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WO2018105569A1 - Procédé de traitement de l'eau et dispositif associé - Google Patents

Procédé de traitement de l'eau et dispositif associé Download PDF

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Publication number
WO2018105569A1
WO2018105569A1 PCT/JP2017/043524 JP2017043524W WO2018105569A1 WO 2018105569 A1 WO2018105569 A1 WO 2018105569A1 JP 2017043524 W JP2017043524 W JP 2017043524W WO 2018105569 A1 WO2018105569 A1 WO 2018105569A1
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WIPO (PCT)
Prior art keywords
water
humic substance
humic
water treatment
substance
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2017/043524
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English (en)
Japanese (ja)
Inventor
橋野　昌年
大祐 岡村
克輝 木村
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Asahi Kasei Corp
Hokkaido University NUC
Asahi Chemical Industry Co Ltd
Original Assignee
Asahi Kasei Corp
Hokkaido University NUC
Asahi Chemical Industry Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
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Priority to JP2018554993A priority Critical patent/JP7113454B2/ja
Publication of WO2018105569A1 publication Critical patent/WO2018105569A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • 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
    • B01D61/22—Controlling or regulating
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N15/00—Investigating characteristics of particles; Investigating permeability, pore-volume or surface-area of porous materials
    • G01N15/02—Investigating particle size or size distribution

Definitions

  • the present invention relates to a water treatment method and apparatus for clarifying water to be treated containing humic substances and polymer substances.
  • Filtration membranes used for the filtration of various raw waters are used in various separation membrane devices for reasons such as excellent filtration accuracy, a small installation space, and easy operation management.
  • a gas such as air is introduced as bubbles into the raw water side of the filtration membrane, and a backwash medium such as filtered water or clarified water is applied from the filtrate side in the direction opposite to the filtration direction.
  • back-pressure water cleaning (hereinafter referred to as back-washing) is performed to remove the deposits on the filtration surface of the membrane.
  • a method of adding sodium hypochlorite having an oxidizing action to the backwash medium a method of backwashing using ozone water (for example, Patent Document 1), and backwashing with ozonized pressurized air.
  • a washing method for example, Patent Document 2
  • a method for example, Patent Document 3 in which ozonized air is injected as bubbles into the raw water side of the filtration membrane is known.
  • humic substances such as humic acid and fulvic acid have been said to be the main cause of fouling when filtering natural water such as river water and seawater.
  • the fouling substance that induces clogging of the filtration membrane is a biopolymer composed of microorganism-derived polysaccharides and proteins.
  • seawater has a higher concentration of biopolymer than river water and is difficult to filter.
  • Patent Document 1 Methods for removing the humic substance from the water to be treated and subjecting it to membrane filtration are disclosed in Patent Document 1 and Patent Document 2.
  • Patent Document 2 Methods for removing the humic substance from the water to be treated and subjecting it to membrane filtration are disclosed in Patent Document 1 and Patent Document 2.
  • these methods can remove humic substances but cannot remove biopolymers, which is insufficient for stable membrane filtration.
  • the present invention has been made to solve such a problem, and it is possible to stably perform membrane filtration of water to be treated containing humic substances and biopolymers without causing clogging of the filtration membrane.
  • a water treatment method and apparatus are provided.
  • the water treatment method of the present invention is a water treatment method for clarifying water to be treated containing humic substances and a polymer substance.
  • humic substances are removed from water to be treated to produce humic-reduced water.
  • the humic substance can be removed by ion exchange treatment in the humic substance removing step.
  • the polymer substance can be aggregated with an inorganic flocculant in the polymer aggregation process.
  • the polymer substance can be a biopolymer.
  • the retention time of the water to be treated in the humic substance removing means for performing the humic substance removing process according to the biopolymer concentration in the aggregate-containing water, and the coagulating means for performing the polymer coagulating process is changed at least one of the retention time of the humic substance-reducing water and the addition amount of the flocculant.
  • the amount of ion exchange resin used in the humic substance removing step and the humic substance removing means are used so that the humic substance concentration in the humic substance-reduced water is 0.7 mg / L. At least one of the residence times of the water to be treated can be adjusted.
  • the biopolymer concentration in water after the aggregate-containing water is filtered through a 0.45 ⁇ m filter can be controlled to 40 ⁇ g / L or less.
  • the water treatment device of the present invention is a water treatment device that performs membrane filtration of water to be treated containing humic substances and a high-molecular substance, and removes humic substances from the water to be treated to provide humic substance-reduced water.
  • a membrane filtration means, and a humic substance removing treatment means and a coagulation means are provided in this order before the membrane filtration means.
