WO2016059691A1 - Procédé de production d'eau purifiée à usage quotidien et appareil de production de cette eau - Google Patents

Procédé de production d'eau purifiée à usage quotidien et appareil de production de cette eau Download PDF

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Publication number
WO2016059691A1
WO2016059691A1 PCT/JP2014/077499 JP2014077499W WO2016059691A1 WO 2016059691 A1 WO2016059691 A1 WO 2016059691A1 JP 2014077499 W JP2014077499 W JP 2014077499W WO 2016059691 A1 WO2016059691 A1 WO 2016059691A1
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water
membrane
raw water
nucleating agent
raw
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PCT/JP2014/077499
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English (en)
Japanese (ja)
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丸木祐治
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株式会社タカギ
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Priority to PCT/JP2014/077499 priority Critical patent/WO2016059691A1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
    • 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
    • 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
    • B01D61/16—Feed pretreatment
    • 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
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities

Definitions

  • the present invention relates to water treatment technology.
  • Patent Document 1 a filtration apparatus using a membrane module is known (for example, Patent Documents 1 to 3).
  • Patent Document 1 a plurality of membrane modules, an introduction line for introducing a stock solution to the primary side of each of the membrane modules, and a secondary side of each of the membrane modules are connected and filtered by the membrane module.
  • a filtration liquid discharge line for discharging the filtrate, and at the time of backwashing, the flow path of the introduction line communicating with the membrane module to be backwashed is provided in the introduction line in a filtration device that is closed
  • the flow path from the membrane module to be backwashed during backwashing is opened and connected to the primary side of each of the membrane modules and the backwash line through which the filtrate flows as backwashing liquid.
  • Patent Document 2 in a method of operating a membrane separation apparatus having a plurality of membrane modules having a common permeate line, the permeate from other membrane modules is used when backwashing is performed in some membrane modules.
  • a method of operating a membrane separation device characterized in that it is supplied to the secondary side of the membrane module to be backwashed by the discharge pressure and then pressurized gas is supplied to the secondary side.
  • Patent Document 3 discloses that in a membrane filtration apparatus including a plurality of membrane modules, a membrane passage that performs backwashing is directly passed with membrane permeated water obtained from another membrane module and backwashed. Equipped with a fluid passage switching mechanism for switching, a compressor and air piping for supplying pressurized air to each membrane module, stops the introduction of raw water into the membrane module performing backwashing, and instead pressurizes from the compressor Introduce air to the primary side of the membrane module for backwashing and introduce permeated water from other membrane modules to the secondary side of the membrane module for backwashing to perform backwashing or backwashing.
  • a membrane filtration device configured to supply pressurized air to the secondary side of a membrane module that performs washing, mix in backwash water, and backwash with a gas-liquid mixed fluid.
  • the main pipe is connected, and the raw water main pipe Branch pipes are branched, the end side of each raw water branch pipe is connected to the raw water inlet of each membrane module, each raw water branch pipe is provided with an open / close valve, and the concentrated water outlet of each membrane module is connected via the pipe
  • the three-way valve is connected to an inflow port of the three-way valve, and each of the three-way valves has two outflow ports. One of the outflow ports is connected to a branch pipe for circulating the concentrated water.
  • one end of the branch pipe for backwash drainage is connected to the other outflow port of the three-way valve, and the other end of the branch pipe is connected to the main pipe for backwash drainage discharge
  • One end of a branch pipe for extracting permeate is connected to the permeate outlet of the membrane module, and the other end of the branch pipe is connected to a main pipe for extracting permeate, Raw water branch piping
  • the end side of the air branch pipe is connected to the portion between each on-off valve and each membrane module, the upstream end side of each air branch pipe is connected to the air main pipe, and this air main pipe is connected to the compressor.
  • Patent Document 4 is a coagulation filtration apparatus for filtering water to be treated, which has flocs formed by adding a flocculant, with a membrane module, and is provided with an addition unit for adding the flocculant to the water to be treated.
  • An aggregating and filtering apparatus comprising: a stirrer that stirs water to be treated with a flocculant added downstream of the adding unit; and the membrane module that is disposed downstream of the agitator. It is disclosed.
  • a water treatment method using ferric hydroxide colloid is known.
  • a ferrous salt aqueous solution and a positively charged ferric hydroxide colloid solution are added to water to be treated and stirred, and then the pH of the water is adjusted to 6-8.
  • a water purification method is disclosed, in which an organic substance or an inorganic substance dissolved or dispersed in water is removed by precipitation and a porous membrane.
  • Patent Document 6 in a wastewater treatment method for reducing COD of wastewater with high COD in which phenols are dissolved, (1) ferrous chloride aqueous solution, ferric chloride aqueous solution, or ferrous chloride in an oxidized state An aqueous solution mixed with ferric chloride or an aqueous solution of ferric hydroxide colloid having an average particle size of 4 nm or more and less than 30 nm is added, or iron is generated by electrolysis of the waste water using iron as an anode.
  • the pH of the waste water is adjusted by mixing an alkaline aqueous solution or an aqueous acid solution to 5 or more and less than 9, and (3) after removing the generated precipitate, (4) with an average particle size of 10 nm or more
  • a method for treating waste water which comprises adding a ferric hydroxide colloid aqueous solution of less than 20 nm to remove precipitates.
  • a method of adding a flocculant and precipitating and removing agglomerates requires a coagulation sedimentation tank, which increases the size of the apparatus.
  • a coagulation sedimentation tank which increases the size of the apparatus.
  • it is required to reduce the size of the filtration device.
  • a foreign material will clog the filtration membrane with which a membrane module is provided, and filtration efficiency will fall.
  • it is necessary to back-wash the membrane module.
  • Patent Documents 5 and 6 disclose a water treatment technique that uses ferric hydroxide colloid and diffuses and filters pores using a porous membrane.
  • the pore diffusion / filtration method is a method of performing filtration by a cross flow method with a transmembrane pressure difference of 0.3 atm or less, and has a low raw water treatment capacity.
  • the porous flat membrane is used, there is a problem that the apparatus becomes large in order to increase the raw water treatment amount.
  • This invention is made
  • Another object of the present invention is to reduce the size of a central water purification apparatus that supplies clean water for daily use to the entire building such as a condominium and a building.
  • the method for producing domestic water for purification according to the present invention is a method for producing domestic water for purification by adding a nucleating agent to raw water and filtering with a membrane means, wherein the nucleating agent has a weight average particle diameter of 5 nm to 160 nm.
