要があるので、海水の塩濃度が高いほど、海水を逆浸透膜装置に圧送するために多大なエネルギーが必要となるという問題があった。   However, in the seawater desalination method and seawater desalination facility described in Patent Document 1, it is necessary to pressurize seawater and pump it to the reverse osmosis membrane device with a pump or the like in order to filter the seawater with the reverse osmosis membrane device. Therefore, there was a problem that the higher the salt concentration of seawater, the greater the energy required to pump seawater to the reverse osmosis membrane device.

そこで、有機物を含有する廃水（以下、有機性廃水とも言う）を生物処理して得られる生物処理水を希釈水として海水に混合し、混合により得られた混合水を逆浸透膜装置に供給してろ過処理することで、海水の圧送に要する動力（エネルギー）を低減する海水を淡水化する海水淡水化方法及び海水淡水化装置が提案されている（例えば特許文献２）。   Therefore, biological treatment water obtained by biological treatment of wastewater containing organic matter (hereinafter also referred to as organic wastewater) is mixed with seawater as dilution water, and the mixed water obtained by mixing is supplied to the reverse osmosis membrane device. In addition, a seawater desalination method and a seawater desalination apparatus for desalinating seawater that reduce power (energy) required for pumping seawater by filtration are proposed (for example, Patent Document 2).

特開２００８−５５３１７号公報JP 2008-55317 A 特開２０１０−１４９１００号公報JP 2010-149100 A

しかしながら、上記特許文献２の海水淡水化方法及び海水淡水化装置において、海水の淡水化に要するエネルギーを低減するために、希釈水としての生物処理水の比率を大きくすると、生物処理水に含有される有機物や生物、および生物由来の有機性固形物が付着し堆積するために逆浸透膜（ＲＯ膜）の詰り（所謂バイオファウリング）の海水混合による抑制が不十分となる場合があることがわかった。バイオファウリングの程度が大きいと、ＲＯ膜を洗浄する回数が多くなる、多量のバイオファウリング抑制剤を必要とする、また、最悪の場合、必要なＲＯ透過水の量が確保できなくなるなど、海水から淡水を生成する効率が低下してしまう。   However, in the seawater desalination method and seawater desalination apparatus of Patent Document 2, if the ratio of biologically treated water as dilution water is increased in order to reduce the energy required for seawater desalination, it is contained in the biologically treated water. Organic matter and organisms, and organic solids derived from organisms may adhere and accumulate, and the suppression of reverse osmosis membrane (RO membrane) clogging (so-called biofouling) by seawater mixing may be insufficient. all right. If the degree of biofouling is large, the number of times the RO membrane is washed increases, a large amount of biofouling inhibitor is required, and in the worst case, the amount of necessary RO permeate cannot be secured. The efficiency of producing fresh water from seawater will decrease.

本発明は、上記問題点に鑑み、海水の淡水化に要するエネルギーを低減するとともに、バイオファウリングを十分に抑制する海水淡水化方法及び海水淡水化装置を提供することを課題とする。   In view of the above problems, an object of the present invention is to provide a seawater desalination method and a seawater desalination apparatus that reduce energy required for seawater desalination and sufficiently suppress biofouling.

本発明者は、海水の淡水化に要するエネルギーを低減するために、有機性廃水を生物処理して得られる生物処理水を利用した場合であっても、バイオファウリングを十分に抑制するために、生物処理水に含有される生物の耐塩性を検討し、生物処理水に含有される生物のうち、低度好塩性生物及び非好塩性生物は０．５Ｍを超える塩濃度の雰囲気では生育されにくいことに着目して本発明を完成させた。   In order to sufficiently suppress bio-fouling even when the present inventor uses biologically treated water obtained by biologically treating organic wastewater in order to reduce the energy required for desalination of seawater. Investigate the salt tolerance of organisms contained in biologically treated water. Among organisms contained in biologically treated water, low-halogenated organisms and non-halophilic organisms are used in an atmosphere with a salt concentration exceeding 0.5M. This invention was completed paying attention to being hard to grow.

すなわち、本発明の一の局面における海水淡水化方法は、逆浸透膜装置を用いたろ過処理によって海水を淡水化する海水淡水化方法であって、有機性廃水を生物処理して得られる生物処理水と海水とを混合することにより、０．５Ｍ以下の塩濃度を有する低濃度塩水を生成し、該低濃度塩水を該逆浸透膜装置に供給してろ過処理する工程と、該生物処理水と該海水とを混合することにより、または海水のみを用いることにより、０．５Ｍを超える塩濃度を有する高濃度塩水を生成し、該高濃度塩水を該逆浸透膜装置に供給してろ過処理する工程とを備える。   That is, the seawater desalination method according to one aspect of the present invention is a seawater desalination method for desalinating seawater by filtration using a reverse osmosis membrane device, and is a biological treatment obtained by biologically treating organic wastewater. A step of producing low-concentration salt water having a salt concentration of 0.5 M or less by mixing water and seawater, supplying the low-concentration salt water to the reverse osmosis membrane device, and performing a filtration treatment; And high-concentration salt water having a salt concentration of more than 0.5M is generated by mixing the salt water with the sea water or by using only sea water, and the high-concentration salt water is supplied to the reverse osmosis membrane device and filtered. And a step of performing.

本発明の一の局面における海水淡水化装置は、逆浸透膜装置を用いたろ過処理によって海水を淡水化するための海水淡水化装置であって、有機性廃水を生物処理して得られる生物処理水と海水とを混合することにより、０．５Ｍ以下の塩濃度を有する低濃度塩水を生成することと、該生物処理水と海水とを混合することにより、または海水のみを用いることにより、０．５Ｍを超える塩濃度を有する高濃度塩水を生成することとが可能なように構成されている混合部と、該混合部で得られる該低濃度塩水及び該高濃度塩水をろ過処理する逆浸透膜装置とを備える。   A seawater desalination apparatus according to one aspect of the present invention is a seawater desalination apparatus for desalinating seawater by filtration using a reverse osmosis membrane apparatus, and is a biological treatment obtained by biologically treating organic wastewater. By mixing water and seawater, low-concentration saltwater having a salt concentration of 0.5 M or less is generated, by mixing the biologically treated water and seawater, or by using only seawater, 0 A mixing unit configured to be capable of generating high-concentration salt water having a salt concentration exceeding 5M, and the reverse osmosis for filtering the low-concentration salt water obtained in the mixing unit and the high-concentration salt water A membrane device.

本発明の一の局面における海水淡水化方法及び海水淡水化装置によれば、塩濃度が０．５Ｍを超える高濃度塩水を逆浸透膜装置に供給することにより、低度好塩性生物及び非好塩性生物が生育されにくい雰囲気になる。このため、塩濃度が０．５Ｍ以下の低濃度塩水を逆浸透膜装置でろ過処理する工程により、海水の淡水化に要するエネルギーを低減しつつ、高濃度塩水を逆浸透膜装置に供給することにより、バイオファウリングを十分に抑制できる。したがって、本発明は、海水の淡水化に要するエネルギーを低減するとともに、バイオファウリングを十分に抑制することができる海水淡水化方法及び海水淡水化装置を提供することができる。   According to the seawater desalination method and seawater desalination apparatus in one aspect of the present invention, by supplying high-concentration salt water having a salt concentration exceeding 0.5 M to the reverse osmosis membrane device, An atmosphere in which halophilic organisms are difficult to grow. For this reason, supplying the high concentration salt water to the reverse osmosis membrane device while reducing the energy required for seawater desalination by the step of filtering the low concentration salt water having a salt concentration of 0.5 M or less by the reverse osmosis membrane device. Thus, biofouling can be sufficiently suppressed. Therefore, this invention can provide the seawater desalination method and seawater desalination apparatus which can fully suppress biofouling while reducing the energy required for seawater desalination.

また、本発明者は、海水の淡水化に要するエネルギーを低減するために、有機性廃水を生物処理して得られる生物処理水を利用した場合であっても、バイオファウリングを十分に抑制するために、生物処理水に含有される生物の耐塩性を検討し、生物処理水に含有される生物のうち、非好塩性生物は０．２Ｍを超える塩濃度の雰囲気では生育されにくいことに着目して本発明を完成させた。   In addition, in order to reduce energy required for desalination of seawater, the present inventor sufficiently suppresses biofouling even when biologically treated water obtained by biologically treating organic wastewater is used. Therefore, the salt tolerance of the organisms contained in the biologically treated water is examined, and among the organisms contained in the biologically treated water, non-halogenous organisms are difficult to grow in an atmosphere with a salt concentration exceeding 0.2M. The present invention was completed with attention.

