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WO2020158456A1 - Système de concentration et procédé de concentration - Google Patents

Système de concentration et procédé de concentration Download PDF

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Publication number
WO2020158456A1
WO2020158456A1 PCT/JP2020/001504 JP2020001504W WO2020158456A1 WO 2020158456 A1 WO2020158456 A1 WO 2020158456A1 JP 2020001504 W JP2020001504 W JP 2020001504W WO 2020158456 A1 WO2020158456 A1 WO 2020158456A1
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Prior art keywords
chamber
target solution
target
component
concentration
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Ceased
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PCT/JP2020/001504
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English (en)
Japanese (ja)
Inventor
要二 阿部
大樹 河野
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Toyobo Co Ltd
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Toyobo Co Ltd
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Priority to JP2020534998A priority Critical patent/JPWO2020158456A1/ja
Publication of WO2020158456A1 publication Critical patent/WO2020158456A1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/02—Crystallisation from solutions
    • 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

Definitions

  • the present invention relates to a concentration system and a concentration method.
  • the components in the target solution can be concentrated.
  • a part of the target solution is caused to flow into one of the first chambers of the semipermeable membrane module, and the other is By flowing another part of the target solution into the second chamber and pressurizing the target solution in the first chamber, the water contained in the target solution in the first chamber is transferred to the second chamber through the semipermeable membrane.
  • a membrane separation method in which the target solution in the first chamber is concentrated and the target solution in the second chamber is diluted (hereinafter, may be abbreviated as “BC”) is under study.
  • the other side of the semipermeable membrane basically has an osmotic pressure. Since there is only water, there is a large difference in osmotic pressure between the two sides of the semipermeable membrane, and it is necessary to pressurize the target solution with a high pressure that overcomes the pressure generated thereby. Since the pressurization pressure is limited by the operating pressure (limit pressure) of the semipermeable membrane and the maximum pressure of the pump used, in RO, the osmotic pressure of the target solution is the operating pressure of the semipermeable membrane or the maximum pressure of the pump. The target solution cannot be concentrated to such a high concentration that it exceeds the pressure.
  • BC by flowing the target solution also on the other side (low pressure side) of the semipermeable membrane, the osmotic pressure difference between both sides of the semipermeable membrane is reduced, and the target solution on the high pressure side is pressurized.
  • the pressure can be reduced. Therefore, by using BC, the target solution can be concentrated to a high concentration such that the osmotic pressure of the target solution exceeds the operating pressure of the semipermeable membrane, the maximum pressure of the pump, or the like.
  • the target solution cannot be concentrated to a saturation concentration or more, but the target solution can be concentrated to a maximum saturation concentration.
  • Patent Document 2 Japanese Patent Laid-Open No. 2013-43860 discloses a method of crystallizing and removing calcium lactate by cooling a solution containing calcium lactate concentrated by reverse osmosis.
  • the plurality of dissolved components are basically concentrated at the same concentration rate, so that a desired component (target component) of the plurality of components is replaced with another component. It is not possible to perform selective concentration such as concentration at a higher concentration rate.
  • the target solution in which multiple components are dissolved is concentrated with BC, if the components other than the target component reach the saturation concentration first, the concentration of the target component cannot proceed any further.
  • the target solution contains a component that reaches the saturation concentration before the target component, there is also a problem that the target component cannot be concentrated to a high concentration near the saturation concentration.
  • the present invention for the target solution in which a plurality of components are dissolved in water, can be concentrated to a high concentration such that the osmotic pressure of the target solution exceeds the operating pressure of the semipermeable membrane, the maximum pressure of the pump, etc., and
  • An object of the present invention is to provide a concentration system and a concentration method capable of concentrating at least one component (target component) contained in a target solution at a higher concentration rate than other components.