  • the humic substance removal treatment means is preferably a treatment method using ion exchange means using powder ion exchange resin, adsorption with activated carbon, and decomposition with an oxidizing agent.
  • the aggregating means uses an inorganic aggregating agent.
  • a filtration membrane having a pore diameter of 0.2 ⁇ m or less as the membrane filtration means.
  • a biopolymer measuring apparatus can be provided after the aggregating means.
  • the biopolymer measuring apparatus is preferably LC-OCD (Liquid Chromatography-Organic Carbon Detection).
  • the biopolymer measurement apparatus removes the humic substance from the water to be treated by the humic substance removing treatment means, and then membrane-filtering with a filtration membrane having an average pore diameter of 50 nm or less possessed by the membrane filtering means. It is preferable to measure the total organic carbon concentration contained in the water.
  • the biopolymer in the water to be treated can be efficiently removed, clogging of the filtration membrane can be suppressed, and membrane filtration can be performed stably. Further, it is possible to operate by reducing the number of times the membrane is washed or increasing the filtration speed.
  • FIG. 1 is a diagram showing a schematic configuration of an embodiment of a water treatment apparatus of the present invention.
  • FIG. 2 is a flowchart for explaining an embodiment of the water treatment method of the present invention.
  • FIG. 3 is a diagram showing an LC-OCD chromatogram of organic substances in water in Example 1.
  • FIG. 1 is a block diagram showing an example of a water treatment apparatus according to an embodiment of the present invention.
  • the water treatment apparatus 1 of this embodiment includes a humic substance reducing means 2 such as an ion exchange means, a flocculant adding means 3 and a separation membrane device 4.
  • a humic substance reducing means 2 such as an ion exchange means
  • a flocculant adding means 3 and a separation membrane device 4.
  • water to be treated containing humic substances and a polymer substance is continuously or intermittently introduced into the humic substance reducing unit 2, and then the flocculant adding unit 3.
  • the flocculant is continuously or intermittently added to the separation membrane device 4.
  • a membrane filtration process is performed by the separation membrane device 4 in which a filtration membrane module is incorporated, and filtered water is obtained from the separation membrane device 4.
  • the ion exchange means corresponds to the humic substance removal processing means 2 of the present invention
  • the separation membrane device 4 corresponds to the membrane filtration means of the present invention
  • the flocculant The adding means 3 and the buffer tank 7 described later correspond to the aggregating means of the present invention.
  • natural water contains humic substances that are degradation products of microorganisms such as plants, and biopolymers that are metabolites of microorganisms.
  • humic substances that are degradation products of microorganisms such as plants
  • biopolymers that are metabolites of microorganisms.
  • the biopolymer is filtered. This causes clogging of the membrane, and the subsequent separation membrane device 4 does not operate stably. Further, even if only humic substance is reduced, stable operation by the separation membrane device 4 cannot be performed. Further, it was found that even if only the aggregation treatment was performed, the biopolymer could not be removed efficiently in the presence of humic substances.
  • FIG. 2 is a flowchart showing a flow of a water treatment method using the water treatment apparatus 1 of the present embodiment.
  • the water treatment apparatus 1 of the present embodiment includes a raw water supply pump 6, a buffer tank, in addition to the humic substance reduction means 2 such as the ion exchange means, the flocculant addition means 3, and the separation membrane device 4 described above. 7 and a filtration pump 8 are provided.
  • the water to be treated is continuously or intermittently supplied to the ion exchange means 2 by the raw water supply pump 6, and the humic substance is removed from the water to be treated by the humic substance reducing means 2.
  • the humic substance-reduced water is generated (S10).
  • the humic substance-reduced water produced by the humic substance-reducing means 2 is temporarily stored in the buffer tank 7.
  • the flocculant is continuously added to the humic substance-reduced water by the coagulant-adding means 3. Or intermittently (S12).
  • the high-molecular substance (biopolymer) in the humic substance-reduced water is aggregated to generate aggregate-containing water (S14).
  • the aggregate-containing water produced in the buffer tank 7 is supplied to the separation membrane device 4 by the filtration pump 8, and the separation membrane device 4 is filtered by the membrane, and the humic substances and the biopolymer are removed. Filtered water is obtained (S16).
  • the ion exchange means is not particularly limited, but is preferably provided with an anion exchange resin capable of adsorbing and removing humic substances centering on humic acid and fulvic acid.
  • the ion exchange resin is preferably a powder.
  • the average particle size is preferably in the range of 30 ⁇ m to 70 ⁇ m. The average particle diameter is measured by a laser diffraction method or a centrifugal sedimentation method.