すなわち、本発明の他の局面における海水淡水化方法は、逆浸透膜装置を用いたろ過処理によって海水を淡水化する海水淡水化方法であって、有機性廃水を生物処理して得られる生物処理水と海水とを混合することにより、０．２Ｍ以下の塩濃度を有する低濃度塩水を生成し、該低濃度塩水を該逆浸透膜装置に供給してろ過処理する工程と、該生物処理水と該海水とを混合することにより、または海水のみを用いることにより、０．２Ｍを超える塩濃度を有する高濃度塩水を生成し、該高濃度塩水を該逆浸透膜装置に供給してろ過処理する工程とを備える。   That is, the seawater desalination method according to another aspect of the present invention is a seawater desalination method that desalinates seawater by filtration using a reverse osmosis membrane device, and is a biological treatment obtained by biologically treating organic wastewater. A step of producing low-concentration salt water having a salt concentration of 0.2M or less by mixing water and seawater, supplying the low-concentration salt water to the reverse osmosis membrane device, and performing a filtration treatment; Is mixed with seawater or only seawater is used to produce high-concentration salt water having a salt concentration of more than 0.2M, and supply the high-concentration salt water to the reverse osmosis membrane device for filtration treatment And a step of performing.

本発明の他の局面における海水淡水化装置は、逆浸透膜装置を用いたろ過処理によって海水を淡水化するための海水淡水化装置であって、有機性廃水を生物処理して得られる生物処理水と海水とを混合することにより、０．２Ｍ以下の塩濃度を有する低濃度塩水を生成することと、該生物処理水と海水とを混合することにより、または海水のみを用いることにより、０．２Ｍを超える塩濃度を有する高濃度塩水を生成することとが可能なように構成されている混合部と、該混合部で得られる該低濃度塩水及び該高濃度塩水をろ過処理する逆浸透膜装置とを備える。   A seawater desalination apparatus according to another aspect of the present invention is a seawater desalination apparatus for desalinating seawater by filtration using a reverse osmosis membrane apparatus, and is a biological treatment obtained by biologically treating organic wastewater. By mixing water and seawater, producing low-concentration saltwater having a salt concentration of 0.2 M or less, mixing the biologically treated water and seawater, or using only seawater, 0 A mixing unit configured to be capable of generating high-concentration salt water having a salt concentration exceeding 2M, and the low-concentration salt water obtained in the mixing unit and reverse osmosis for filtering the high-concentration salt water A membrane device.

本発明の他の局面における海水淡水化方法及び海水淡水化装置によれば、塩濃度が０．２Ｍを超える高濃度塩水を逆浸透膜装置に供給することにより、非好塩性生物が生育されにくい雰囲気になる。このため、塩濃度が０．２Ｍ以下の低濃度塩水を逆浸透膜装置でろ過処理する工程により、海水の淡水化に要するエネルギーを低減しつつ、高濃度塩水を逆浸透膜装置に供給することにより、バイオファウリングを十分に抑制できる。したがって、本発明は、海水の淡水化に要するエネルギーを低減するとともに、バイオファウリングを十分に抑制することができる海水淡水化方法及び海水淡水化装置を提供することができる。   According to the seawater desalination method and seawater desalination apparatus according to another aspect of the present invention, non-halophilic organisms are grown by supplying high-concentration salt water having a salt concentration of more than 0.2M to the reverse osmosis membrane apparatus. It becomes difficult atmosphere. For this reason, high concentration salt water is supplied to a reverse osmosis membrane apparatus, reducing the energy required for seawater desalination by the process of filtering low concentration salt water having a salt concentration of 0.2 M or less with a reverse osmosis membrane apparatus. Thus, biofouling can be sufficiently suppressed. Therefore, this invention can provide the seawater desalination method and seawater desalination apparatus which can fully suppress biofouling while reducing the energy required for seawater desalination.

上記海水淡水化方法において好ましくは、高濃度塩水を逆浸透膜装置に供給してろ過処理する工程を一時的に実施する。   In the seawater desalination method, preferably, a step of supplying high-concentration salt water to the reverse osmosis membrane device and performing a filtration treatment is temporarily performed.

これにより、定常時は低濃度塩水を逆浸透膜装置に供給することができるので、海水の淡水化に要するエネルギーをより低減できる海水淡水化方法を提供することができる。   Thereby, since low concentration salt water can be supplied to a reverse osmosis membrane apparatus at the time of steady state, the sea water desalination method which can reduce more the energy required for sea water desalination can be provided.

ここで、本明細書において塩濃度の単位として用いている「Ｍ」とはモル体積濃度のことであり、物質量を全体量の体積で除したものである（ｍｏｌ／Ｌ）。例えば、０．５Ｍとは、１Ｌの溶液中に０．５ｍｏｌの塩が溶解していることを示す。   Here, “M” used as a unit of salt concentration in the present specification is molar volume concentration, and is obtained by dividing the amount of substance by the volume of the total amount (mol / L). For example, 0.5M indicates that 0.5 mol of salt is dissolved in 1 L of solution.

以上のように、本発明によれば、海水の淡水化に要するエネルギーを低減するとともに、バイオファウリングを十分に抑制することができる海水淡水化方法及び海水淡水化装置を提供することができる。   As described above, according to the present invention, it is possible to provide a seawater desalination method and a seawater desalination apparatus capable of reducing energy required for seawater desalination and sufficiently suppressing biofouling.

本発明の実施の形態における海水淡水化装置の模式図である。It is a schematic diagram of the seawater desalination apparatus in embodiment of this invention. 本発明の実施の形態の変形例における海水淡水化装置の模式図である。It is a schematic diagram of the seawater desalination apparatus in the modification of embodiment of this invention. 本発明の実施の形態における海水淡水化方法及び海水淡水化装置の効果を説明するための図である。It is a figure for demonstrating the effect of the seawater desalination method and seawater desalination apparatus in embodiment of this invention.

以下、図面に基づいて本発明の実施の形態を説明する。なお、以下の図面において同一または相当する部分には同一の参照符号を付しその説明は繰り返さない。   Hereinafter, embodiments of the present invention will be described with reference to the drawings. In the following drawings, the same or corresponding parts are denoted by the same reference numerals, and description thereof will not be repeated.

まず、図１を参照して、本発明の一実施の形態における海水淡水化装置１０について説明する。本実施の形態の海水淡水化装置１０は、逆浸透（ＲＯ）膜を用いた逆浸透膜装置によるろ過処理によって海水を淡水化する装置である。   First, a seawater desalination apparatus 10 according to an embodiment of the present invention will be described with reference to FIG. The seawater desalination apparatus 10 of this Embodiment is an apparatus which desalinates seawater by the filtration process by the reverse osmosis membrane apparatus using a reverse osmosis (RO) membrane.

海水淡水化装置１０は、生物処理槽１１と、第１の除濁部１２と、第１の加圧部１３と、第１の逆浸透膜装置１４と、第２の除濁装置１５と、混合部１６と、第２の加圧部１７と、第２の逆浸透膜装置１８とを備えている。第１の除濁部１２は、生物処理槽１１に収容されている。第１の逆浸透膜装置１４は、第１の加圧部１３を介して、第１の除濁部１２と配管等により接続されている。第２の除濁装置１５は、海水Ａが通過する。混合部１６は、第１の逆浸透膜装置１４及び第２の除濁装置１５のそれぞれと配管や中継槽等により接続されている。第２の逆浸透膜装置１８は、第２の加圧部１７を介して、混合部１６と配管等により接続されている。   The seawater desalination apparatus 10 includes a biological treatment tank 11, a first turbidity removal unit 12, a first pressurization unit 13, a first reverse osmosis membrane device 14, a second turbidity removal device 15, A mixing unit 16, a second pressure unit 17, and a second reverse osmosis membrane device 18 are provided. The first turbidity removal unit 12 is accommodated in the biological treatment tank 11. The first reverse osmosis membrane device 14 is connected to the first turbidity removing unit 12 through a first pressurizing unit 13 and a pipe or the like. Seawater A passes through the second turbidity removal device 15. The mixing unit 16 is connected to each of the first reverse osmosis membrane device 14 and the second turbidity removal device 15 by a pipe, a relay tank, or the like. The second reverse osmosis membrane device 18 is connected to the mixing unit 16 by piping or the like via the second pressure unit 17.

生物処理槽１１は、細菌、原生動物、後生動物等の生物種によって水に含まれる有機物が分解される処理が行われる。このような処理として、例えば、活性汚泥を用いた曝気処理等を挙げることができる。   The biological treatment tank 11 is subjected to a treatment in which organic substances contained in water are decomposed by biological species such as bacteria, protozoa, and metazoans. Examples of such treatment include aeration treatment using activated sludge.