  • a cooling apparatus which cools the target solution to a specified temperature to precipitate the other components
  • a semipermeable membrane and a semipermeable membrane module having a first chamber and a second chamber partitioned by the semipermeable membrane, wherein the target solution is flown into each of the first chamber and the second chamber, and By pressurizing the target solution in the first chamber so as to be higher than the pressure of the target solution in the second chamber, the water contained in the target solution in the first chamber is transferred to the semipermeable membrane.
  • a membrane separation device that moves the solution into the second chamber through the second chamber, concentrates the target solution in the first chamber, and dilutes the target solution in the second chamber,
  • the specified temperature is set such that at that temperature, the other component precipitates and the target component does not precipitate, or the amount of the target component deposited is less than the amount of the other component deposited. , Concentration system.
  • a method for concentrating a target solution in which at least one target component and at least one other component are dissolved in water, wherein the target component is concentrated at a higher concentration rate than the other component A semipermeable membrane, and a semipermeable membrane module having a first chamber and a second chamber partitioned by the semipermeable membrane, the target solution is flown into each of the first chamber and the second chamber, and , The water contained in the target solution in the first chamber is pressurized by pressurizing the target solution in the first chamber to be higher than the pressure of the target solution in the second chamber.
  • a membrane separation step in which the target solution in the first chamber is diluted and the target solution in the second chamber is diluted while being transferred to the second chamber via Cooling the target solution to a specified temperature to precipitate the other component, a precipitation step,
  • the specified temperature is set such that at that temperature, the other component precipitates and the target component does not precipitate, or the amount of the target component deposited is less than the amount of the other component deposited.
  • the osmotic pressure of the target solution can be concentrated to a high concentration such that the operating pressure of the semipermeable membrane or the maximum pressure of the pump is exceeded, and It is possible to provide a concentration system and a concentration method capable of concentrating at least one component (target component) contained in a target solution at a higher concentration rate than other components.
  • the concentration system of the present embodiment is a concentration system that concentrates a target component at a higher concentration ratio than other components in a target solution in which at least one target component and at least one other component are dissolved in water. is there.
  • the concentration system includes a precipitation device and a membrane separation device.
  • the target components are selectively concentrated in the liquid phase by the precipitation device (precipitation process). Further, the target solution is concentrated to a high concentration by a membrane separation device (membrane separation step: BC).
  • Either the concentration by the membrane separator (membrane separation step: BC) or the concentration by the precipitation device 2 (precipitation step) may be performed first.
  • the concentration by the precipitation apparatus 2 may be followed by the concentration by the membrane separation apparatus.
  • the concentration by the precipitation apparatus 2 is performed. May be.
  • the target solution may be concentrated until the target component reaches a desired concentration by repeating the concentration using these membrane separators (semi-permeable membrane modules) and the precipitation device.
  • concentration by the membrane separation device and the concentration by the precipitation device are repeated, for example, both may be alternately repeated, or one may be continuously repeated and the other may be continuously repeated.
  • Target solution It is a solution in which at least one target component and at least one other component are dissolved in water.
  • the target component is preferably an inorganic salt, more preferably a metal salt.
  • Specific target components are not particularly limited, for example, zinc chloride, ammonium chloride, yttrium chloride, indium chloride, uranyl chloride, cadmium chloride, gold chloride, cobalt chloride, samarium chloride, mercury chloride, tin chloride, strontium chloride. , Cesium chloride, cerium chloride, iron chloride, nickel chloride, neodymium chloride, barium chloride, praseodymium chloride, beryllium chloride, manganese chloride, radium chloride, rubidium chloride, sodium chloride, magnesium chloride, aluminum chloride, lithium chloride, calcium chloride, etc.
  • Chloride sodium sulfate, magnesium sulfate, lithium sulfate, zinc sulfate, aluminum sulfate, ytterbium sulfate, ammonium aluminum sulfate, ammonium sulfate, uranyl sulfate, uranium sulfate, cadmium sulfate, potassium sulfate, calcium sulfate, chromium sulfate, cobalt sulfate, zirconium sulfate And ammonium sulfate, potassium hydrogen sulfate, scandium sulfate, tin sulfate, cesium sulfate, thallium sulfate, iron sulfate, copper sulfate, nickel sulfate, praseodymium sulfate, beryllium sulfate, manganese sulfate, rubidium sulfate
  • the target component is preferably a lithium salt.