  • the ratio of the iron mass of the aqueous ferric hydroxide colloidal particles to the total mass of iron added to the raw water is set to 0.9 or more. It is characterized by that.
  • the commercially available flocculants are suitable for aggregating colloidal particles of about 100 ⁇ m to 1 ⁇ m floating in the water to be treated, for example, but agglomerate ionic substances and ionic molecules such as small metal ions. Is difficult.
  • the present inventors used an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm (hereinafter sometimes simply referred to as “aqueous dispersion of ferric hydroxide”). For example, the inventors have found that the effect of capturing ionic substances and ion molecules such as heavy metal ions having a small particle size is increased, and the present invention has been completed.
  • the aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm used in the present invention adsorbs ionic impurities contained in the raw water by the charge effect due to the potential, It is considered that the particle grows as the center and has an effect of increasing the particle size. Furthermore, an aggregate in which particles centering on a nucleating agent are aggregated may be generated. In the present invention, an aqueous dispersion of ferric hydroxide colloidal particles having such an effect is called a “nucleating agent” and is distinguished from a general flocculant.
  • the general flocculant is intended to agglomerate impurities, to enlarge and precipitate the aggregate, and to remove it, in the method for producing purified water for daily use of the present invention, the flocculating agent formed by the “nucleating agent” It is characterized in that it is filtered directly by membrane means without precipitating the product.
  • the nucleating agent if an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm is used as the nucleating agent, the particle size of the aggregate formed by the “nucleating agent” is controlled, There is an effect of suppressing the blockage of the membrane means. As a result, a certain amount of clean water for daily use can be stably supplied.
  • the apparatus used in the method for producing domestic purified water according to the present invention includes a raw water supply channel, a raw water supply unit that is disposed in the raw water supply channel, and feeds the raw water, and a plurality of branching the raw water supply channel into at least two or more.
  • a separation tank that precipitates and separates agglomerates generated by the addition of a nucleating agent.
  • the present invention it is possible to provide clean water for daily use from which ionic impurities such as heavy metal ions and arsenic are efficiently removed. Moreover, according to this invention, the water purifier with high backwashing efficiency is obtained.
  • the water purifier of the present invention can be reduced in size.
  • the manufacturing method of domestic water purification of this invention is a manufacturing method of domestic water purification which adds a nucleating agent to raw
  • a nucleating agent Using an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm, the mass of iron in the aqueous dispersion of ferric hydroxide colloidal particles relative to the total mass of iron added to the raw water The ratio is made 0.9 or more.
  • ionic impurities such as heavy metal ions having a small particle size contained in the raw water are captured by the nucleating agent and efficiently removed.
  • raw water to be treated by the method for producing water for daily life of the present invention will be described.
  • the raw water include natural water or tap water.
  • Natural water is fresh water that exists in the natural world such as well water, groundwater, rainwater, rivers, ponds, and lakes.
  • Tap water is purified water supplied from a water purification facility.
  • the raw water to be treated in the present invention does not include industrial wastewater, industrial wastewater and the like. This is because industrial wastewater and industrial wastewater have many types of impurities and have a high concentration of impurities, so that the impurities cannot be removed even by the present invention and are not acceptable as clean water for daily use.
  • natural water can be removed.
  • the ionic impurities contained in the raw water include heavy metal ions such as iron (Fe 2+ , Fe 3+ ), cadmium (Cd 2+ ), copper (Cu 2+ ), lead (Pb 2+ ), arsenic (AsO 4 3 ⁇ , etc.) Metal ions such as aluminum (Al 3+ ) can be removed. According to the present invention, both anionic impurities and cationic impurities can be removed.
  • an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm used as a nucleating agent in the present invention will be described.
  • the aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of 5 nm to 160 nm used in the present invention adsorbs ionic impurities contained in the raw water by the charge effect due to electric potential, and the particles are mainly composed of colloidal particles. Are believed to grow and become larger in particle size. Furthermore, the grown particles centering on the nucleating agent may aggregate to form an aggregate.
  • the present invention by using a ferric hydroxide colloid particle aqueous dispersion having a weight average particle size of 5 nm to 160 nm as a nucleating agent, an ionic impurity having a small particle size contained in raw water (heavy metal ions, arsenic, Ionic substances such as fluorine) can be efficiently captured.
  • the weight average particle size of the nucleating agent is preferably controlled to 5 nm to 160 nm.
  • the weight average particle size of the aqueous dispersion of ferric hydroxide is more preferably 10 nm or more, further preferably 15 nm or more, preferably 50 nm or less, more preferably 40 nm or less, and further preferably 25 nm or less. If the weight average particle size becomes too small, the aqueous dispersion of ferric hydroxide may permeate the membrane means. Moreover, when the weight average particle diameter becomes too large, the effect of capturing ionic molecules such as arsenic and heavy metals is reduced. In the present invention, the weight average particle size of the aqueous dispersion of ferric hydroxide is measured by a dynamic light scattering method using, for example, DLS-8000 / 6500 manufactured by Otsuka Electronics Co., Ltd.
  • ferric hydroxide colloidal particle aqueous dispersion for example, a colloidal particle formed by adsorbing a negatively charged counterion on the outside of a positively charged ferric ion particle is dispersed in water.
  • the counter ion include sulfate ion, hydroxide ion, and chlorine ion.
  • FIG. 1 is an explanatory view schematically illustrating ferric hydroxide colloidal particles 100 used as a nucleating agent.
  • a layer 102 made of hydroxide ions (OH ⁇ ) as counter ions is formed on the surface of the nucleus 101 made of positively charged iron ions (Fe 3+ ).
  • the ferric hydroxide colloidal particles 100 have a high affinity with water and a high stability in water because the layer 102 made of hydroxide ions is formed outside the core 101 made of iron ions. .
  • a layer 103 made of iron ions (Fe 3+ ) Layers 104 made of hydroxide ions (OH ⁇ ) are alternately formed, and the particle diameter is increased.
  • FIG. 3 is an explanatory view schematically illustrating an aspect in which ferric hydroxide colloidal particles, which are nucleating agents, capture heavy metal ions (X ⁇ ).