第１の除濁部１２は、生物処理水をろ過するためのものであり、ＲＯ膜よりも粗いろ過、即ち、ＲＯ膜で分離するよりも粗い不純物（例えば固形物質等）を除去し、第１の逆浸透膜装置１４の前処理装置である。第１の除濁部１２は、生物処理槽１１内の液面下に浸漬されており、例えば、精密ろ過膜（ＭＦ膜）及び限外ろ過膜（ＵＦ膜）の少なくともいずれか一方を有する。   The first turbidity removing unit 12 is for filtering biologically treated water, and removes impurities that are coarser than the RO membrane, that is, removes impurities (eg, solid substances) that are coarser than those separated by the RO membrane. 1 is a pretreatment device for the reverse osmosis membrane device 14 of FIG. The 1st turbidity part 12 is immersed under the liquid level in the biological treatment tank 11, for example, has at least any one of a microfiltration membrane (MF membrane) and an ultrafiltration membrane (UF membrane).

第１の加圧部１３は、第１の除濁部１２で粗い不純物がろ過された生物処理水を加圧する。第１の加圧部１３は、例えばポンプである。   The first pressurizing unit 13 pressurizes the biologically treated water from which coarse impurities are filtered by the first turbidity removing unit 12. The first pressure unit 13 is, for example, a pump.

第１の逆浸透膜装置１４は、加圧された生物処理水が供給され、この生物処理水をＲＯ膜により、透過水たる浄化水Ｃと、塩濃度が相対的に高い濃縮水とに分離する。第１の逆浸透膜装置１４は、例えば、ＲＯ膜と、このＲＯ膜を収容する圧力容器とを有している。本明細書におけるＲＯ膜は、ナノろ過膜（ＮＦ膜）を含む概念である。   The first reverse osmosis membrane device 14 is supplied with pressurized biologically treated water, and the biologically treated water is separated into purified water C as permeate and concentrated water having a relatively high salt concentration by the RO membrane. To do. The first reverse osmosis membrane device 14 has, for example, an RO membrane and a pressure vessel that accommodates the RO membrane. The RO membrane in this specification is a concept including a nanofiltration membrane (NF membrane).

第２の除濁装置１５は、海水をろ過するためのものであり、ＲＯ膜よりも粗い不純物を除去し、第２の逆浸透膜装置１８の前処理装置である。第２の除濁装置１５は、例えば、ＭＦ膜および限外ろ過膜の少なくともいずれか一方の除濁手段と、この除濁手段を収容する容器とを有しているが、砂ろ過や凝集沈殿による除濁手段を有するように構成されてもよい。   The second turbidity removal device 15 is for filtering seawater, removes impurities that are coarser than the RO membrane, and is a pretreatment device for the second reverse osmosis membrane device 18. The second turbidity removal device 15 has, for example, at least one of MF turbidity and ultrafiltration membrane turbidity and a container that accommodates this turbidity, but sand filtration or coagulation sedimentation It may be configured to have turbidity removing means.

混合部１６は、低濃度塩水を生成することと、高濃度塩水を生成することとが可能なように構成されている。低濃度塩水とは、第１の逆浸透膜装置１４から生成される濃縮水と、第２の除濁装置１５で粗い不純物が除去された海水とを混合することにより得られる混合水で、生物処理水中の生物の生育可能な塩濃度上限値以下の塩濃度を有する水である。高濃度塩水とは、第１の逆浸透膜装置１４から生成される濃縮水と、海水とを混合することにより、または、海水のみを用いることにより、生物処理水中の生物の生育可能な塩濃度上限値を超える塩濃度を有する水である。
具体的には、非好塩性生物及び低度好塩性生物の生育を十分に抑制する場合には、低濃度塩水は０．５Ｍ以下の塩濃度を有する水であり、高濃度塩水は０．５Ｍを超える塩濃度を有する水である。
低濃度塩水の塩濃度は、低ければ低い程よく、高濃度塩水の塩濃度は、高ければ高い程よい。実際的には、高濃度塩水が０．５Ｍを超えると共に低濃度塩水が０．５Ｍ以下である場合には、生物処理水と海水との混合上、低濃度塩水は０．２Ｍ以上０．５Ｍ以下であることが好ましく、日本近海の海水の塩濃度が０．６Ｍ程度（３．５％）であり、日本近海以外の海では０．８Ｍ程度（４．５％）の所もあることを考慮すれば、高濃度塩水は０．５Ｍを超えて０．８Ｍ以下であることが好ましく、０．５Ｍを超えて０．６Ｍ以下であることがより好ましい。 The mixing unit 16 is configured to generate low-concentration salt water and high-concentration salt water. Low-concentration salt water is mixed water obtained by mixing concentrated water produced from the first reverse osmosis membrane device 14 and seawater from which coarse impurities have been removed by the second turbidity removal device 15, It is water having a salt concentration that is equal to or lower than the salt concentration upper limit value at which organisms can grow in the treated water. The high-concentration salt water is a salt concentration capable of growing organisms in biologically treated water by mixing the concentrated water generated from the first reverse osmosis membrane device 14 and seawater or using only seawater. Water having a salt concentration exceeding the upper limit.
Specifically, in the case of sufficiently suppressing the growth of non-halophilic organisms and low-halogenated organisms, low-concentration salt water is water having a salt concentration of 0.5 M or less, and high-concentration salt water is 0. Water with a salt concentration above 5M.
The lower the salt concentration of the low-concentration salt water, the better. The higher the salt concentration of the high-concentration salt water, the better. Actually, when the high-concentration salt water exceeds 0.5 M and the low-concentration salt water is 0.5 M or less, the low-concentration salt water is 0.2 M or more and 0.5 M in terms of mixing the biologically treated water and seawater. It is preferable that the salt concentration of seawater in the sea near Japan is about 0.6M (3.5%), and that there is about 0.8M (4.5%) in seas other than Japan. In consideration, the high-concentration salt water is preferably more than 0.5M and 0.8M or less, more preferably more than 0.5M and 0.6M or less.

なお、生物処理水中の生物として非好塩性生物及び低度好塩性生物の生育可能な塩濃度上限値は０．５Ｍであり、生物処理水中の生物として非好塩性生物の生育可能な塩濃度上限値は０．２Ｍである。このため、非好塩性生物の生育を十分に抑制する場合には、低濃度塩水は０．２Ｍ以下の塩濃度を有し、高濃度塩水は０．２Ｍを超える塩濃度を有する。   It should be noted that the upper limit of the salt concentration at which non-halophilic organisms and low-halogenated organisms can grow as organisms in biologically treated water is 0.5 M, and non-halogenous organisms can grow as organisms in biologically treated water. The upper limit of salt concentration is 0.2M. For this reason, in the case of sufficiently suppressing the growth of non-halophilic organisms, the low-concentration salt water has a salt concentration of 0.2M or less, and the high-concentration salt water has a salt concentration exceeding 0.2M.

混合部１６は、例えば、低濃度塩水及び高濃度塩水を貯留可能な貯留槽であり、第１の逆浸透膜装置１４から濃縮水が導入される濃縮水導入部と、海水が導入される海水導入部と、低濃度塩水または高濃度塩水を第２の逆浸透膜装置１８へ排出する排出部とを含んでいる。濃縮導入部及び海水導入部は、混合部に導入される量を調整することが可能なように、例えば、開口度を調整できるように構成されている。   The mixing unit 16 is, for example, a storage tank capable of storing low-concentration salt water and high-concentration salt water, and a concentrated water introduction unit into which concentrated water is introduced from the first reverse osmosis membrane device 14 and seawater into which seawater is introduced. An introduction part and a discharge part for discharging low-concentration salt water or high-concentration salt water to the second reverse osmosis membrane device 18 are included. The concentration introduction part and the seawater introduction part are configured such that the opening degree can be adjusted, for example, so that the amount introduced into the mixing part can be adjusted.

混合部１６では、第２の逆浸透膜装置１８に供給する供給水の塩濃度が０．５Ｍ以下から０．５Ｍを超えるように生物処理水（本実施の形態では濃縮水）と海水との混合比を変更することが可能なように構成されている。本実施の形態では、混合部１６において、濃縮水導入部及び海水導入部の開口度を調整して、供給水の塩濃度を調整することが可能であるため、排出部から第２の逆浸透膜装置１８に供給する供給水を０．５Ｍ以下の塩濃度と、０．５Ｍを超える塩濃度とに選択できる。   In the mixing unit 16, the biological treatment water (concentrated water in the present embodiment) and seawater are supplied so that the salt concentration of the supply water supplied to the second reverse osmosis membrane device 18 exceeds 0.5M or less and exceeds 0.5M. The mixing ratio can be changed. In the present embodiment, in the mixing unit 16, it is possible to adjust the opening degree of the concentrated water introduction unit and the seawater introduction unit to adjust the salt concentration of the supply water, so that the second reverse osmosis from the discharge unit. The supply water supplied to the membrane device 18 can be selected between a salt concentration of 0.5M or less and a salt concentration exceeding 0.5M.

