WO2019087867A1

WO2019087867A1 - Seawater desalination method and seawater desalination system

Info

Publication number: WO2019087867A1
Application number: PCT/JP2018/039342
Authority: WO
Inventors: 崇人中尾; 周美韓; 櫻井　秀彦
Original assignee: 東洋紡株式会社
Priority date: 2017-10-30
Filing date: 2018-10-23
Publication date: 2019-05-09
Also published as: JP7102706B2; JP2019081134A

Abstract

Provided is a seawater desalination method in which the amount of energy consumed in a reverse osmosis step is reduced. This seawater desalination method for obtaining fresh water from seawater includes: a forward osmosis step for contacting seawater supplied from a seawater tank and water having a low osmotic pressure with one another across a semi-permeable membrane, and obtaining a diluted salt water which is diluted seawater; and a reverse osmosis step for using a reverse osmosis membrane and obtaining, from the diluted salt water obtained in the forward osmosis step, concentrated salt water which is a concentrate of the diluted salt water, and produced water which has passed through the reverse osmosis membrane.

Description

Seawater desalination method and sea water desalination system

The present invention relates to a seawater desalination method and a seawater desalination system.

Forward osmosis (FO) means a solution (draw solution) with high concentration (high osmotic pressure) of water at the low concentration (low osmotic pressure) side of the treated water (feed solution) via the forward osmosis membrane It is a phenomenon that moves toward. On the other hand, in the field of water treatment, a water treatment method using a reverse osmosis (RO) process is conventionally known. The reverse osmosis step is a step of moving water from the high concentration treated water to the low concentration solution side contrary to the forward osmosis by artificially applying a strong pressure.

In a freshwater production system (seawater desalination system) that produces fresh water from seawater, seawater pressurized to a predetermined pressure by a boost pump is supplied to an RO membrane module, and the RO membrane is permeated to allow salt and the like in seawater to be extracted. A reverse osmosis step is performed to remove and take out fresh water (produced water). At this time, the remaining salt water which has not permeated through the RO membrane is discharged from the RO membrane module as concentrated salt water (brine) (Patent Document 1: Japanese Patent Application Laid-Open No. 2004-97911).

Japanese Patent Laid-Open No. 2004-97911

However, the salt concentration of seawater is about 3.5 w / v%, and the osmotic pressure is very high at 2.5 to 3 MPa. For this reason, the reverse osmosis step in the seawater desalination apparatus requires a pressure (preferably 6 to 8 MPa) that is higher than the osmotic pressure of seawater, and the energy consumption is extremely large, so the energy efficiency is low.

Then, an object of this invention is to provide the seawater desalination method which can reduce the energy consumption of a reverse osmosis process.

[1] A seawater desalination method for obtaining fresh water from seawater,
A forward osmosis process, wherein seawater supplied from a seawater tank is brought into contact with hypotonic water through a semipermeable membrane to obtain diluted seawater in which the seawater is diluted;
A reverse osmosis step of obtaining, from the diluted brine obtained in the forward osmosis step, product water having permeated through the reverse osmosis membrane and a concentrated brine which is the concentrated dilute brine using a reverse osmosis membrane;
Seawater desalination methods, including:

[2] The seawater desalination method according to [1], wherein the low osmotic pressure water is drainage.

[3] The seawater desalination method according to [1] or [2], wherein the concentrated brine obtained in the reverse osmosis step is returned to the seawater tank and reused in the forward osmosis step.

[4] The seawater desalination method according to any one of [1] to [3], wherein the seawater is pretreated seawater.

[5] The seawater desalination method according to any one of [1] to [4], wherein the salt concentration of the concentrated brine is 2 w / v% or more.

[6] A seawater desalination system for use in the seawater desalination method according to any one of [1] to [5], wherein
A forward osmosis treatment device having a semipermeable membrane, bringing seawater supplied from a seawater tank into contact with low osmotic pressure water via the semipermeable membrane, and discharging diluted salt water diluted with the seawater;
Reverse osmosis treatment, which comprises a reverse osmosis membrane and discharges, from the diluted brine discharged from the forward osmosis treatment device, the product water having permeated through the reverse osmosis membrane and the concentrated brine which is the concentrated dilute brine; A device,
Desalination system, equipped with

ADVANTAGE OF THE INVENTION According to this invention, the energy consumption of a reverse osmosis process in a seawater desalination method can be reduced.

It is a schematic diagram which shows the structure of the seawater desalination method (seawater desalination system) which concerns on embodiment.

Hereinafter, a seawater desalination method and a seawater desalination system according to an embodiment of the present invention will be described with reference to FIG. In the drawings, the same reference numerals indicate the same or corresponding parts.