  • X ⁇ heavy metal ions
  • a layer 102 made of hydroxide ions (OH ⁇ ) as counter ions is formed on the surface of the nucleus 101 made of positively charged iron ions (Fe 3+ ). Since the layer 102 of hydroxide ions (OH ⁇ ) is negatively charged, it attracts cations (M + ) and hydrogen ions (H + ) contained in the nucleating agent and raw water. As a result, a layer 105 made of positively charged cations is formed outside the layer 102 made of hydroxide ions.
  • the layer 105 made of cations attracts heavy metal ions (X ⁇ ) and hydroxide ions (OH ⁇ ), and the layer 106 made of anions is formed outside the layer 105 made of cations. Is done.
  • the electric charge effect by an electric potential becomes weak as it leaves
  • the nucleating agent grows particles by adsorbing the counter ion around the core of the metal ion. At that time, ionic impurities in the raw water are trapped inside the particles.
  • FIG. 4 shows a mode in which nucleated particles aggregate to form further aggregates.
  • the aqueous ferric hydroxide colloidal particle dispersion can be prepared, for example, by adding sodium hydroxide to ferric chloride and adjusting the pH to about 2.7 and heating. .
  • the average particle diameter can be controlled by the amount of iron ions added for the growth of trivalent iron ions and hydroxide ions or colloidal particles.
  • the aqueous dispersion of ferric hydroxide colloidal particles preferably has a pH adjusted to 1.5 to 4.0. This is because as the pH increases, the stability of the ferric hydroxide colloid may decrease. If the ferric hydroxide colloidal particle aqueous dispersion contains ferric chloride or other iron ions, the size of the aggregates generated from the raw water by the nucleating agent increases, and the membrane means is used. Since it becomes easy to block, by adjusting the amount of ferric chloride and sodium hydroxide, the aqueous dispersion of ferric hydroxide colloidal particles does not contain ferric chloride-derived iron ions. It is better to do so.
  • the total iron concentration of the aqueous dispersion of ferric hydroxide colloidal particles used as a nucleating agent is determined by the transportability of the nucleating agent and Considering the transportation cost, a high concentration is preferable. That is, the total iron concentration is preferably 1,000 mg / L or more, more preferably 3,000 mg / L or more, and further preferably 4,000 mg / L or more. However, if it exceeds 10,000 mg / L, it is self-aggregated to produce a precipitate, so that it is preferably 10,000 mg / L or less, more preferably 8,000 mg / L or less, and even more preferably 6,000 mg / L or less.
  • the total iron concentration is the total mass (mg) of iron (Fe) contained in 1 L of the aqueous dispersion of ferric hydroxide colloid particles. Total iron concentration is measured by ICP mass spectrometry.
  • nucleating agent for example, an aspect of adding the nucleating agent to the raw water stored in the raw water tank, an aspect of adding the nucleating agent to the raw water in the raw water supply path for supplying the raw water to the membrane means And so on.
  • the nucleating agent it is preferable to add the nucleating agent to the raw water immediately before the membrane means. If the aggregate particle size becomes too large, the aggregate may block the pores of the membrane means.
  • the amount of nucleating agent (aqueous dispersion of ferric hydroxide colloidal particles) added to the raw water exhibits a removal effect as the concentration increases, so that the total iron concentration is preferably 0.05 mg / L or more, 0 .3 mg / L or more is more preferable, and 0.5 mg / L or more is more preferable.
  • the amount of the nucleating agent added to the raw water is preferably 9 mg / L or less, more preferably 6 mg / L or less, and further preferably 4 mg / L or less in terms of total iron concentration. If it is 9 mg / L or less, the manufacturing cost can be reduced and the nucleating agent tank can be downsized.
  • the upper limit of the nucleating agent concentration relative to the raw water is preferably 3 mg / L, more preferably 2 mg / L, from the viewpoint of cost reduction. L is more preferable.
  • the addition amount of the nucleating agent is represented by the total mass (mg) of the iron component (Fe) of the nucleating agent (aqueous dispersion of ferric hydroxide colloid particles) added to 1 L of raw water.
  • the ratio of the mass of iron contained in the aqueous dispersion of ferric hydroxide colloid particles to the total mass of iron added to the raw water is set to 0.9 or more. That is, when an iron-containing aqueous liquid other than the aqueous dispersion of ferric hydroxide colloid particles is added to the raw water, the mass of iron contained in the aqueous dispersion of ferric hydroxide colloid particles is A, Aqueous dispersion of ferric hydroxide colloidal particles relative to the total mass of iron added to the raw water (A + B), where B is the mass of iron contained in the iron-containing aqueous liquid other than the aqueous dispersion of ferric colloidal particles
  • the mass ratio (A / (A + B)) of iron A contained in the product is preferably 0.9 or more, more preferably 0.95 or more, and even more preferably 0.99 or more.
  • the iron content of the aqueous dispersion of ferric hydroxide colloidal particles includes, for example, the iron content of the colloidal particles themselves and the colloidal particles.
  • the iron content derived from ferric chloride used as a raw material is included.
  • the iron-containing aqueous liquid other than the aqueous dispersion of ferric hydroxide colloidal particles include a ferrous chloride aqueous solution and a ferric chloride aqueous solution.
  • the iron content contained in the iron-containing aqueous liquid may be adsorbed on the colloidal particles to increase the particle size of the nucleating agent.
  • the value of (A / (A + B)) may be set to 0.99 or less, and may be set to 0.98 or less.
  • the iron concentration is measured by ICP mass spectrometry.
  • the raw water may contain iron ions.
  • the mass C of iron contained in the raw water, the mass of iron contained in the aqueous dispersion of ferric hydroxide colloid particles is A, and iron content other than the aqueous dispersion of ferric hydroxide colloid particles is contained.
  • the mass of iron contained in the aqueous liquid is B
  • the value of A / (A + B + C) is preferably 0.9 or more, more preferably 0.95 or more, and 0.99 or more. More preferably.
  • the iron contained in the raw water or the iron contained in the iron-containing aqueous liquid is adsorbed on the colloidal particles to increase the particle size of the nucleating agent.
  • the value of (A / (A + B + C)) may be set to 0.99 or less, and may be set to 0.98 or less.
  • the iron concentration is measured by ICP mass spectrometry.
  • the pH of raw water is preferably 4.5 or more, more preferably 5 or more, preferably 7.5 or less, more preferably 7 or less, and even more preferably 6.5 or less.
  • the pH may be adjusted by adding an alkali or acid to the raw water. Examples of the alkali include alkali solutions such as sodium hydroxide, potassium hydroxide, and ammonia.