なお、非好塩性生物及び低度好塩性生物の生育を十分に抑制する場合には、混合部１６は、０．２Ｍ以下の塩濃度を有する低濃度塩水を生成することと、０．２Ｍを超える塩濃度を有する高濃度塩水を生成することとが可能なように構成されている。   In the case where the growth of non-halophilic organisms and low-degree halophilic organisms is sufficiently suppressed, the mixing unit 16 generates low-concentration salt water having a salt concentration of 0.2 M or less; It is configured to be able to generate high-concentration salt water having a salt concentration exceeding 2M.

また、混合部１６は、濃縮水の供給を停止して、海水のみを第２の逆浸透膜装置１８に供給することが可能なように構成されている。混合部１６において海水のみを生成することは、混合部１６において、濃縮水導入部を閉口し、海水導入部のみを開口することで、実現できる。この場合、混合部１６の排出部から第２の逆浸透膜装置１８に供給する水の塩濃度を高めることができる。   Further, the mixing unit 16 is configured to be able to stop the supply of concentrated water and supply only seawater to the second reverse osmosis membrane device 18. It is possible to generate only seawater in the mixing unit 16 by closing the concentrated water introduction unit and opening only the seawater introduction unit in the mixing unit 16. In this case, the salt concentration of the water supplied to the 2nd reverse osmosis membrane apparatus 18 from the discharge part of the mixing part 16 can be raised.

混合部１６には、上記のように供給水の塩濃度の制御をするために、供給水の塩濃度を測定する測定部がさらに設けられていてもよい。
また、海水淡水化装置１０は、供給水の塩濃度を測定する測定部の値及び後述する第２の逆浸透膜装置１８のＲＯ膜の状態に応じて、供給水の塩濃度を制御する制御部をさらに備えていてもよい。 The mixing unit 16 may further include a measurement unit that measures the salt concentration of the feed water in order to control the salt concentration of the feed water as described above.
In addition, the seawater desalination apparatus 10 controls the salt concentration of the supplied water according to the value of the measurement unit that measures the salt concentration of the supplied water and the state of the RO membrane of the second reverse osmosis membrane device 18 described later. A part may be further provided.

第２の加圧部１７は、混合部１６で生成された供給水を加圧する。第２の加圧部１７は、例えばポンプである。   The second pressurizing unit 17 pressurizes the supply water generated by the mixing unit 16. The second pressure unit 17 is, for example, a pump.

第２の逆浸透膜装置１８は、加圧された低濃度塩水または高濃度塩水が供給され、この水をＲＯ膜により、透過水たる淡水Ｅと、濃縮水Ｄとに分離する。第２の逆浸透膜装置１８は、例えば、ＲＯ膜と、このＲＯ膜を収容する圧力容器とを有している。第２の逆浸透膜装置１８のＲＯ膜と、第１の逆浸透膜装置１４のＲＯ膜とは同一であってもよく、異なっていてもよい。   The second reverse osmosis membrane device 18 is supplied with pressurized low-concentration salt water or high-concentration salt water, and separates this water into permeated fresh water E and concentrated water D by the RO membrane. The second reverse osmosis membrane device 18 includes, for example, an RO membrane and a pressure vessel that accommodates the RO membrane. The RO membrane of the second reverse osmosis membrane device 18 and the RO membrane of the first reverse osmosis membrane device 14 may be the same or different.

第２の逆浸透膜装置１８により製造された淡水Ｅと、第１の逆浸透膜装置１４により浄化された浄化水Ｃとは混合されてもよく（図示せず）、混合されなくてもよい。   The fresh water E produced by the second reverse osmosis membrane device 18 and the purified water C purified by the first reverse osmosis membrane device 14 may be mixed (not shown) or may not be mixed. .

なお、第１の逆浸透膜装置１４は省略されてもよい。この場合、第１の除濁部１２は、例えば、混合部１６と接続される。   Note that the first reverse osmosis membrane device 14 may be omitted. In this case, the 1st turbidity removal part 12 is connected with the mixing part 16, for example.

続いて、図１を参照して、本実施の形態における海水淡水化方法について説明する。本実施の形態の海水淡水化方法は、図１に示す海水淡水化装置１０を用いて、ＲＯ膜を用いた逆浸透膜装置によるろ過処理によって海水を淡水化する方法である。   Then, with reference to FIG. 1, the seawater desalination method in this Embodiment is demonstrated. The seawater desalination method of the present embodiment is a method of desalinating seawater by filtration using a reverse osmosis membrane device using an RO membrane, using the seawater desalination device 10 shown in FIG.

まず、有機性廃水Ｂを生物処理槽１１に供給する。有機性廃水Ｂは、有機物を含む廃水であり、例えば、有機物濃度の指標としてのＢＯＤ（生物化学的酸素要求量）が２０００ｍｇ/Ｌ以下の廃水であり、より具体的には、２００ｍｇ／Ｌ程度の廃水である。また、有機性廃水Ｂは、海水よりも塩濃度が低い水である。有機性廃水Ｂは、例えば、海水Ａの塩濃度に対する有機性廃水Ｂの塩濃度の比が０．１以下のもの、より具体的には、海水Ａの塩濃度に対する有機性廃水Ｂの塩濃度の比が０．０１以下のものである。
有機性廃水Ｂとしては、下水（生活廃水や雨水が下水道に流れた水等）や、工業廃水（食品工場、化学工場、電子産業工場、パルプ工場等の工場から排出される廃水）等が挙げられる。 First, the organic waste water B is supplied to the biological treatment tank 11. The organic wastewater B is wastewater containing organic matter, for example, wastewater having a BOD (biochemical oxygen demand) as an indicator of organic matter concentration of 2000 mg / L or less, more specifically about 200 mg / L. Waste water. The organic waste water B is water having a lower salt concentration than seawater. The organic wastewater B has, for example, a ratio of the salt concentration of the organic wastewater B to the salt concentration of the seawater A of 0.1 or less, more specifically, the salt concentration of the organic wastewater B with respect to the salt concentration of the seawater A. The ratio is 0.01 or less.
Examples of organic wastewater B include sewage (such as water from which domestic wastewater and rainwater flow into the sewer) and industrial wastewater (wastewater discharged from factories such as food factories, chemical factories, electronics industry factories, and pulp factories). It is done.

次いで、生物処理槽１１で、有機性廃水を生物処理、即ち、細菌、原生動物、後生動物等の生物種によって水に含まれる有機物を分解処理する。生物処理として、例えば、活性汚泥を用いた曝気処理等を挙げることができる。   Next, in the biological treatment tank 11, the organic wastewater is biologically treated, that is, the organic matter contained in the water is decomposed by biological species such as bacteria, protozoa, and metazoans. Examples of biological treatment include aeration treatment using activated sludge.

次に、生物処理槽１１に収容された第１の除濁部１２で、生物処理水をろ過する。このろ過により、生物処理水中の固形物質等の粗い不純物を除去することができる。   Next, the biologically treated water is filtered by the first turbidity removing unit 12 accommodated in the biological treatment tank 11. By this filtration, coarse impurities such as solid substances in the biologically treated water can be removed.

次に、第１の除濁部１２で粗い不純物が除去された生物処理水を第１の加圧部１３で加圧する。生物処理水に加える圧力は特に限定されないが、第１の逆浸透膜装置１４で浄化水Ｃを得るために必要な圧力を加える。   Next, the biological treatment water from which coarse impurities have been removed by the first turbidity removing unit 12 is pressurized by the first pressurizing unit 13. The pressure applied to the biologically treated water is not particularly limited, but a pressure necessary for obtaining purified water C by the first reverse osmosis membrane device 14 is applied.

次に、第１の逆浸透膜装置１４で、加圧された生物処理水を、透過水たる浄化水Ｃと、濃縮水とに分離する。浄化水Ｃは、製造対象物である。濃縮水は、海水Ａよりも低い塩濃度を有するため、海水Ａの希釈液として用いる。   Next, in the first reverse osmosis membrane device 14, the pressurized biologically treated water is separated into purified water C as permeated water and concentrated water. The purified water C is a manufacturing object. Since concentrated water has a lower salt concentration than seawater A, it is used as a dilution of seawater A.