  • the lithium salt is preferably lithium sulfate.
  • the target component is a component whose solubility does not decrease with a decrease in temperature within a predetermined range (for example, 0 to 100° C.).
  • a predetermined range for example, 0 to 100° C.
  • the target component does not deposit when other components are deposited by the deposition device 2, and the target component can be efficiently concentrated.
  • examples of such a target component include lithium sulfate.
  • target components other than inorganic salts include aldehydes such as formaldehyde, acetaldehyde, propionaldehyde and acrolein, ketones such as methyl ethyl ketone, diacetyl, methyl isobutyl ketone and acetone, 1,4-dioxane, 2-methyl-1, Esters such as 3-dioxolane, 1,3-dioxolane, tetrahydrofuran, methyl acetate, ethyl acetate, propyl acetate and butyl acetate, alcohols such as ethanol, n-propyl alcohol, isopropyl alcohol and butanol, ethylene glycol, propylene glycol, Glycols such as diethylene glycol and triethylene glycol, organic acids such as acetic acid and propionic acid, aromatic compounds such as phenols, toluene, xylene and cyclohexane, ethers such as
  • the other components are components that precipitate before the target component by cooling the target solution. Further, the other components preferably have a lower solubility than the target component.
  • the other component is preferably an inorganic salt other than the target component, and more preferably a metal salt other than the target component.
  • the metal salt is preferably a potassium salt or a sodium salt, more preferably potassium sulfate or sodium sulfate.
  • FIG. 1 is a schematic diagram showing the concentration system of the first embodiment.
  • the concentration system of the present embodiment includes at least a deposition device 2 and a membrane separation device (including the semipermeable membrane module 1). Further, the returning means 3 may be provided.
  • the target solution cooled to the specified temperature in the deposition device 2 is the target solution concentrated in the membrane separation device (semipermeable membrane module 1).
  • the target solution is first concentrated in the liquid phase by the precipitation device 2 (precipitation step) and then further concentrated by the membrane separation device (membrane separation step: BC).
  • the deposition apparatus 2 cools the target solution to a specified temperature and deposits other components.
  • the specified temperature is set such that at that temperature, other components are deposited and the target component is not deposited, or the amount of the target component deposited is smaller than the amount of the other components deposited.
  • the concentration of other components in the target liquid decreases, so that the target component can be concentrated at a higher concentration rate than other components. That is, the target component can be selectively concentrated in the target solution. Note that other components and the like that have precipitated are removed as necessary.
  • the membrane separation device includes a semipermeable membrane 10 and a semipermeable membrane module 1 having a first chamber 11 and a second chamber 12 partitioned by the semipermeable membrane 10.
  • a concentrated solution which is the target solution concentrated by the precipitation device 2
  • the pressure of the target solution in the first chamber 11 is set to the second chamber 12.
  • the water contained in the target solution inside the first chamber 11 is transferred into the second chamber 12 through the semipermeable membrane 10, and the first chamber 11
  • the target solution in the second chamber 12 can be diluted while the target solution in the second chamber 12 is concentrated.
  • the target solution can be concentrated to such a high concentration that the osmotic pressure of the target solution exceeds the operating pressure of the semipermeable membrane or the maximum pressure of the pump.
  • the precipitation concentrate (the supernatant liquid excluding the precipitate obtained in the precipitation device 2) is a saturated solution of the precipitated components (other components).
  • the deposition concentrate is concentrated in the membrane separator (semipermeable membrane) at the same temperature (without heating), the components in the saturated state are deposited and the semipermeable membrane is clogged, and the membrane separator The concentration cannot be continued due to. Therefore, in this embodiment, the deposition concentrate is heated and then supplied to the membrane separation device (the first chamber 11 and the second chamber 12 of the semipermeable membrane module 1). As a result, the solubility of the saturated component (other component) in the precipitation concentrate increases, so that the precipitation of the component can be prevented when the concentration is performed by the membrane separator.