  • Sodium hydroxide or potassium hydroxide is preferable and sodium hydroxide is more preferable because it is inexpensive and easy to handle.
  • the acid include hydrochloric acid, nitric acid, acetic acid, dilute sulfuric acid, and the like, and hydrochloric acid and dilute sulfuric acid are preferable, and hydrochloric acid is more preferable because it is inexpensive and easy to handle.
  • the membrane means used in the present invention removes foreign matters such as fine particles and turbidity in raw water and discharges purified water.
  • the membrane means include filtration membranes such as reverse osmosis membranes (RO membranes), nanofiltration membranes (NF membranes), microfiltration membranes (MF membranes), and ultrafiltration membranes (UF membranes).
  • RO membranes reverse osmosis membranes
  • NF membranes nanofiltration membranes
  • MF membranes microfiltration membranes
  • UF membranes ultrafiltration membranes
  • a membrane means a microfiltration membrane (MF membrane) and an ultrafiltration membrane (UF membrane) are preferable from the viewpoint that raw water can be filtered at a relatively low pressure and low cost.
  • an ultrafiltration membrane (UF membrane) or a microfiltration membrane (MF membrane) is not used as the membrane means.
  • the ultrafiltration membrane (UF membrane) and microfiltration membrane (MF membrane) have larger pore diameters than the heavy metal ions, and the heavy metal ions in the raw water permeate the membrane means. Therefore, when removing heavy metal ions in raw water by a membrane means, it is necessary to use a reverse osmosis membrane (RO membrane) or nanofiltration membrane (NF membrane) having a small pore diameter.
  • RO membrane reverse osmosis membrane
  • NF membrane nanofiltration membrane
  • a hollow fiber membrane as the membrane means.
  • a filtration method all raw water is filtered through a filtration membrane to make purified water (dead-end filtration method), and raw water is run parallel to the surface of the filtration membrane.
  • a cross-flow filtration method that discharges both purified water that has been filtered through a filtration membrane
  • a full-volume filtration method that can increase the amount of purified water.
  • B / A is 1 to 20 More preferably.
  • B / A is preferably 2 or more, more preferably 5 or more, and preferably 10 or less, more preferably 7 or less.
  • the pore diameter B (nm) of the membrane means can be determined according to the bubble point method (JIS K 3832).
  • the size of the eyes is classified according to the molecular weight cut off using the substance to be separated as an index. That is, classification is performed based on the molecular weight of the marker that can be separated on the target membrane. Representative markers are shown in the table below.
  • the membrane rejection is defined by the ratio of the concentration of the target substance on the permeate side to the concentration of the target substance on the supply liquid side, and the separation performance can be evaluated.
  • the molecular weight of the target substance having a rejection rate of about 90% is defined as the fractional molecular weight.
  • the transmembrane pressure difference of the membrane means is preferably more than 0.03 MPa, more preferably 0.04 MPa or more, and further preferably 0.05 MPa or more. Preferably, it is 0.45 MPa or less, more preferably 0.3 MPa or less, further preferably 0.2 MPa or less, and particularly preferably 0.15 MPa or less.
  • the pressure on the primary side of the membrane means is preferably 0.08 MPa or more, more preferably 0.13 MPa or more, further preferably 0.15 MPa or more, preferably 0.50 MPa or less, more preferably 0.35 MPa or less. 0.25 MPa or less is more preferable.
  • the pressure on the secondary side of the membrane means is preferably 0.05 MPa or more, more preferably 0.10 MPa or more, further preferably 0.12 MPa or more, preferably 0.30 MPa or less, more preferably 0.25 MPa or less. 0.20 MPa or less is more preferable.
  • the ratio (V / S, (m / hr)) of the filtration amount V (m 3 ) per hour to the total filtration area S (m 2 ) of the membrane means is 0 .05 or more, preferably 0.1 or more, more preferably 0.3 or more, particularly preferably 0.5 or more, and 3.0 or less. Preferably, it is 2.5 or less, more preferably 2.0 or less.
  • the ratio is 0.05 or more and 3.0 or less, the amount of raw water treated per unit filtration area becomes a desired range.
  • the amount of raw water treated per unit filtration area is extremely small, and in order to increase the amount of raw water treated, the filtration area is increased.
  • the filtration device becomes larger.
  • a chemical solution may be added to the purified water for domestic use obtained by filtering with a membrane means, if necessary.
  • medical solution For example, hypochlorous acid, sodium hypochlorite, hypochlorous acid aqueous solution, etc. can be mentioned. Among these, it is preferable to use a sodium hypochlorite aqueous solution. By adding sodium hypochlorite, it ionizes to hypochlorite ions in water, and part of it reacts with water to form hypochlorous acid.
  • the chlorine concentration in the obtained purified water is preferably 0.3 mg / L or more in consideration of the relationship between sterilizing power and chlorine removal efficiency in the secondary water purification device. 0.4 mg / L or more is more preferable, 0.5 mg / L or more is more preferable, 0.8 mg / L or less is preferable, and 0.7 mg / L or less is more preferable.
  • the domestic purified water obtained by the production method of the present invention includes domestic water used for cooking, washing, bathing, showering, and drinking water.
  • the production method of the present invention is suitable for producing drinking water.
  • the water purification apparatus for domestic use of the present invention is an apparatus used in the method for manufacturing water for domestic use of the present invention, Raw water supply channel, Raw water supply means that is disposed in the raw water supply path and feeds raw water, A plurality of raw water branch paths that branch the raw water supply path into at least two or more; A membrane module that is disposed in the plurality of raw water branches and includes a plurality of membrane means for filtering raw water; A discharge path connected to a primary side of the plurality of membrane modules; A plurality of water purification branches connected to the secondary side of the plurality of membrane modules; A plurality of water purifying branches, and The primary side of the membrane module is provided with means for supplying a nucleating agent to raw water, and is not provided with a separation tank for precipitating and separating aggregates generated by the addition of the nucleating agent.
  • the nucleating agent contacts the impurity in the raw water, and the nucleating agent captures the impurity.
  • the nucleating agent that has captured the impurity cannot pass through the membrane means, and is removed from the raw water together with the impurity.
  • Means for supplying a nucleating agent comprising an aqueous dispersion of ferric hydroxide colloid particles having a weight average particle diameter of 5 nm to 160 nm is not particularly limited.