また、海水Ａを第２の除濁装置１５に供給する。海水Ａは、塩を含む水であり、例えば、塩濃度が１．０質量％以上８．０質量％以下の水であり、より具体的には、塩濃度が例えば２．５質量％以上６．０質量％以下である。
本明細書において、海水Ａは、海に存在する水に限定されず、塩濃度が１．０質量％以上の水であれば、湖（塩湖、汽水湖）の水、沼水、池水等の陸に存在する水も含む。また、海水Ａは、鹹（かん）水を含む。 Further, the seawater A is supplied to the second turbidity removal device 15. The seawater A is water containing salt, for example, water having a salt concentration of 1.0% by mass or more and 8.0% by mass or less, and more specifically, the salt concentration is, for example, 2.5% by mass or more and 6% by mass. 0.0 mass% or less.
In this specification, the seawater A is not limited to the water which exists in the sea, If it is water whose salt concentration is 1.0 mass% or more, the water of a lake (salt lake, brackish lake), swamp water, pond water, etc. Including water existing on the land. Moreover, the seawater A contains salt water.

次に、第１の逆浸透膜装置１４で生成された生物処理水由来の濃縮水と、第２の除濁装置１５で除濁された海水とを混合することにより、０．５Ｍ以下の塩濃度を有する低濃度塩水を生成する。さらに、この工程は、０．２Ｍ以上０．５Ｍ以下の塩濃度を有する低濃度塩水を生成することが好ましい。   Next, the salt of 0.5 M or less is obtained by mixing the concentrated water derived from the biologically treated water generated by the first reverse osmosis membrane device 14 and the seawater turbidized by the second turbidity removal device 15. Produces low-concentration brine with a concentration. Furthermore, it is preferable that this process produces | generates the low concentration salt water which has a salt concentration of 0.2M or more and 0.5M or less.

次に、低濃度塩水を第２の加圧部１７で加圧する。低濃度塩水に加える圧力は特に限定されないが、逆浸透膜装置１８で淡水Ｅを分離するのに必要な圧力を加える。第２の加圧部１７で低濃度塩水に加える圧力は、海水により塩濃度が高まることにより、第１の加圧部１３で加える圧力よりも大きい。   Next, the low-concentration salt water is pressurized by the second pressure unit 17. The pressure applied to the low-concentration salt water is not particularly limited, but a pressure necessary for separating the fresh water E by the reverse osmosis membrane device 18 is applied. The pressure applied to the low-concentration salt water by the second pressurizing unit 17 is larger than the pressure applied by the first pressurizing unit 13 as the salt concentration is increased by seawater.

次に、加圧された低濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する。この工程では、低濃度塩水を、透過水たる淡水Ｅと、濃縮水Ｄとに分離する。淡水Ｅは、海水淡水化における製造対象物である。濃縮水Ｄは、通常は放流される。   Next, the pressurized low-concentration salt water is supplied to the second reverse osmosis membrane device 18 and filtered. In this step, the low-concentration salt water is separated into fresh water E that is permeated water and concentrated water D. Fresh water E is a manufacturing object in seawater desalination. The concentrated water D is normally discharged.

なお、第１の逆浸透膜装置１４により浄化された浄化水Ｃと、第２の逆浸透膜装置１８により生成されて製造された淡水Ｅとは、混合されてもよく、混合されなくてもよい。   The purified water C purified by the first reverse osmosis membrane device 14 and the fresh water E produced and manufactured by the second reverse osmosis membrane device 18 may or may not be mixed. Good.

次に、第１の逆浸透膜装置１４で生成された生物処理水由来の濃縮水と、第２の除濁装置１５で生成された海水とを混合することにより、または海水のみを用いることにより、０．５Ｍを超える塩濃度を有する高濃度塩水を生成する。つまり、この工程では、塩濃度が０．５Ｍ以下の低濃度塩水から０．５Ｍを超えるように濃縮水と海水との混合比を変更する。この工程では、０．５Ｍを超えて０．８Ｍ以下の高濃度塩水を生成することが好ましく、０．５Ｍを超えて０．６Ｍ以下の高濃度塩水を生成することがより好ましい。   Next, by mixing concentrated biological water derived from the biologically treated water generated by the first reverse osmosis membrane device 14 and seawater generated by the second turbidity removal device 15, or by using only seawater , Producing high-concentration brine with a salt concentration greater than 0.5M. That is, in this step, the mixing ratio of the concentrated water and the seawater is changed so that the salt concentration exceeds 0.5 M from the low-concentration salt water with 0.5 M or less. In this step, it is preferable to generate high-concentration salt water of more than 0.5M and 0.8M or less, and more preferable to generate high-concentration salt water of more than 0.5M and 0.6M or less.

この工程において、海水のみを用いることで高濃度塩水を生成する場合には、混合部１６への濃縮水の供給を停止する。この場合、海水のみを第２の逆浸透膜装置１８に供給することになる。海水のみからなる高濃度塩水を供給する場合には、海水は生物処理水よりも塩濃度が高いため、塩濃度が０．５Ｍを超える高濃度塩水を容易に生成することができる。   In this step, when high-concentration salt water is generated by using only seawater, the supply of concentrated water to the mixing unit 16 is stopped. In this case, only seawater is supplied to the second reverse osmosis membrane device 18. When supplying high-concentration salt water consisting only of seawater, since seawater has a higher salt concentration than biologically treated water, a high-concentration saltwater with a salt concentration exceeding 0.5M can be easily generated.

次に、高濃度塩水を第２の加圧部１７で加圧する。高濃度塩水に加える圧力は特に限定されないが、第２の逆浸透膜装置１８で透過水たる淡水Ｅを分離可能な程度に、高濃度塩水に圧力を加える。第２の加圧部１７で高濃度塩水に加える圧力は、低濃度塩水に加える圧力よりも大きい。   Next, the high-concentration salt water is pressurized by the second pressure unit 17. The pressure applied to the high-concentration salt water is not particularly limited, but the pressure is applied to the high-concentration salt water to such an extent that the fresh water E that is permeated water can be separated by the second reverse osmosis membrane device 18. The pressure applied to the high-concentration salt water by the second pressurizing unit 17 is greater than the pressure applied to the low-concentration salt water.

次に、加圧された高濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する。この工程では、透過水たる淡水Ｅと、濃縮水Ｄとに分離する。淡水Ｅは、海水淡水化における製造対象物である。濃縮水Ｄは、通常は放流される。   Next, the pressurized high-concentration salt water is supplied to the second reverse osmosis membrane device 18 and filtered. In this step, fresh water E as permeated water and concentrated water D are separated. Fresh water E is a manufacturing object in seawater desalination. The concentrated water D is normally discharged.

次に、低濃度塩水を生成し、この低濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する低濃度運転工程と、高濃度塩水を生成し、この高濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する高濃度運転工程とを繰り返す。海水淡水化に要するエネルギーを低減するという目的からは、低濃度運転工程を定常運転とし、高濃度運転工程を一時的に実施することが好ましい。   Next, a low-concentration salt water is generated, the low-concentration salt water is supplied to the second reverse osmosis membrane device 18 and filtered, and a high-concentration salt water is generated. The high concentration operation process of supplying to the reverse osmosis membrane device 18 and performing the filtration treatment is repeated. For the purpose of reducing the energy required for seawater desalination, it is preferable that the low concentration operation step is a steady operation and the high concentration operation step is temporarily performed.

第２の逆浸透膜装置１８に供給する水（供給水）の塩濃度は、例えば、第２の逆浸透膜装置１８に向けて排出する排出部において、塩濃度計や電気伝導計などにより測定することができる。このように測定される塩濃度に応じて、低濃度塩水及び高濃度塩水の制御ができる。   The salt concentration of water (supply water) supplied to the second reverse osmosis membrane device 18 is measured by a salt concentration meter, an electric conductivity meter, or the like, for example, at a discharge portion that discharges toward the second reverse osmosis membrane device 18. can do. The low-concentration salt water and the high-concentration salt water can be controlled according to the salt concentration thus measured.

なお、本実施の形態の海水淡水化方法において、生物処理水中の生物として非好塩性生物及び低度好塩性生物を十分に抑制する場合を説明したが、非好塩性生物の生育を十分に抑制する場合には、本発明の海水淡水化方法は、０．２Ｍ以下の塩濃度を有する低濃度塩水を第２の逆浸透膜装置１８に供給する工程と、０．２Ｍを超える塩濃度を有する高濃度塩水を第２の逆浸透膜装置１８に供給する工程とを備える。   In the seawater desalination method of the present embodiment, the case where non-halophilic organisms and low-degree halophilic organisms are sufficiently suppressed as organisms in biologically treated water has been described. When sufficiently suppressing, the seawater desalination method of the present invention includes a step of supplying low-concentration salt water having a salt concentration of 0.2M or less to the second reverse osmosis membrane device 18, and a salt exceeding 0.2M. And a step of supplying high-concentration salt water having a concentration to the second reverse osmosis membrane device 18.