(Forward penetration process)
In this step, referring to FIG. 1, seawater supplied from seawater tank 6 is brought into contact with low osmotic pressure water through semipermeable membrane 1a to obtain diluted brine in which seawater is diluted.

The forward osmosis treatment apparatus used in the forward osmosis step of the present invention has the semipermeable membrane 1a, and the seawater supplied from the seawater tank 6 is brought into contact with the low osmotic pressure water through the forward osmosis membrane 1a to Drain the diluted salted water.

Specifically, the forward osmosis treatment apparatus comprises a forward osmosis (FO) membrane module 1. The FO membrane module 1 includes an FO membrane 1a which is a semipermeable membrane used for forward osmosis treatment, a first chamber 11 to which a feed solution (FS) is supplied, and a second to which a draw solution (DS) is supplied. A chamber 12 is provided, and the first chamber 11 and the second chamber 12 are separated by the FO membrane 1a. In addition, the forward osmosis treatment apparatus includes a pump 31 for supplying FS to the first chamber 11 of the FO membrane module 1, and a pump 32 for supplying DS to the second chamber 12 of the FO membrane module 1 from the seawater tank 6. Prepare.

In the present embodiment, DS is seawater. FS is not particularly limited as long as it is a liquid (hypotonic water) having an osmotic pressure lower than DS, but, for example, fresh water (for example, river water, drainage (industrial drainage, treated sewage etc.)), and seawater Low salt water (eg, brine, brackish water) is used. The low osmotic pressure water is preferably waste water. When waste water is used as the low osmotic pressure water, the amount of waste water discarded as industrial waste can be reduced.

In the forward osmosis step, low osmotic pressure water is supplied to the first chamber 11 of the FO membrane module 1 via the pump 31, and the low osmotic pressure water is brought into contact with one surface of the semipermeable membrane 1a. The seawater pumped from the seawater tank 6 is supplied to the second chamber 12 of the FO membrane module 1 and brought into contact with the opposite surface of the semipermeable membrane 1a.

Since an osmotic pressure difference occurs between seawater and hypotonic water in contact through the semipermeable membrane, the water contained in the low osmotic pressure water permeates the semipermeable membrane 1a by the forward osmosis phenomenon, and the seawater Move to The diluted seawater (salt water) having a reduced salt concentration is discharged from the FO membrane module 1 and supplied to the RO membrane module 2 via the pressure rising pump 33.

(Reverse osmosis process)
In this step, referring to FIG. 1, from the diluted brine obtained in the forward osmosis step, using reverse osmosis membrane 2a, the product water permeated through reverse osmosis membrane 2a and concentrated brine which is concentrated diluted brine Get

The reverse osmosis treatment apparatus used in the reverse osmosis process of the present invention has a reverse osmosis membrane 2a, and from the diluted brine discharged from the forward osmosis treatment apparatus, the produced water permeating the reverse osmosis membrane and the concentrated diluted brine Drain the concentrated brine.

Specifically, the reverse osmosis treatment apparatus comprises a reverse osmosis (RO) membrane module 2a, a reverse osmosis (RO) membrane module 2, and a pressure rising pump for supplying seawater diluted in the RO membrane module 2 (diluted salt water) 33 is provided.

In the present invention, the shapes of the FO membrane 1a and the RO membrane 2a are not particularly limited, and examples thereof include flat membranes, spiral membranes, and hollow fiber membranes. In addition, in FIG. 1, although flat membrane is simplified and drawn as FO membrane and RO membrane, it is not limited in particular in such a shape. A hollow fiber membrane (hollow fiber type semipermeable membrane) can increase the membrane area per module compared to a spiral type semipermeable membrane etc., and can improve the efficiency of reverse osmosis and forward osmosis. Is advantageous.

The material of the FO membrane and the RO membrane is not particularly limited, and examples thereof include cellulose acetate, polyamide and sulfonated polysulfone. The materials of the FO film 1a and the RO film 2a may be the same or different. Since cellulose acetate is excellent in chlorine resistance, when cellulose acetate is used, a chlorine-based bactericide can be added to the water supplied to each module as a bactericide.

The form of the FO membrane module 1 and the RO membrane module 2 is not particularly limited, but in the case of using a hollow fiber membrane, a module in which the hollow fiber membrane is arranged straight or a cross in which the hollow fiber membrane is wound around a core tube Wind-type module etc. are mentioned. When a flat membrane is used, a stacked module in which flat membranes are stacked, or a spiral type module in which a flat membrane is enveloped and wound around a core tube may, for example, be mentioned.