  • the water purifier of this invention does not provide the separation tank which precipitates and isolate
  • the production apparatus for domestic water purification of the present invention is configured so that the membrane module can be back-washed. This is for removing clogging of the membrane module and supplying clean water stably for a long period of time.
  • the manufacturing apparatus of this invention is demonstrated based on the aspect of the central water purifier comprised so that back washing
  • the central water purification apparatus 1 shown in FIG. 5 is disposed in the raw water supply path 3, the raw water supply path 3, a raw water supply means P ⁇ b> 1 that feeds the raw water, and a plurality of branches that branch the raw water supply path 3 into at least two or more A raw water branch 5A, 5B, a plurality of membrane modules 9A, 9B that are disposed in the plurality of raw water branches 5A, 5B and filter raw water, and membrane means 9c that filters the raw water included in the membrane modules 9A, 9B.
  • the passage 13 is provided with a tank 37 for storing a nucleating agent, and a supply means P3 for supplying the nucleating agent.
  • the side on which raw water is supplied to the membrane means is referred to as the primary side
  • the side from which the purified water is discharged from the membrane means is referred to as the secondary side.
  • the raw water supply path 3 supplies raw water to be subjected to purification treatment such as tap water and natural water.
  • the raw water supply channel 3 is preferably connected to a raw water tank that stores tap water from a water main supplied to a building such as an apartment, an apartment, a building, a hotel, or a plurality of detached houses. It can also be connected directly to the main.
  • the raw water supply path 3 is constituted by a pipe line having a predetermined pipe diameter.
  • the raw water supply path 3 preferably includes an inflow valve (first valve V1) for opening and closing the raw water supply path 3.
  • the inflow valve may be a check valve.
  • raw water supply means P1 for sending raw water is disposed.
  • the raw water supply means P1 include a vertical multi-stage centrifugal pump, a horizontal multi-stage centrifugal pump, and a positive displacement pump. Among these, it is preferable to use a vertical multistage centrifugal pump as the raw water supply means P1 because the raw water is stably pressurized and fed.
  • the downstream end of the raw water supply path 3 is connected at the branch point 4 to the upstream ends of the raw water branch paths 5A and 5B that branch the raw water supply path 3 into a plurality.
  • the raw water branch paths 5A and 5B are constituted by pipe lines having a predetermined pipe diameter.
  • the raw water branch paths 5A and 5B include inflow valves (second valve V2 and third valve V3) for opening and closing the raw water branch paths 5A and 5B, respectively.
  • the downstream ends of the raw water branch paths 5A and 5B are connected to membrane modules 9A and 9B that filter the raw water.
  • the membrane modules 9A and 9B remove foreign matters such as fine particles and turbidity in the raw water, and discharge purified water.
  • the membrane modules 9A and 9B include membrane means 9c for filtering raw water and a cylindrical container 9d for housing the membrane means 9c.
  • the raw water region 9e to which raw water is supplied and the purified water filtered by the membrane means flow into the cylindrical container 9d with the membrane means 9c for filtering the raw water interposed therebetween. It is preferable to provide the purified water region 9f.
  • the membrane modules 9A and 9B are provided with a raw water inlet 9g and a purified water outlet 9h, and further with a concentrated water outlet 9i for discharging concentrated water.
  • the raw water inlet 9g and the concentrated water outlet 9i are connected to the raw water area 9e of the membrane modules 9A and 9B, and the purified water outlet 9h is connected to the purified water area 9f of the membrane modules 9A and 9B.
  • the membrane module may be either an external pressure type or an internal pressure type, preferably an internal pressure type.
  • membrane it is preferable to use a hollow fiber membrane comprising an ultrafiltration membrane (UF membrane) or a microfiltration membrane (MF membrane).
  • UF membrane ultrafiltration membrane
  • MF membrane microfiltration membrane
  • the water purifier of the present invention has means for supplying a nucleating agent.
  • the means for supplying the nucleating agent includes a tank 37 for storing the nucleating agent, a supplying means P3 for supplying the nucleating agent, and a nucleating agent supply path 6.
  • the nucleating agent is supplied to the raw water stored in the raw water tank 35. It is also preferable to provide the raw water tank 35 with a stirring function such as stirring by a stirring blade or stirring by a circulation pump.
  • the stirring function can increase the contact efficiency between the nucleating agent and various ions, and can contribute to increasing the particle size of the nucleating agent.
  • nucleating agent supply path 6 is composed of a pipe having a predetermined pipe diameter.
  • the discharge path is a flow path for discharging the backwash water when the membrane module is mainly backwashed.
  • the said discharge path should just be connected to the upstream of the membrane means 9c with which membrane module 9A, 9B is equipped, for example, the aspect connected to the raw
  • the discharge passages 7A and 7B are preferably composed of pipe passages having a predetermined pipe diameter, and are provided with valves (fourth valve V4 and fifth valve V5) for opening and closing the respective passages.
  • the discharge paths 7A and 7B may further merge.
  • the upstream ends of the purified water branch paths 11A and 11B are connected to the downstream side of the membrane modules 9A and 9B.
  • the purified water branch paths 11A and 11B are connected to the purified water discharge port 9h of the membrane modules 9A and 9B.
  • the downstream sides of the purified water branch paths 11A and 11B are formed so that the purified water branch paths 11A and 11B connected at the junction 17 and connected to the plurality of membrane modules communicate with each other.
  • the junction 17 is provided with a three-way cock 49 for switching the flow path. Instead of the three-way cock 49, an open / close valve for switching the flow path may be provided on the downstream side of the purified water branch paths 11A and 11B.
  • the raw water branch 5A and 5B are preferably provided with pressure gauges 14A and 14B for measuring the pressure of the raw water flowing in the raw water branch. Moreover, it is preferable that the pressure gauges 16A and 16B which measure the pressure of the purified water which flows through the inside of the purified water branch are provided in the purified water branches 11A and 11B.
  • the purified water path 13 is connected to the junction 17 of the purified water branch paths 11A and 11B.
  • the water purification channel 13 is provided with a valve (eighth valve V8) for opening and closing the water purification channel 13.
  • the water purification path 13 is composed of a pipe having a predetermined pipe diameter. It is preferable that the purified water path 13 is provided with a purified water discharge path 19 for discharging purified water.
  • the purified water discharge path 19 is constituted by a pipeline having a predetermined pipe diameter, and includes a valve (a ninth valve V9) for opening and closing the purified water discharge path 19.