（変形例）
図２を参照して、本実施の形態の変形例における海水淡水化装置２０及び海水淡水化方法を説明する。 (Modification)
With reference to FIG. 2, the seawater desalination apparatus 20 and the seawater desalination method in the modification of this Embodiment are demonstrated.

変形例の海水淡水化装置２０は、基本的には図１に示す実施の形態１の海水淡水化装置１０と同様であるが、生物処理槽１１内に収容された除濁部１２の代わりに、生物処理槽１１外に第１の除濁装置２１を備えている点において異なる。第１の除濁装置２１は、例えば、ＭＦ膜および限外ろ過膜の少なくともいずれか一方の除濁手段と、この除濁手段を収容する容器とを有しているが、砂ろ過や凝集沈殿による除濁手段を有するように構成されてもよい。   The seawater desalination apparatus 20 of the modified example is basically the same as the seawater desalination apparatus 10 of Embodiment 1 shown in FIG. 1, but instead of the turbidity removing unit 12 accommodated in the biological treatment tank 11. The difference is that the first turbidity removal device 21 is provided outside the biological treatment tank 11. The first turbidity removal device 21 has, for example, at least one of MF turbidity and ultrafiltration membrane, and a container that accommodates the turbidity, but sand filtration or coagulation sedimentation It may be configured to have turbidity removing means.

変形例の海水淡水化方法は、基本的には実施の形態１の海水淡水化方法と同様であるが、生物処理槽１１に収容された第１の除濁部１２で生物処理水をろ過する代わりに、第１の除濁装置２１で生物処理水をろ過する点において異なる。   The seawater desalination method of the modified example is basically the same as the seawater desalination method of the first embodiment, but the biologically treated water is filtered by the first turbidity removing unit 12 accommodated in the biological treatment tank 11. Instead, it differs in that the biologically treated water is filtered by the first turbidity removal device 21.

続いて、図１及び図３を参照して、本実施の形態の海水淡水化装置１０及び海水淡水化方法の効果について説明する。   Then, with reference to FIG.1 and FIG.3, the effect of the seawater desalination apparatus 10 and the seawater desalination method of this Embodiment is demonstrated.

図３に示すように、混合部１６から第２の逆浸透膜装置１８に供給する水（供給水）における海水の体積比率（海水混合比）が低いほど、供給水の塩濃度が低くなる。このため、供給水を加圧するエネルギーが海水のみからなる場合に比べて小さいので、得られる淡水Ｅの量当たりにおける、海水を淡水化するのに必要なエネルギー量を抑制できる。このように、要するエネルギーを低減するためには、海水混合比が小さいことが好ましい。   As shown in FIG. 3, the lower the volume ratio (seawater mixture ratio) of seawater in the water (supply water) supplied from the mixing unit 16 to the second reverse osmosis membrane device 18, the lower the salt concentration of the supply water. For this reason, since the energy which pressurizes supply water is small compared with the case where it consists only of seawater, the amount of energy required in order to desalinate seawater per quantity of the freshwater E obtained can be suppressed. Thus, in order to reduce the required energy, it is preferable that the seawater mixing ratio is small.

しかし、図３において、海水混合比が３０％以下の場合、即ち、供給水の塩濃度が０．２Ｍ以下の場合には、非好塩性の雰囲気であるので、非好塩性生物が生育可能である。海水混合比が３０％を超えて８０％以下の場合、即ち、供給水の塩濃度が０．２Ｍを超えて０．５Ｍ以下の場合には、低度好塩性の雰囲気であるので、低度好塩性生物が生育可能である。
ここで、供給水中に存在する生物について説明する。生物を耐塩性で分類すると、高度好塩性生物と、中度好塩性生物と、低度好塩性生物と、非好塩性生物とに分かれる。高度好塩性生物は、至適増殖ＮａＣｌ濃度が２．５Ｍを超える生物である。中度好塩性生物は、至適増殖ＮａＣｌ濃度が０．５Ｍを超えて２．５Ｍ以下であり、様々な含塩試料から分離される細菌が該当する。低度好塩性生物は、至適増殖ＮａＣｌ濃度が０．２Ｍを超えて０．５Ｍ以下であり、例えば、海洋性の高等生物や細菌が該当する。非好塩性生物は、至適増殖ＮａＣｌ濃度が０Ｍを超えて０．２Ｍ以下であり、多くの高等生物や土壌細菌が該当する。 However, in FIG. 3, when the seawater mixing ratio is 30% or less, that is, when the salt concentration of the feed water is 0.2M or less, the atmosphere is non-halogenous, so that non-halophilic organisms grow. Is possible. When the seawater mixing ratio is more than 30% and 80% or less, that is, when the salt concentration of the feed water is more than 0.2M and 0.5M or less, the atmosphere is low in halophilicity. A moderately halophilic organism can grow.
Here, the living thing which exists in supply water is demonstrated. When organisms are classified by salt tolerance, they are divided into highly halophilic organisms, moderately halophilic organisms, lowly halophilic organisms, and non-halophilic organisms. Highly halophilic organisms are organisms with optimal growth NaCl concentrations above 2.5M. The moderately halophilic organisms include bacteria that have an optimal growth NaCl concentration of more than 0.5M and not more than 2.5M, and are separated from various salt-containing samples. The low-degree halophilic organism has an optimal growth NaCl concentration of more than 0.2M and 0.5M or less, and examples include marine higher organisms and bacteria. Non-halophilic organisms have an optimal growth NaCl concentration of more than 0 M and not more than 0.2 M, and many higher organisms and soil bacteria are applicable.

仮に、海水の塩濃度が３．５％である場合、ＮａＣｌ（ＭＷ：モル質量＝５８．４４）換算で０．６Ｍになる。また、生物処理水の塩濃度が０．０２４％である場合、ＮａＣｌ換算で０．００４Ｍとなり、第１の除濁部１２及び第１の逆浸透膜装置１４によるろ過処理をして得られる濃縮水の塩濃度は０．０２Ｍ程度である。
図３に示すように、海水混合比が０％の場合、即ち、供給水が生物処理水由来の濃縮水のみ（濃縮水１００％）の場合、供給水の塩濃度は０．０２Ｍである。海水混合比が２０％の場合、即ち、供給水が海水２０％で濃縮水８０％の場合、供給水の塩濃度は０．１２Ｍである。海水混合比が４０％の場合、即ち、供給水が海水４０％で濃縮水６０％の場合、供給水の塩濃度は０．２４Ｍである。海水混合比が６０％の場合、即ち、供給水が海水６０％で濃縮水４０％の場合、供給水の塩濃度は０．３６Ｍである。海水混合比が８０％の場合、即ち、供給水が海水８０％で濃縮水２０％の場合、供給水の塩濃度は０．５０Ｍである。海水混合比が１００％の場合、即ち、供給水が海水のみ（海水１００％）の場合、供給水の塩濃度は０．６０Ｍである。 If the salt concentration of seawater is 3.5%, it becomes 0.6 M in terms of NaCl (MW: molar mass = 58.44). Moreover, when the salt concentration of biologically treated water is 0.024%, it becomes 0.004M in terms of NaCl, and is obtained by filtration through the first turbidity removing unit 12 and the first reverse osmosis membrane device 14. The salt concentration of water is about 0.02M.
As shown in FIG. 3, when the seawater mixing ratio is 0%, that is, when the supply water is only concentrated water derived from biologically treated water (concentrated water 100%), the salt concentration of the supply water is 0.02M. When the seawater mixing ratio is 20%, that is, when the supply water is 20% seawater and 80% concentrated water, the salt concentration of the supply water is 0.12M. When the seawater mixing ratio is 40%, that is, when the supply water is 40% seawater and 60% concentrated water, the salt concentration of the supply water is 0.24M. When the seawater mixing ratio is 60%, that is, when the supply water is 60% seawater and 40% concentrated water, the salt concentration of the supply water is 0.36M. When the seawater mixing ratio is 80%, that is, when the supply water is 80% seawater and 20% concentrated water, the salt concentration of the supply water is 0.50M. When the seawater mixing ratio is 100%, that is, when the supply water is only seawater (seawater 100%), the salt concentration of the supply water is 0.60M.