In the reverse osmosis step, the diluted brine discharged from the FO membrane module 1 is pressurized by the pressure pump 33 to a pressure higher than the osmotic pressure possessed by the diluted brine, and is supplied to the RO membrane module 2. The diluted brine supplied to the RO membrane module 2 can pass through the RO membrane 2a to obtain fresh water from which the salt content, impurities and the like have been removed from the diluted seawater. The remaining diluted brine that has not permeated the RO membrane 2a is concentrated and discharged from the RO membrane module 2 as concentrated brine. The obtained fresh water is sent to the next purification step or the like as necessary to be produced water.

Diluted saltwater has lower salt concentration and lower osmotic pressure compared to seawater. Therefore, in the reverse osmosis step, the amount of energy consumed by the pressure rising pump 33 can be suppressed. The salt concentration of the diluted brine is not particularly limited, and is, for example, 0.5 w / v% to 2.0 w / v%. As a method (means) for adjusting the concentration of the diluted brine to the above range, the diluted brine discharged from the second chamber 12 of the FO membrane module 1 is diluted in the flow path (route) until it is supplied to the RO membrane module 2 A method of installing a measuring device for measuring the concentration, osmotic pressure or flow rate of salt water, and controlling the output (pressure) of the

pumps

31, 32 based on the value measured by the measuring device, and as necessary, an FO membrane A method of adjusting the opening degree of a flow rate adjusting valve (not shown) installed in a flow path (path) until the diluted brine discharged from the second chamber 12 of the module 1 is supplied to the RO membrane module 2, etc. It can be mentioned. Note that, for example, by reducing the output of the pump 32, the salt concentration of the diluted brine can be reduced. Also, for example, by increasing the output of the pump 31, the salt concentration of the diluted brine can be reduced.

The present invention is particularly useful when applied to an existing seawater desalination system using reverse osmosis treatment (apparatus).

In the present invention, it is preferable to return the concentrated brine concentrated in the reverse osmosis step back to the seawater tank 6 for reuse in the forward osmosis step.

Specifically, in FIG. 1, the concentrated salt water discharged from the RO membrane module 2 is supplied to the seawater tank 6 through the circulation path 4. The concentrated salt water supplied to the seawater tank 6 is supplied to the second chamber 12 of the FO membrane module 1 via the pump 32 and used again as DS.

The seawater is preferably seawater pretreated by the seawater pretreatment device 5. When pretreatment of seawater is not performed, suspended turbidity, soluble organic matter, microorganisms adhering to the surface of the membrane, and the like are generated to cause membrane contamination. The pretreatment method of seawater includes sand filtration, flocculation filtration, pressure flotation separation, UF membrane (Ultrafiltration), MF membrane (Microfiltration: microfiltration), cartridge filter etc. There is a method of processing, which can remove pollution sources and obtain seawater of water quality compatible with the FO membrane module 1.

These pretreatments require large-scale equipment. Moreover, in order to perform sufficient treatment according to the water quality condition of the taken-in seawater, detailed operation management by a skilled engineer is also necessary. When concentrated salt water is circulated and reused, the amount of pretreatment of seawater can be reduced, and the pretreatment equipment can be miniaturized. Conventionally, when, for example, pretreatment of 30,000 tons / day of seawater is necessary, the amount of the treatment can be reduced to, for example, 500 tons / day by circulating concentrated salt water.

In addition, when starting the operation of the seawater desalination system, the seawater required to simultaneously bring up all the trains (the smallest unit that can be switched on / off independently including multiple RO membrane modules) is pretreated at one time do not have to. The seawater pretreatment device 5 may be used to start up one train at a time, and in this case, the pretreatment device can be further miniaturized. Pretreatment can be partially omitted by using an aqueous NaCl solution which does not require pretreatment in place of seawater.

When the concentrated brine is recycled for reuse, the salt concentration of the concentrated brine is preferably 2 w / v% or more, more preferably 2 w / v% or more and 7 w / v% or less, still more preferably 3 w It is not less than / v% and not more than 4w / v%. When the salt concentration is in this range, in the forward osmosis treatment step after being returned to the seawater tank 6, the osmotic pressure difference with the low osmotic pressure water is sufficient, so that the forward osmosis phenomenon easily occurs. In addition, when the salt concentration is higher than this range, the osmotic pressure is increased, and energy consumption in the pressure rising pump 33 is increased, which is not preferable.

As a method (means) to adjust the salt concentration of the concentrated brine to the above range, measure the concentration (osmotic pressure) of the concentrated brine in the path (flow path) where the concentrated brine is discharged from the RO membrane module 2 or the circulation route 4 Method for installing a measuring device to adjust the output of the pressure pump 33 based on the value measured by the measuring device, or a flow path or circulation path where concentrated salt water is discharged from the RO membrane module 2 as needed The method of adjusting the opening degree of the flow control valve (not shown) installed in 4 etc. is mentioned. In addition, the salt concentration of concentrated salt water can be raised by raising the output of the pressure rising pump 33, for example.