  • the semipermeable membrane 10 may be, for example, a reverse osmosis membrane (RO membrane: Reverse Osmosis Membrane), a forward osmosis membrane (FO membrane: Forward Osmosis Membrane), or a nanofiltration membrane (NF membrane: Nanofiltration Membrane).
  • RO membrane Reverse Osmosis Membrane
  • FO membrane Forward Osmosis Membrane
  • NF membrane Nanofiltration Membrane
  • the semipermeable membrane is preferably a reverse osmosis membrane or a forward osmosis membrane, a nanofiltration membrane.
  • the pressure of the target solution in the first chamber 11 is preferably 0.5 to 10.0 MPa.
  • the pore size of RO membrane and FO membrane is about 2 nm or less, and the pore diameter of UF membrane is about 2 to 100 nm.
  • the NF membrane is a RO membrane having a relatively low rejection of ions and salts, and the pore diameter of the NF membrane is usually about 1 to 2 nm.
  • the RO film, the FO film, or the NF film preferably has a salt removal rate of 90% or more.
  • the material forming the semipermeable membrane is not particularly limited, but examples thereof include cellulose resin, polysulfone resin, and polyamide resin.
  • the semipermeable membrane is preferably composed of a material containing at least one of a cellulose resin and a polysulfone resin.
  • the cellulose resin is preferably a cellulose acetate resin.
  • Cellulose acetate-based resin is resistant to chlorine, which is a bactericide, and is characterized by being able to suppress the growth of microorganisms.
  • the cellulose acetate resin is preferably cellulose acetate, and more preferably cellulose triacetate from the viewpoint of durability.
  • the polysulfone resin is preferably a polyether sulfone resin.
  • the polyether sulfone resin is preferably sulfonated polyether sulfone.
  • the shape of the semipermeable membrane 10 is not particularly limited, but examples thereof include a flat membrane, a spiral membrane or a hollow fiber membrane.
  • a flat membrane is illustrated in a simplified manner as the semipermeable membrane 10, but the shape is not limited to such a shape, and a hollow fiber membrane is preferable.
  • Hollow fiber membranes (hollow fiber type semipermeable membranes) have a smaller film thickness than spiral type semipermeable membranes, and in addition, the membrane area per module can be increased and permeation efficiency can be improved. It is advantageous.
  • the semipermeable membrane module preferably includes a plurality of hollow fiber membranes, and each of the plurality of hollow fiber membranes has openings at both ends.
  • the first chamber 11 is preferably outside the hollow fiber membrane and the second chamber 12 is preferably inside the hollow fiber membrane.
  • the solution outside the hollow fiber membranes is preferably pressurized. Even if the solution flowing inside the hollow fiber membrane (hollow part) is pressurized, the pressure loss may increase and it may be difficult to pressurize sufficiently.
  • the structure of the hollow fiber membrane itself is This is because it is easy to hold and the membrane may burst when a high internal pressure is applied.
  • a hollow fiber membrane having a small pressure loss that is, a large inner diameter and a large pressure resistance against the internal pressure is used, there is no problem even if the first chamber 11 is inside the hollow fiber membrane.
  • the membrane separation device may be a single-stage device using one semipermeable membrane module 1 as shown in FIG. 1, but is a multi-stage device using a plurality of semipermeable membrane modules 1. May be.
  • the concentration system of the present embodiment may further include return means (return flow path) 3 for returning the target solution (membrane concentrate) concentrated in the membrane separation apparatus to the deposition apparatus 2.
  • return means return flow path 3 for returning the target solution (membrane concentrate) concentrated in the membrane separation apparatus to the deposition apparatus 2. This makes it possible to concentrate the target solution until the target component reaches a desired concentration by repeating the concentration using the precipitation device 2 and the membrane separation device (semipermeable membrane module 1).