  • the control means 21 preferably includes, for example, an inverter control unit 23, a valve control unit 25, a membrane differential pressure calculation unit 27, a display 29, a manual switch 31, a timer 33, and the like.
  • the water purifier 1 in FIG. 5 has an inverter control unit 23 that controls the raw water supply means P1. It is preferable to control the raw water pressure supplied by the raw water supply means by controlling the raw water supply means P1 with an inverter.
  • the inverter control unit 23 controls the raw water supply means P1 so that the pressure of the raw water is substantially constant during the production of purified water, and controls the raw water supply means P1 so that the pressure of the raw water pulsates during the reverse cleaning operation. .
  • the membrane differential pressure calculation unit 27 receives the measurement values of the pressure gauges 14A, 14B, 16A, and 16B, and calculates the transmembrane pressure difference between the primary side and the secondary side of the membrane modules 9A and 9B. For example, the membrane differential pressure calculation unit 27 instructs the valve control unit 25 to switch the valve so as to perform the purified water production operation or the reverse cleaning operation in accordance with the data of the transmembrane differential pressure.
  • the valve control unit 25 opens and closes the valve based on manual switch operation data, transmembrane pressure data supplied by the membrane pressure calculation unit, time data supplied by a timer, and the like.
  • the valve controller and each valve are preferably connected by wire or wirelessly.
  • the timer 33 measures the time of the normal filtration operation and the time of the back washing operation, and when each operation time reaches a predetermined time, the water purification manufacturing operation or the back washing operation is performed on the valve control unit 25. Thus, it is possible to instruct switching of the valve.
  • the indicator 29 can display, for example, the pressure value received from the pressure gauge, the transmembrane pressure difference, the current operation process, and the like.
  • the purified water obtained by the purified water manufacturing apparatus 1 is shown in figure so that it may be supplied to the water receiving tank 45, the water receiving tank 45 is not necessarily required.
  • the raw water tank 35 and the water receiving tank 45 include level meters L1 and L2.
  • the valve control unit 25 switches the valve so that the normal filtration operation and the reverse cleaning operation are switched when a certain amount of raw water is processed. You may be instructed.
  • the membrane module is described based on a form having the first membrane module 9A and the second membrane module 9B, but the number of membrane modules is preferably two or more.
  • the aspect which has two or more pairs of membrane module sets which consist of a 1st membrane module and a 2nd membrane module can be mentioned. Since the water purifier of the present invention has a plurality of pairs of membrane module sets each composed of a first membrane module and a second membrane module, the amount of raw water treated can be increased.
  • the purified water obtained from one membrane module in a filtered state is configured to be used as backwash water for another one membrane module to be backwashed. That is, the ratio of the number of membrane modules in a filtered state to the membrane module to be backwashed is 1: 1.
  • the purified water obtained from a plurality of membrane modules in a filtered state may be merged and used as backwash water for one membrane module to be backwashed, or 1 in a filtered state. You may comprise so that the purified water obtained from one membrane module may be branched and used as the backwash water of the several membrane module used as the backwash object.
  • membrane module to be backwashed multiple: 1
  • the pressure of backwashing water becomes too high, and there is a risk of damaging the filtration membrane provided in the membrane module to be backwashed.
  • the membrane module to be backwashed 1: many
  • the pressure of backwashing water is lowered, so that the backwashing efficiency may be lowered. Therefore, it is preferable that the ratio of the number of membrane modules in a filtered state and the number of membrane modules to be backwashed is 1: 1.
  • the water purification apparatus of the present invention can be suitably used as a central water purification apparatus that can supply purified water to buildings such as apartments, apartments, buildings, hotels, and multiple houses.
  • the amount of purified water supplied from the central water purification apparatus is appropriately set according to the number of supply destinations and the amount of water used.
  • the supply amount of purified water of the central water purification device is preferably 3,000 L / hour or more, and 4,000 L / hour. More preferably, 5,000 L / hour or more is more preferred, 8,000 L / hour or less is preferred, 7,000 L / hour or less is more preferred, and 6,000 L / hour or less is more preferred.
  • the water purification method using the water purification apparatus of FIG. 5 supplies raw water in parallel to a plurality of membrane modules having at least a first membrane module and a second membrane module, and filters the raw water through the plurality of membrane modules.
  • FIG. 6 is a view showing a water flow state of the water purifier 1 of the present invention in the water purification production process.
  • the first to third valves V1 to V3 and the eighth valve V8 are released, and the fourth to seventh valves V4 to V7 and the ninth valve V9 are closed.
  • a raw water treatment line is formed in which the raw water supply path 3, the raw water branch paths 5A and 5B, the purified water branch paths 11A and 11B, and the purified water path 13 communicate with each other through the membrane modules 9A and 9B.
  • the valve opening / closing operation may be automatic control by the valve control unit or may be manually controlled.
  • the raw water supply means P1 preferably pressurizes the raw water and sends it to the raw water supply path.
  • the pressure of the raw water is preferably set as appropriate according to the allowable pressure of the membrane module to be used.
  • the allowable pressure is about 0.35 MPa
  • the pressure Pf of the pressurized raw water is preferably 0.08 MPa or more, 0.13 MPa or more is more preferable, 0.15 MPa or more is more preferable, 0.35 MPa or less is preferable, 0.32 MPa or less is more preferable, and 0.30 MPa or less is more preferable.
  • the pressure Pf of the pressurized raw water exceeds the allowable pressure, the filtration membrane is easily damaged. Moreover, if the pressure Pf of the pressurized raw water is too low, the flow rate of the raw water is reduced. In the purified water production process, the pressure Pf of the raw water is preferably substantially constant.
  • the raw water branches at the branch point 4 and is supplied to the first and second membrane modules 9A and 9B through the raw water branch paths 5A and 5B.
  • the raw water is filtered by the first and second membrane modules 9A and 9B. Foreign matter and turbidity contained in the raw water are removed by the membrane module. Impurities contained in the raw water (heavy metal ions, arsenic, fluorine, etc.) are captured by the nucleating agent and removed from the raw water by the membrane means.
  • the fourth and fifth valves V4 and V5 are opened, and the concentrated water is filtered while being discharged from the discharge passages 7A and 7B.
  • a method may be adopted.
  • the purified water discharged from the first and second membrane modules 9A and 9B merges at the junction 17 through the purified water branch paths 11A and 11B, and flows out to the purified water path 13, respectively.