生物の生育は、至適増殖ＮａＣｌ濃度の範囲外では十分に抑制され、特に至適増殖ＮａＣｌ濃度よりも高くなると効果的に抑制され、死滅する場合もある。このため、図３に示すように、供給水の海水混合比が３０％以下である場合には、供給水の塩濃度は０．２Ｍ以下であるので、非好塩性生物は生育可能である。また、供給水の海水混合比が３０％を超え８０％以下である場合には、供給水の塩濃度は０．２Ｍを超え０．５Ｍ以下であるので、低度好塩性生物は生育可能である。しかし、供給水の塩濃度が０．５Ｍを超えるように海水の比率を高めると、非好塩性生物及び低度好塩性生物の生育が十分に抑制される。生物処理水には非好塩性生物及び低度好塩性生物が相対的に多く含まれているので、供給水の塩濃度が０．５Ｍ以下から０．５Ｍを超えるように生物処理水由来の濃縮水と海水との混合比を変更することにより、非好塩性生物及び低度好塩性生物の生育を十分に抑制できるので、第２の逆浸透膜装置１８を構成するＲＯ膜においてバイオファウリングを十分に抑制することができる。なお、供給水の海水混合比が３０％以下である場合には、供給水の塩濃度が０．２Ｍを超えるように海水の比率を高めて、非好塩性生物の生育を十分に抑制してもよい。
仮に、バイオファウリングによる有機物の付着であるバイオフィルムが形成されていても、供給水中の海水及び濃縮水の比率を変更することで、生物にショックを与えることができると共に、適応する微生物の種類を変化させることができるので、バイオフィルムが剥がれ易くなり、場合によってはバイオフィルムが剥がれることもある。
バイオファウリングを十分に抑制できると、ＲＯ膜を洗浄する回数を低減することができ、バイオファウリング抑制剤の使用量を低減することができる。その結果、ＲＯ膜を長期間使用することができるので、海水及び有機性廃水から淡水を生成する効率を高めることができる。 The growth of the organism is sufficiently suppressed outside the range of the optimal growth NaCl concentration, and is effectively suppressed and may be killed particularly when the concentration is higher than the optimal growth NaCl concentration. For this reason, as shown in FIG. 3, when the seawater mixing ratio of the feed water is 30% or less, the salt concentration of the feed water is 0.2 M or less, so that non-halophilic organisms can grow. . In addition, when the seawater mixing ratio of the feed water is more than 30% and 80% or less, the salt concentration of the feed water is more than 0.2M and less than 0.5M, so that low-halophilic organisms can grow. It is. However, if the ratio of the seawater is increased so that the salt concentration of the feed water exceeds 0.5M, the growth of non-halophilic organisms and low-halogenated organisms is sufficiently suppressed. Since the biologically treated water contains a relatively large amount of non-halophilic organisms and low-level halophilic organisms, it is derived from biologically treated water so that the salt concentration of the feed water exceeds 0.5M to 0.5M. Since the growth of non-halophilic organisms and low-halophilic organisms can be sufficiently suppressed by changing the mixing ratio of the concentrated water and seawater, in the RO membrane constituting the second reverse osmosis membrane device 18 Biofouling can be sufficiently suppressed. In addition, when the seawater mixing ratio of the feed water is 30% or less, the ratio of the seawater is increased so that the salt concentration of the feed water exceeds 0.2M to sufficiently suppress the growth of non-halophilic organisms. May be.
Even if a biofilm, which is the attachment of organic matter due to biofouling, is formed, it is possible to shock organisms by changing the ratio of seawater and concentrated water in the supply water, and the types of microorganisms to be adapted Therefore, the biofilm is easily peeled off, and in some cases, the biofilm may be peeled off.
If biofouling can be sufficiently suppressed, the number of times of washing the RO membrane can be reduced, and the amount of biofouling inhibitor used can be reduced. As a result, since the RO membrane can be used for a long time, the efficiency of generating fresh water from seawater and organic wastewater can be increased.

したがって、生物処理水由来の濃縮水の比率が高い状態での運転時（塩濃度が０．５Ｍ以下の低濃度塩水をＲＯ膜でろ過処理する時）には、要するエネルギーを低減し、海水の比率が高い状態での運転（塩濃度が０．５Ｍを超える高濃度塩水をＲＯ膜でろ過処理する）時には、バイオファウリングを十分に抑制できる。このため、この２つの状態の運転を輪番で行うことにより、海水の淡水化に要するエネルギーを低減するとともに、バイオファウリングを十分に抑制することができる。
なお、非好塩性生物の生育を十分に抑制する場合には、生物処理水由来の濃縮水の比率が高い状態での運転時とは、塩濃度が０．２Ｍ以下の低濃度塩水をＲＯ膜でろ過処理する時であり、海水の比率が高い状態での運転とは、塩濃度が０．２Ｍを超える高濃度塩水をＲＯ膜でろ過処理する時である。 Therefore, during operation with a high ratio of concentrated water derived from biologically treated water (when low-concentration salt water with a salt concentration of 0.5 M or less is filtered through an RO membrane), the energy required is reduced, Biofouling can be sufficiently suppressed during operation in a high ratio state (high-concentration salt water with a salt concentration exceeding 0.5 M is filtered with an RO membrane). For this reason, by performing the driving | running | working of these two states with a rotation number, while reducing the energy required for desalination of seawater, biofouling can fully be suppressed.
In the case of sufficiently suppressing the growth of non-halophilic organisms, when operating with a high ratio of concentrated water derived from biologically treated water, low concentration brine with a salt concentration of 0.2 M or less is RO. The time when the membrane is filtered and the operation in a state where the ratio of seawater is high is when the high-concentration salt water having a salt concentration exceeding 0.2M is filtered by the RO membrane.

特に、基本的には塩濃度を０．５Ｍ（非好塩性生物の生育を十分に抑制する場合には０．２Ｍ）以下の低濃度塩水を第２の逆浸透膜装置１８に供給し、一時的に混合水の塩濃度が０．５Ｍ（非好塩性生物の生育を十分に抑制する場合には０．２Ｍ）を超える高濃度塩水を第２の逆浸透膜装置１８に供給するように生物処理水由来の濃縮水と海水との混合比を変更することが好ましい。なお、「一時的に」とは、高濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する工程の実施時間が、低濃度塩水をＲＯ膜に供給してろ過処理する工程の実施時間よりも短いことを意味する。高濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する工程は、例えば、第２の逆浸透膜装置１８を構成するＲＯ膜の詰り具合に応じて、または、非好塩性生物及び低度好塩性生物の生存期間に応じて、所定のタイミング及び所定の期間実施する。具体的には、高濃度塩水を第２の逆浸透膜装置１８に供給してろ過処理する工程は、例えば、２日に１回、３０分程度実施されることが好ましい。   In particular, a low-concentration salt water having a salt concentration of 0.5 M or less (0.2 M when sufficiently suppressing the growth of non-halophilic organisms) is basically supplied to the second reverse osmosis membrane device 18, A high-concentration salt water in which the salt concentration of the mixed water temporarily exceeds 0.5 M (0.2 M when sufficiently suppressing the growth of non-halophilic organisms) is supplied to the second reverse osmosis membrane device 18. It is preferable to change the mixing ratio of concentrated water derived from biologically treated water and seawater. “Temporarily” means that the time for supplying the high-concentration salt water to the second reverse osmosis membrane device 18 and performing the filtration process is the time for supplying the low-concentration salt water to the RO membrane and performing the filtration process. Means shorter than the implementation time. The step of supplying high-concentration salt water to the second reverse osmosis membrane device 18 and performing the filtration treatment is performed according to, for example, the degree of clogging of the RO membrane constituting the second reverse osmosis membrane device 18 or non-halophilic Depending on the life of the organism and the low halophilic organism, it is carried out at a predetermined timing and for a predetermined period. Specifically, the step of supplying the high-concentration salt water to the second reverse osmosis membrane device 18 and performing the filtration treatment is preferably performed once every two days for about 30 minutes, for example.

今回開示された実施の形態はすべての点で例示であって制限的なものではないと考えられるべきである。本発明の範囲は上記した実施の形態ではなくて特許請求の範囲によって示され、特許請求の範囲と均等の意味及び範囲内でのすべての変更が含まれることが意図される。   The embodiment disclosed this time should be considered as illustrative in all points and not restrictive. The scope of the present invention is shown not by the above-described embodiment but by the scope of claims, and is intended to include all modifications within the meaning and scope equivalent to the scope of claims.