  • the concentration of the membrane concentrated liquid returned to the deposition device 2 by the returning means 3 may be approximately the same as the concentration of other components in the initial target solution (for example, the concentration change rate is within 10% by mass). preferable.
  • the concentration by the precipitation device 2 and the membrane separation device can be repeated while the operating conditions of the precipitation device 2 and the membrane separation device remain constant, so that the control of the concentration system becomes easy.
  • the deposition rate in the precipitation device 2 ( The specified temperature of the deposition device 2 may be set in consideration of the difference between the concentration of the component and the solubility of the other component at the specified temperature) and the concentration rate in the membrane separation device.
  • the temperature of the membrane concentrated liquid returned to the precipitation device 2 by the return means 3 is about the same as the temperature of the initial target solution (for example, the initial target solution
  • the temperature is preferably ⁇ 5° C.).
  • the concentration by the precipitation device 2 and the membrane separation device can be repeated while the operating conditions of the precipitation device 2 and the membrane separation device remain constant, so that the control of the concentration system becomes easy.
  • the above-described heating temperature of the precipitation concentrate is set to the initial value (precipitation device 2). It is preferable to set the temperature to be about the same as the temperature of the target solution (before being cooled in step 1). As a result, the temperature of the membrane concentrate returned to the deposition apparatus 2 can be made approximately the same as the initial temperature of the target solution without heating the membrane concentrate in the returning means 3.
  • FIG. 2 is a schematic diagram showing a concentration system of a modified example of the first embodiment. This modification is different from the first embodiment in that the target solution supplied to the second chamber 12 of the semipermeable membrane module 1 is a part of the target solution concentrated by passing through the first chamber 11. different. The other points are similar to those of the first embodiment.
  • the first embodiment there is no osmotic pressure difference between the liquids on both sides (the first chamber 11 and the second chamber 12) of the semipermeable membrane 10 on the inlet side of the semipermeable membrane module 1, but on the outlet side of the semipermeable membrane module 1. Since the osmotic pressure difference between the liquids on both sides of the semipermeable membrane 10 gradually increases as it goes, it is necessary to apply a pressure that overcomes the osmotic pressure to the target solution in the first chamber 11.
  • the difference in the liquids on both sides of the semipermeable membrane 10 on the outlet side (the outlet side of the first chamber 11) in the semipermeable membrane module 1 is reduced, so that the first chamber 11
  • the pressure applied to the target solution of can be made lower than that of the first embodiment.
  • the operation is performed at the same pressure as that of the first embodiment, it is possible to obtain a membrane concentrated solution having a higher concentration than that of the first embodiment.
  • FIG. 3 is a schematic diagram showing the concentration system of the second embodiment.
  • the target solution cooled to the specified temperature in the precipitation device 2 is the target solution concentrated in the membrane separation device (semipermeable membrane module 1).
  • the target solution is first concentrated in the membrane separator (membrane separation step: BC), and then the target component is selectively concentrated in the liquid phase by the precipitation device 2 (precipitation step).
  • the concentration system of the present embodiment is a return means (return flow path) for returning the target solution (precipitated concentrated solution) concentrated by depositing other components in the deposition apparatus 2 to the semipermeable membrane module 1. 3 may be further provided. This makes it possible to concentrate the target solution until the target component reaches a desired concentration by repeating concentration by the membrane separator (semipermeable membrane module 1) and the precipitation device 2.
  • the concentration of the precipitation concentrated liquid returned to the membrane separation device by the returning means 3 may be approximately the same as the concentration of other components in the initial target solution (for example, the concentration change rate is within 10% by mass). preferable.
  • the concentration by the precipitation device 2 and the membrane separation device can be repeated while the operating conditions of the precipitation device 2 and the membrane separation device remain constant, so that the control of the concentration system becomes easy.
  • the specified temperature of the deposition apparatus 2 described above is determined. Just set it.