  • raw water is supplied to one of the first membrane module or the second membrane module and filtered, and at least a part of the obtained purified water is used as backwash water from the downstream side of the other membrane module.
  • the other membrane module is back-washed by flowing back to the side.
  • the first membrane module is operated in the filtration state and the second membrane module is backwashed
  • the first and second valves V1, V2, the fifth valve V5, and the eighth valve V8 are released, and the third, fourth, The sixth and seventh valves V3, V4, V6, V7 and the ninth valve V9 are closed.
  • the valve opening / closing operation may be automatic control by the valve control unit or may be manually controlled.
  • a raw water treatment line is formed in which the raw water supply path 3, the raw water branch path 5A, the purified water branch path 11A, and the purified water path 13 communicate with each other through the membrane module 9A. Further, a backwash line is formed in which the purified water branch path 11B and the discharge path 7B communicate with each other via the second membrane module 9B.
  • the backwash water that has entered the second membrane module 9B passes through the membrane means 9c disposed in the second membrane module 9B, and flows out from the upstream concentrated water discharge port 9i to the discharge path 7B. At this time, the foreign matter adhering to the membrane means 9c of the second membrane module 9B is released and flows out into the discharge path 7B together with the backwash water.
  • the foreign matter adhering to the backwash water and the second membrane module 9B is discharged out of the water purifier from the discharge path 7B connected to the concentrated water discharge port 9i.
  • the foreign matter adhering to the film means 9c includes a nucleating agent adhering to the film means 9c and an aggregate formed by the nucleating agent.
  • the remaining portion of the purified water discharged from the first membrane module 9A flows out to the purified water channel 13. Thereby, it is possible to continue discharging a certain amount of purified water while backwashing the second membrane module 9B.
  • the eighth valve V8 may be closed and all the purified water discharged from the first membrane module 9A may be backwashed water.
  • a line in which the purified water branch path 11B, the second membrane module 9B, and the discharge path 7B communicate with each other is adopted as the backwash line.
  • the purified water branch path 11B, the raw water branch path 5B, and the discharge path 15B are adopted.
  • the raw water supply means P1 may supply the raw water to the first membrane module 9A while pulsating the water pressure of the raw water.
  • Supplying the raw water to the first membrane module 9A while pulsating the water pressure of the raw water pulsates the purified water discharged from the first membrane module 9A, that is, the backwash water pressure, so that the reverse of the second membrane module 9B This is because the cleaning efficiency is increased.
  • As a method of pulsating the water pressure of the raw water for example, it is preferable to continuously change the rotation speed of the raw material supply means P1 by the inverter control unit 23.
  • the first, third valves V1, V3, the fourth valve V4, and the eighth valve V8 are released,
  • the second, fifth, sixth, and seventh valves V2, V5, V6, V7, and the ninth valve V9 may be closed to perform the same operation.
  • the valve opening / closing operation may be automatic control by the valve control unit or may be manually controlled.
  • a raw water treatment line is formed in which the raw water supply path 3, the raw water branch path 5B, the purified water branch path 11B, and the purified water path 13 communicate with each other through the second membrane module 9B. Moreover, the purified water branch path 11A and the discharge path 7A form a backwash line communicating with the first membrane module 9A.
  • the backwash line in which the purified water branch path 11A and the discharge path 7A communicated with each other via the first membrane module 9A is adopted as the backwash line.
  • the purified water branch path 11A and A line in which the raw water branch 5A and the discharge path 15A communicate with each other via the first membrane module 9A may be adopted.
  • the method for producing purified water of the present invention in which a nucleating agent is added to raw water and filtered through a membrane module provided with membrane means includes, for example, the following steps, and includes the following steps (2) to (4) as appropriate: It is preferable to carry out switching.
  • (1) Step of adding a nucleating agent to raw water (2) Purified water production step of filtering raw water through both the first membrane module and the second membrane module (3) The first membrane module is put into a filtered state, and the second membrane module (4) Backwashing process in which the second membrane module is in the filtered state and the first membrane module is in the backwashed state.
  • manual switch operation data, membrane differential pressure calculation This is preferably performed based on differential pressure data supplied by the unit, time data supplied by the timer, and the like.
  • the time of the water purification production process may vary from several minutes to several hours to several days.
  • the time for the back washing step is, for example, preferably 30 seconds or more, more preferably 1 minute or more, particularly preferably 5 minutes or more, preferably 20 minutes or less, more preferably 10 minutes or less, and particularly preferably 7 minutes or less.
  • the present invention has been described based on preferred embodiments, but the present invention is not limited to the above-described embodiments, and the shape, configuration, arrangement, and the like of each embodiment are within the scope of the present invention. Materials, processes, and the like can be changed as appropriate. In addition, the definitions of the configuration, arrangement, material, shape, numerical range, process, and the like shown in each embodiment can be applied independently or in combination of any two or more rules.
  • nucleating agent aqueous dispersion of ferric hydroxide colloidal particles
  • An aqueous dispersion of viscosity was obtained.
  • particle size control of nucleating agent The weight average particle diameter of the nucleating agent was proportional to the ratio of ferric chloride and was controlled by the mixing ratio of ferric chloride and sodium hydroxide.
  • Flocculant As comparative flocculants, the following commercial products were used.
  • Flocculant 1 Polyglutamic acid-based flocculant
  • Flocculant 2 Polyglutamic acid-based flocculant (including magnetic substance)
  • Flocculant 3 Inorganic flocculant (mainly Shirasu)
  • Coagulant 4 Calcium salt type coagulant
  • Coagulant 5 Zeolite type coagulant
  • Method removal test (1) Removal test for various metals A nucleating agent (an aqueous dispersion of ferric hydroxide colloid particles having a weight average particle diameter of about 10 nm) was added to 50 mL of raw water in which various metal components were adjusted to predetermined concentrations. . The nucleating agent was added so that the total iron concentration relative to the raw water was 0.6 mg / L. After the nucleating agent was added, the liquid to be treated was stirred for 1 minute to generate aggregates. Thereafter, the liquid to be treated was filtered through a filter membrane (filter paper: Advantec No. 2, pore size: 5 ⁇ m), and the removal rate was calculated. The calculated removal rate is shown in Table 2.