In addition, a measuring device for measuring the concentration, osmotic pressure or flow rate of diluted brine in the flow path (pathway) where the diluted brine discharged from the second chamber 12 of the FO membrane module 1 is supplied to the RO membrane module 2 Install and integrate the outputs (pressures) of the

pumps

31, 32 and boost pump 33 (also the opening of the flow rate adjustment valve provided in each flow path if necessary) based on the value measured by the measuring device. It is also possible to use control methods.

However, since the salt slightly passes through the FO membrane 1a and the RO membrane 2a, the salinity in the circulating seawater gradually decreases. At this time, seawater may be newly collected from the ocean, pretreated by the seawater pretreatment apparatus 5, and then replenished to the seawater tank 6.

In addition, additives such as a scale inhibitor, a chlorine-based bactericidal agent, and a pH adjuster can be added to the seawater if necessary.

The anti-scaling agent is not particularly limited, but for example, inorganic polyphosphates such as sodium hexametaphosphate, sodium tripolyphosphate, phosphonic acids such as aminomethyl phosphonic acid and phosphonobutane tricarboxylic acid for preventing calcium-based scale A scale inhibitor containing phosphorus, a copolymer of maleic acid and isobutylene, a terpolymer of maleic acid and vinyl ethyl acetate and ethyl acrylate, an AA (acrylic acid) -AMPS (2-acrylamido-2-methylpropyl sulfonic acid) copolymer and a PMA The scale inhibiting agent etc. which do not contain phosphorus, such as a combined agent with polymaleic acid, etc. are mentioned. The addition of these scale inhibitors can suppress scale failure of the membrane.

The chlorine-based germicide is not particularly limited, and examples thereof include chlorine gas, free chlorine such as sodium hypochlorite and calcium hypochlorite, combined chlorine such as monochloramine, and chlorine dioxide. The addition of these chlorine-based germicides can suppress the growth of microorganisms that cause biofouling, and make it difficult to cause deterioration in membrane performance.

Since these additives do not easily permeate through the FO membrane or RO membrane, there is no need to re-add additives when circulating the concentrated salt water discharged from the RO membrane module 2 for recycling, or fresh seawater The amount of additive added can be reduced compared to the case of treatment.

It should be understood that the embodiments disclosed herein are illustrative and non-restrictive in every respect. The scope of the present invention is shown not by the above description but by the scope of claims, and is intended to include all modifications within the scope and meaning equivalent to the scope of claims.

1 Forward Osmosis Membrane Module (FO Membrane Module), 1a Semipermeable Membrane (FO Membrane), 11 First Chamber, 12 Second Chamber, 2 Reverse Osmosis Membrane Module (RO Membrane Module), 2a Reverse Osmosis Membrane (RO Membrane), 31, 32 pumps, 33 boost pumps, 4 circulation paths, 5 seawater pretreatment equipment, 6 seawater tanks.

Claims

A seawater desalination method for obtaining fresh water from seawater,
A forward osmosis process, wherein seawater supplied from a seawater tank is brought into contact with hypotonic water through a semipermeable membrane to obtain diluted seawater in which the seawater is diluted;
A reverse osmosis step of obtaining, from the diluted brine obtained in the forward osmosis step, product water having permeated through the reverse osmosis membrane and a concentrated brine which is the concentrated dilute brine using a reverse osmosis membrane;
Seawater desalination methods, including:
The seawater desalination method according to claim 1, wherein the low osmotic pressure water is drainage.
The seawater desalination method according to claim 1 or 2, wherein the concentrated brine obtained in the reverse osmosis step is returned to the seawater tank and reused in the forward osmosis step.
The seawater desalination method according to any one of claims 1 to 3, wherein the seawater is pretreated seawater.
The seawater desalination method according to any one of claims 1 to 4, wherein the salt concentration of the concentrated brine is 2 w / v% or more.
A seawater desalination system for use in the seawater desalination method according to any one of claims 1 to 5, comprising:
A forward osmosis treatment device having a semipermeable membrane, bringing seawater supplied from a seawater tank into contact with low osmotic pressure water via the semipermeable membrane, and discharging diluted salt water diluted with the seawater;
Reverse osmosis treatment, which comprises a reverse osmosis membrane and discharges, from the diluted brine discharged from the forward osmosis treatment device, the product water having permeated through the reverse osmosis membrane and the concentrated brine which is the concentrated dilute brine; A device,
Desalination system, equipped with