  • the temperature of the membrane concentrated liquid returned to the membrane separation device by the returning means 3 is about the same as the temperature of the initial target solution (for example, the initial target solution
  • the temperature is preferably ⁇ 5° C.).
  • the concentration by the membrane separation device and the precipitation device 2 can be repeated while the operating conditions of the membrane separation device and the precipitation device 2 remain constant, so that the control of the concentration system becomes easy.
  • the precipitation concentrate In order to make the temperature of the membrane concentrate returned to the membrane separation device (semipermeable membrane module 1) approximately the same as the initial temperature of the target solution, the precipitation concentrate is in the initial state (before being cooled in the precipitation device 2). (3) The precipitation concentrate may be heated in the returning means so that the temperature of the target solution becomes approximately the same as the temperature of the target solution.
  • FIG. 4 is a schematic diagram showing a concentration system of a modified example of the second embodiment.
  • This modification is different from the second embodiment in that the target solution supplied to the second chamber 12 of the semipermeable membrane module 1 is a part of the target solution concentrated by passing through the first chamber 11. different.
  • the other points are the same as in the second embodiment. Note that the other description of this modification is similar to that of the first embodiment, and will not be repeated.
  • Examples 1 and 2 are examples corresponding to the above Embodiment 1 using the concentration system as shown in FIG.
  • Examples 3 and 4 are examples corresponding to the above-mentioned Embodiment 2 using the concentration system as shown in FIG.
  • the target solution was transferred to the precipitation device 2 (a container kept at a specified temperature of 10° C.) to generate a precipitate.
  • the target solution is an aqueous solution at 40° C. in which 6.6 mass% lithium sulfate and 12 mass% potassium sulfate are dissolved.
  • potassium sulfate precipitates when the temperature becomes 34° C. or lower.
  • the initial concentration of lithium sulfate in the target solution is one third or less of the solubility of lithium sulfate at 40°C, and the solubility of lithium sulfate is rather large when the temperature decreases from 40°C to 10°C.
  • the concentration of potassium sulfate in the target solution (membrane concentrate) after concentration by a membrane separator described later is set to be approximately the same as the concentration of potassium sulfate in the initial target solution (12% by mass).
  • the specified temperature of the deposition apparatus was set to 10°C.
  • the concentration of lithium sulfate was 6.8% by mass and the concentration of potassium sulfate was 8.8% by mass.
  • the target solution (membrane concentrate) that had flowed out from the first chamber of the semipermeable membrane module was collected as the final concentrate.
  • the concentration of lithium sulfate was 9.0% by mass and the concentration of potassium sulfate was 11.5% by mass. Therefore, the concentration rate of the final concentrated solution in Example 1 (the ratio of the concentration of the final concentrated solution to the concentration of the initial target solution) was 1.4 times for lithium sulfate and 1.0 times for potassium sulfate.
  • the target solution in this example is an aqueous solution in which lithium sulfate and sodium sulfate are dissolved, unlike the first example. That is, the target solution is a 30° C. aqueous solution in which 4.5 mass% lithium sulfate and 25 mass% sodium sulfate are dissolved.
  • This target solution was concentrated under the following conditions in the same manner as in Example 1 using a precipitation device (a container kept at a specified temperature of 20° C.) and a membrane separation device (semipermeable membrane module), and the final concentrated liquid was collected. .. [First chamber side (high pressure side)] Pressure: 6.5 MPa, flow rate: 36 g/min [Second chamber side (low pressure side)] Pressure: 0.1 MPa, flow rate: 11.1 g/min
  • the target solution of this example sodium sulfate is precipitated when the temperature becomes 26° C. or lower, but lithium sulfate does not precipitate even when cooled to 20° C. That is, by cooling to 20° C., the sodium sulfate concentration of the final concentrated liquid can be made lower than that of the target solution. Therefore, the specified temperature of the deposition apparatus was set to 20°C.
  • the concentration of lithium sulfate was 5.0% by mass and the concentration of sodium sulfate was 16.8% by mass.