  • filter paper Advantec No. 2, pore size: 5 ⁇ m
  • the removal load index is a comprehensive index for determining filtration performance expressed by the concentration difference before and after the filtration process ⁇ the treatment amount.
  • Cd were used as heavy metals.
  • the heavy metal concentration and the removal load index before and after the filtration treatment are shown in FIGS.
  • the removal rate of heavy metals is shown in Table 3. In a filtration experiment using filter paper, heavy metals contained in raw water may be adsorbed on the filter paper. Therefore, the overall removal rate including the filter paper and the blank test without adding the nucleating agent and the flocculant showed the removal rate (chemicals only) excluding the influence of the filter paper.
  • the nucleating agent used in the present invention shows a higher removal performance than the flocculants 1-5.
  • the purified water was manufactured using the experimental machine which combined the nucleating agent supply means and the ultrafiltration membrane (UF membrane). That is, in the raw water tank, the raw water whose metal concentration was adjusted to 0.02 mg / L was adjusted to pH 5.5, 6.5, 7.5, and 8.5, respectively. Thereafter, a nucleating agent (an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of about 10 nm) is added from the nucleating agent storage tank to a total iron concentration of 0.12 mg / L, 0.36 mg / L. , 0.6 mg / L was added to the raw water, and the liquid to be treated was stirred for 2 minutes to generate aggregates.
  • a nucleating agent an aqueous dispersion of ferric hydroxide colloidal particles having a weight average particle diameter of about 10 nm
  • the liquid to be treated was filtered using a UF membrane (Membrane Tensha, pore size: about 100 nm) under the following conditions.
  • Transmembrane differential pressure 0.11 MPa
  • Primary pressure 0.24 MPa
  • Secondary pressure 0.13 MPa
  • FIG. 13 is a graph showing the relationship between the pH of raw
  • FIG. 14 is a graph showing the relationship between the pH of raw water and the concentration of heavy metals in purified water after filtration for Pb. From the results of FIG. 13, it can be seen that the removal effect is obtained at pH 8.5, and the removal effect of As is higher when the pH is lower than 8.5. Moreover, it can be seen from the results of FIG. 14 that the effect of removing Pb is higher when the pH is higher than 5.5.
  • the nucleating agent was added to the total iron concentration of 0.12 mg / L, 0.36 mg / L, 0.6 mg. / L was added, and the liquid to be treated was stirred for 1 minute to generate aggregates.
  • the liquid to be treated was filtered through a filtration membrane (Advantec No. 2: pore size: 5 ⁇ m), and the removal rate was calculated.
  • the nucleating agent those having a weight average particle size of 15 nm, 25 nm, 50 nm, and 160 nm were used.
  • FIG. 15 is a graph showing the relationship between the As removal rate and the weight average particle size of the nucleating agent. It can be seen that the nucleating agent used in the present invention exhibits a high removal rate for As when the weight average particle diameter is in the range of 15 nm to 160 nm.
  • the central water purification apparatus of the present invention is small in size, can efficiently remove impurities such as heavy metal ions and arsenic, and has high backwashing efficiency.
  • the central water purification apparatus of this invention is suitable as a water purification apparatus which supplies purified water to the whole building, such as a condominium and a building.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé de production d'eau purifiée, ainsi qu'un appareil de purification d'eau permettant d'éliminer efficacement les impuretés telles que les ions de métaux lourds et l'arsenic. La présente invention permet de réduire la taille d'un appareil de purification d'eau central destiné à acheminer de l'eau purifiée à l'intégralité d'une structure telle qu'un bâtiment de bureaux ou d'appartements. Le procédé de production d'eau purifiée à usage quotidien selon l'invention consiste à ajouter un agent de nucléation à de l'eau brute et à filtrer l'eau à l'aide d'un moyen membranaire. Ce procédé se caractérise en ce que : pour ledit agent de nucléation, une dispersion aqueuse de particules colloïdales d'hydroxyde ferrique de 5 à 160 nm de diamètre de particule moyen en poids est utilisée ; et le rapport de la masse de fer dans les particules colloïdales d'hydroxyde ferrique et de la masse totale de fer ajouté à l'eau brute est d'au moins 0,9.
PCT/JP2014/077499 2014-10-16 2014-10-16 Procédé de production d'eau purifiée à usage quotidien et appareil de production de cette eau WO2016059691A1 (fr)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08206663A (ja) * 1995-02-03 1996-08-13 Suido Kiko Kaisha Ltd 浄水処理における透過膜によるヒ素の除去方法
JP2001286872A (ja) * 2000-04-05 2001-10-16 Kurita Water Ind Ltd 凝集処理装置の運転方法及び凝集処理装置
JP2002172395A (ja) * 2000-12-05 2002-06-18 Nec Environment Eng Ltd 濃厚無機成分含有排水の水酸化鉄凝集沈澱処理方法
JP2002320979A (ja) * 2001-04-27 2002-11-05 Sharp Corp 金属含有排水の処理方法および金属含有排水の処理装置
JP2010247057A (ja) * 2009-04-15 2010-11-04 Kurosaki:Kk 微粒子化法と膜除去法との組み合せによる水の浄化方法。
JP2012196657A (ja) * 2011-03-22 2012-10-18 Kurosaki:Kk フェノール類を含む排水の処理方法
JP2014057926A (ja) * 2012-09-19 2014-04-03 Takagi Co Ltd 浄水装置および浄水の製造方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08206663A (ja) * 1995-02-03 1996-08-13 Suido Kiko Kaisha Ltd 浄水処理における透過膜によるヒ素の除去方法
JP2001286872A (ja) * 2000-04-05 2001-10-16 Kurita Water Ind Ltd 凝集処理装置の運転方法及び凝集処理装置
JP2002172395A (ja) * 2000-12-05 2002-06-18 Nec Environment Eng Ltd 濃厚無機成分含有排水の水酸化鉄凝集沈澱処理方法
JP2002320979A (ja) * 2001-04-27 2002-11-05 Sharp Corp 金属含有排水の処理方法および金属含有排水の処理装置
JP2010247057A (ja) * 2009-04-15 2010-11-04 Kurosaki:Kk 微粒子化法と膜除去法との組み合せによる水の浄化方法。
JP2012196657A (ja) * 2011-03-22 2012-10-18 Kurosaki:Kk フェノール類を含む排水の処理方法
JP2014057926A (ja) * 2012-09-19 2014-04-03 Takagi Co Ltd 浄水装置および浄水の製造方法

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