１０ 海水淡水化装置、１１ 生物処理槽、１２ 第１の除濁部、１３ 第１の加圧部、１４ 第１の逆浸透膜装置、１５ 第２の除濁装置、１６ 混合部、１７ 第２の加圧部、１８ 第２の逆浸透膜装置、２１ 第１の除濁装置、Ａ 海水、Ｂ 有機性廃水、Ｃ 浄化水、Ｄ 濃縮水、Ｅ 淡水。   DESCRIPTION OF SYMBOLS 10 Seawater desalination apparatus, 11 Biological treatment tank, 12 1st turbidity part, 13 1st pressurization part, 14 1st reverse osmosis membrane apparatus, 15 2nd turbidity removal apparatus, 16 Mixing part, 17 1st 2 pressurizing sections, 18 second reverse osmosis membrane device, 21 first turbidity removal device, A seawater, B organic waste water, C purified water, D concentrated water, E fresh water.

Claims (3)

逆浸透膜装置を用いたろ過処理によって海水を淡水化する海水淡水化方法であって、
有機性廃水を生物処理して得られる生物処理水と前記海水とを混合することにより、０．２Ｍ以下の塩濃度を有する低濃度塩水を生成し、前記低濃度塩水を前記逆浸透膜装置に供給してろ過処理する工程と、
前記生物処理水と前記海水とを混合することにより、または前記海水のみを用いることにより、０．２Ｍを超える塩濃度を有する高濃度塩水を生成し、前記高濃度塩水を前記逆浸透膜装置に供給してろ過処理する工程とを備える、海水淡水化方法。 A seawater desalination method for desalinating seawater by filtration using a reverse osmosis membrane device,
By mixing the biologically treated water obtained by biologically treating organic wastewater and the seawater, low-concentration saltwater having a salt concentration of 0.2 M or less is generated, and the low-concentration saltwater is supplied to the reverse osmosis membrane device. Supplying and filtering,
By mixing the biologically treated water and the seawater, or by using only the seawater, high-concentration saltwater having a salt concentration exceeding 0.2M is generated, and the high-concentration saltwater is supplied to the reverse osmosis membrane device. A seawater desalination method comprising a step of supplying and filtering. 前記高濃度塩水を前記逆浸透膜装置に供給してろ過処理する工程を一時的に実施する、請求項１に記載の海水淡水化方法。 The seawater desalination method according to claim 1 , wherein the step of supplying the high-concentration salt water to the reverse osmosis membrane device and performing a filtration treatment is temporarily performed. 逆浸透膜装置を用いたろ過処理によって海水を淡水化するための海水淡水化装置であって、
有機性廃水を生物処理して得られる生物処理水と前記海水とを混合することにより、０．２Ｍ以下の塩濃度を有する低濃度塩水を生成することと、前記生物処理水と前記海水とを混合することにより、または前記海水のみを用いることにより、０．２Ｍを超える塩濃度を有する高濃度塩水を生成することとが可能なように構成されている混合部と、
前記混合部で得られる前記低濃度塩水及び前記高濃度塩水をろ過処理する前記逆浸透膜装置とを備え、
前記混合部は、前記生物処理水が導入される生物処理水導入部と、前記海水が導入される海水導入部と、前記低濃度塩水または前記高濃度塩水を前記逆浸透膜装置へ排出する排出部とを含み、前記生物処理水導入部及び前記海水導入部は、前記混合部に導入される量を調整することが可能なように、開口度を調整できるように構成されている、海水淡水化装置。 A seawater desalination device for desalinating seawater by filtration using a reverse osmosis membrane device,
The biologically treated water obtained by biologically treating organic wastewater and the seawater are mixed to produce low-concentration saltwater having a salt concentration of 0.2 M or less, and the biologically treated water and the seawater. A mixing section configured to be capable of producing high-concentration salt water having a salt concentration exceeding 0.2M by mixing or by using only the seawater;
The reverse osmosis membrane device for filtering the low-concentration salt water and the high-concentration salt water obtained in the mixing unit ,
The mixing unit includes a biologically treated water introduction unit into which the biologically treated water is introduced, a seawater introduction unit into which the seawater is introduced, and a discharge that discharges the low-concentration salt water or the high-concentration salt water to the reverse osmosis membrane device. Seawater freshwater , wherein the biologically treated water introduction unit and the seawater introduction unit are configured to adjust the degree of opening so that the amount introduced into the mixing unit can be adjusted. Device.
JP2011197406A 2011-09-09 2011-09-09 Seawater desalination method and seawater desalination apparatus Expired - Fee Related JP5526093B2 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2011197406A JP5526093B2 (en) 2011-09-09 2011-09-09 Seawater desalination method and seawater desalination apparatus
PCT/JP2012/064517 WO2013035397A1 (en) 2011-09-09 2012-06-06 Seawater desalination method and seawater desalination device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2011197406A JP5526093B2 (en) 2011-09-09 2011-09-09 Seawater desalination method and seawater desalination apparatus

Publications (2)

Publication Number Publication Date
JP2013056320A JP2013056320A (en) 2013-03-28
JP5526093B2 true JP5526093B2 (en) 2014-06-18

Family

ID=47831857

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2011197406A Expired - Fee Related JP5526093B2 (en) 2011-09-09 2011-09-09 Seawater desalination method and seawater desalination apparatus

Country Status (2)

Country Link
JP (1) JP5526093B2 (en)
WO (1) WO2013035397A1 (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP6201998B2 (en) * 2013-05-27 2017-09-27 東レ株式会社 Operation method of water treatment equipment
JP5565536B1 (en) * 2014-03-31 2014-08-06 株式会社フクハラ Brackish water desalination treatment equipment
WO2017168720A1 (en) * 2016-03-31 2017-10-05 三菱重工業株式会社 Reverse osmosis membrane processing method and reverse osmosis membrane processing equipment
CN114506950A (en) * 2020-11-16 2022-05-17 中国石油化工股份有限公司 Zero-discharge method for sewage of refining enterprises

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS62234509A (en) * 1986-04-03 1987-10-14 Sasakura Eng Co Ltd Sterilizing method for reverse osmotic pressure device
JP2004121896A (en) * 2002-09-30 2004-04-22 Toray Ind Inc Method of producing treated water and salt water treatment equipment
JP4481345B1 (en) * 2008-11-28 2010-06-16 株式会社神鋼環境ソリューション Seawater desalination method and seawater desalination apparatus
SG178304A1 (en) * 2009-08-21 2012-03-29 Toray Industries Fresh water production method
JP2011104504A (en) * 2009-11-17 2011-06-02 Toray Ind Inc Washing method of water treatment facility
CN102596822B (en) * 2009-12-25 2014-05-21 东丽株式会社 Water production system and operation method therefor

Also Published As

Publication number Publication date
JP2013056320A (en) 2013-03-28
WO2013035397A1 (en) 2013-03-14

Similar Documents

Publication Publication Date Title
JP4481345B1 (en) Seawater desalination method and seawater desalination apparatus
WO2010061879A1 (en) Fresh water production method, fresh water production apparatus, method for desalinating sea water into fresh water, and apparatus for desalinating sea water into fresh water
NL2018508B1 (en) Method for purifying water as well as a suitable device.
WO2011155281A1 (en) Freshwater-generating device, and freshwater-generating method
JP5526093B2 (en) Seawater desalination method and seawater desalination apparatus
JP2010188344A (en) Method and apparatus of desalinating seawater
JP4499835B1 (en) Fresh water generating apparatus and fresh water generating method
JP4933679B1 (en) Seawater desalination method and seawater desalination apparatus
JP2017012985A (en) Water treatment system and method
JP5250684B2 (en) Seawater desalination method and seawater desalination apparatus
JP5999087B2 (en) Water treatment apparatus and water treatment method
JP4499834B1 (en) Fresh water generating apparatus and fresh water generating method
JP2011056411A (en) System and method for desalination of water to be treated
WO2012057176A1 (en) Water-treatment method and desalinization method
WO2011155282A1 (en) Fresh water-generating device and fresh water-generating method
JP4518435B1 (en) Seawater desalination method and seawater desalination apparatus
JP5232906B2 (en) Purified water generating method and purified water generating apparatus
JP5119280B2 (en) Seawater desalination method and seawater desalination apparatus
JP2024009663A (en) Wastewater treatment method and wastewater treatment equipment
Bui et al. PERFORMANCE OF AIRLIFT MEMBRANE BIOREACTOR TREATING WASTEWATER FROM INDUSTRIAL PARK IN HO CHI MINH CITY

Legal Events

Date Code Title Description
A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20130531

TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20140404

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20140414

R150 Certificate of patent or registration of utility model

Ref document number: 5526093

Country of ref document: JP

Free format text: JAPANESE INTERMEDIATE CODE: R150

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

LAPS Cancellation because of no payment of annual fees