  • the concentration ratio of the final concentrated liquid in Example 2 is 1.4 times for lithium sulfate and 0.84 times for sodium sulfate.
  • the target solution was caused to flow into each of the first chamber 11 and the second chamber 12 of the semipermeable membrane module 1 that constitutes the membrane separation device under the following conditions (see FIG. 1 ).
  • the target solution is an aqueous solution at 40° C. in which 6.6 mass% lithium sulfate and 7.3 mass% potassium sulfate are dissolved.
  • Pressure 0.1 MPa
  • flow rate 14.6 g/min
  • the concentration of lithium sulfate was 9.2 mass% and the concentration of potassium sulfate was 10.1 mass %.
  • the temperature at which potassium sulfate is deposited in the membrane concentrate of this example is 20°C or lower.
  • the membrane concentrate was transferred to the deposition device 2 (a container kept at 10° C.) to generate a deposit.
  • the supernatant liquid (precipitated concentrate) excluding the precipitate was recovered as the final concentrate.
  • the concentration ratio of the final concentrated liquid in Example 3 is 1.4 times for lithium sulfate and 1.2 times for potassium sulfate.
  • the target solution in this example is an aqueous solution in which lithium sulfate and sodium sulfate are dissolved, unlike the first example. That is, the target solution is a 30° C. aqueous solution in which 3.6 mass% lithium sulfate and 20 mass% sodium sulfate are dissolved.
  • This target solution was concentrated under the following conditions in the same manner as in Example 3 using a membrane separation device (semipermeable membrane module) and a precipitation device (container held at 20° C.), and the final concentrated liquid was collected.
  • a membrane separation device semipermeable membrane module
  • a precipitation device container held at 20° C.
  • the concentration of lithium sulfate was 4.5% by mass and the concentration of sodium sulfate was 25% by mass.
  • the temperature at which sodium sulfate is deposited in the membrane concentrate of this example is 26°C or lower.
  • the concentration of lithium sulfate was 5.0% by mass and the concentration of sodium sulfate was 16.8% by mass. Therefore, the concentration ratio of the final concentrated liquid in Example 4 is 1.4 times with lithium sulfate and 0.84 times with sodium sulfate.
  • Comparative Example 1 Comparative Example 1
  • the target solution similar to that of Example 3 was allowed to flow into only the first chamber 11 of the semipermeable membrane module 1 under the same conditions as those of the membrane separation apparatus of Example 3, and the target solution was allowed to flow into the second chamber 12 thereof.
  • Was not supplied ie, reverse osmosis treatment was performed).
  • no permeate was obtained from the second chamber of the semipermeable membrane module, and neither the lithium sulfate nor potassium sulfate was concentrated in the target solution flowing out from the first chamber.
  • the operation pressure of the semipermeable membrane and the pump pressure of the semipermeable membrane can be reduced for the first time by combining the deposition apparatus and the membrane separation apparatus using the brine concentration in which the liquid having the osmotic pressure flows on both sides of the semipermeable membrane. It can be seen that, for a high-concentration solution having an osmotic pressure exceeding the maximum pressure, concentration by membrane separation is possible.
  • 1 semi-permeable membrane module 10 semi-permeable membrane, 11 1st chamber, 12 2nd chamber, 2 deposition device, 3 return means (return flow path).

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Abstract

La présente invention concerne un système de concentration par lequel, dans une solution cible dans laquelle est dissoute une pluralité de composants, un composant cible est augmenté en concentration à un degré supérieur à d'autres composants. Le système de concentration comprend : un dispositif de précipitation qui refroidit la solution cible à une température prescrite pour amener d'autres composants à précipiter ; et un dispositif de séparation à membrane comprenant un module à membrane semi-perméable comportant une membrane semi-perméable et une première chambre et une deuxième chambre qui sont séparées par la membrane semi-perméable, le dispositif de séparation à membrane étant configuré de sorte que la solution cible est amenée à s'écouler dans chacune de la première chambre et la deuxième chambre, et en augmentant la pression de la solution cible dans la première chambre de façon à ce qu'elle soit supérieure à la pression de la solution cible dans la deuxième chambre, l'eau contenue dans la solution cible dans la première chambre est transférée dans la deuxième chambre à travers la membrane semi-perméable, de façon à amener la solution cible dans la première chambre à avoir une concentration accrue, et amener la solution cible dans la deuxième chambre à être diluée.
PCT/JP2020/001504 2019-01-30 2020-01-17 Système de concentration et procédé de concentration Ceased WO2020158456A1 (fr)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112370969A (zh) * 2020-12-08 2021-02-19 郑州大学 一种低能耗膜分离方法及配套装置
JP2022040928A (ja) * 2020-08-31 2022-03-11 オルガノ株式会社 濃縮方法、濃縮装置、水処理方法、および水処理装置
JP2022090763A (ja) * 2020-12-08 2022-06-20 オルガノ株式会社 無機塩回収装置および無機塩回収方法
WO2024117062A1 (fr) * 2022-12-01 2024-06-06 東洋紡エムシー株式会社 Procédé de concentration de solvant et système de concentration de solvant

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0663362A (ja) * 1992-08-24 1994-03-08 Kurita Water Ind Ltd 膜分離装置
JPH10137758A (ja) * 1996-11-14 1998-05-26 Shinko Pantec Co Ltd 水処理方法及び水処理装置
WO2013146391A1 (fr) * 2012-03-30 2013-10-03 東レ株式会社 Procédé de séparation et de récupération d'un métal alcalin et appareil de séparation et de récupération d'un métal alcalin
JP2018001110A (ja) * 2016-07-05 2018-01-11 東洋紡株式会社 ブラインの処理方法、塩水の淡水化処理方法、ブラインの処理システム、および、塩水の淡水化処理システム
JP2018069198A (ja) * 2016-11-02 2018-05-10 東洋紡株式会社 濃縮方法および濃縮装置

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5575015B2 (ja) * 2011-03-07 2014-08-20 株式会社日立製作所 淡水製造システム
JP6977247B2 (ja) * 2016-10-21 2021-12-08 東洋紡株式会社 濃縮方法および濃縮装置

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0663362A (ja) * 1992-08-24 1994-03-08 Kurita Water Ind Ltd 膜分離装置
JPH10137758A (ja) * 1996-11-14 1998-05-26 Shinko Pantec Co Ltd 水処理方法及び水処理装置
WO2013146391A1 (fr) * 2012-03-30 2013-10-03 東レ株式会社 Procédé de séparation et de récupération d'un métal alcalin et appareil de séparation et de récupération d'un métal alcalin
JP2018001110A (ja) * 2016-07-05 2018-01-11 東洋紡株式会社 ブラインの処理方法、塩水の淡水化処理方法、ブラインの処理システム、および、塩水の淡水化処理システム
JP2018069198A (ja) * 2016-11-02 2018-05-10 東洋紡株式会社 濃縮方法および濃縮装置

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2022040928A (ja) * 2020-08-31 2022-03-11 オルガノ株式会社 濃縮方法、濃縮装置、水処理方法、および水処理装置
JP7516167B2 (ja) 2020-08-31 2024-07-16 オルガノ株式会社 濃縮方法、濃縮装置、水処理方法、および水処理装置
CN112370969A (zh) * 2020-12-08 2021-02-19 郑州大学 一种低能耗膜分离方法及配套装置
JP2022090763A (ja) * 2020-12-08 2022-06-20 オルガノ株式会社 無機塩回収装置および無機塩回収方法
JP7587973B2 (ja) 2020-12-08 2024-11-21 オルガノ株式会社 無機塩回収装置および無機塩回収方法
WO2024117062A1 (fr) * 2022-12-01 2024-06-06 東洋紡エムシー株式会社 Procédé de concentration de solvant et système de concentration de solvant

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