  • the powder ion exchange resin is clogged. Therefore, if there is a contaminant, it is preferably removed in advance.
  • the residence time of the water to be treated in the ion exchange means 2 is preferably about 5 to 60 minutes.
  • concentration in the humic substance reduction water after the process by the humic substance reduction means 2 is 0.7 mg / L or less. More preferably, it is 0.6 mg / L or less, More preferably, it is 0.3 mg / L or less.
  • the humic substance concentration in the humic substance-reduced water changes at least one of the addition amount of the powder ion exchange resin and the residence time of the water to be treated in the ion exchange part 2 in the humic substance reducing unit 2 such as by ion exchange. Adjusted by.
  • the flocculant added from the flocculant addition means 3 may be either inorganic or high molecular, but is preferably an inorganic flocculant in terms of low cost and difficulty in clogging the subsequent membrane filtration.
  • the inorganic flocculant is not particularly limited and includes an aluminum flocculant or an iron flocculant, but polyaluminum chloride is preferred.
  • the residence time of the humic-reduced water containing the flocculant in the buffer tank 7 is preferably about 1 to 5 minutes, and it is preferable to use equipment that does not cause a short-circuit flow like the buffer tank 7 of this embodiment.
  • the addition method of the flocculant is not particularly limited, but a method capable of quantitative control injection is preferable. For example, it is preferable to use a natural flow method, an ink jet method, a pumping method, or the like. Moreover, it is preferable to use ph adjusters such as acid and alkali as necessary. Furthermore, the biopolymer concentration is preferably 40 ⁇ g / L or less. In addition, this biopolymer density
  • the biopolymer concentration is adjusted by changing at least one of the retention time of the water to be treated in the humic substance reducing means 2, the residence time of the humic substance reducing water containing the flocculant in the buffer tank 7, and the addition amount of the flocculant. Is done.
  • the biopolymer concentration is measured by a biopolymer measuring device 5 provided after a buffer tank 7 which is an aggregating means.
  • a biopolymer measuring device 5 it is preferable to use LC-OCD (Liquid Chromatography-Organic Carbon Detection).
  • an apparatus that performs the following method can be used instead of the LC-OCD. That is, first, the humic substances in the water to be treated are removed, and the subsequent water is concentrated with an ultrafiltration membrane having an average pore diameter of 50 nm or less, thereby concentrating only the polymer substance, and the soluble total organic carbon concentration of the sample is reduced. By measuring, the concentration of the biopolymer can be measured. In this case, it is preferable to remove humic substances by ion exchange means.
  • the average pore size of the ultrafiltration membrane is preferably 50 nm or less, more preferably 20 nm or less.
  • the concentration rate by an ultrafiltration membrane is 2 times or more, More preferably, it is 5 times or more.
  • the separation membrane device 4 is not particularly limited, and microfiltration, ultrafiltration, nanofiltration membrane, reverse osmosis membrane and the like can be used. Among these, it is preferable to use a microfiltration membrane and an ultrafiltration membrane, and the membrane filtration treatment can be performed stably. Moreover, as a filtration membrane, it is preferable to use a filtration membrane with an average pore diameter of 0.2 ⁇ m or less. More preferably, it is 50 nm or less. The average pore diameter is measured as follows.
  • the filtration membrane is cut in a cross section perpendicular to the length direction. Using a scanning electron microscope, the cross-section is photographed at a magnification that allows the shape of as many pores as possible to be clearly confirmed.
  • overlay the transparent sheet on the copy of the electron microscope image paint the pores black using a black pen, etc., and copy the transparent sheet to a blank sheet. Distinguish clearly from white.
  • the pore diameter of 100 arbitrarily selected pores is obtained using commercially available image analysis software, and the average pore diameter is calculated by calculating the arithmetic average value.
  • image analysis software for example, software “WinRoof” sold by Mitani Corporation can be used.
  • the pore diameter refers to a distance connecting an arbitrary point on the circumference of the pore and a point on the circumference of the pore at a position facing the arbitrary point.
  • the humic substance is a humic substance that is a final product formed by decomposition of a plant or the like by microorganisms, and includes an acidic component such as humic acid.
  • the high-molecular substance indicates a component having a molecular weight of 100,000 or more including a biopolymer, and the biopolymer contains a lot of polysaccharides produced by cells and the like. More specifically, the components observed by the following measurement method can be shown to determine the concentration.
  • xanthan gum (CAS No .: 11138-66-2) was used as a standard substance, and a calibration curve of LC-OCD was prepared to determine the concentration.
  • the humic substance concentration means the carbon component concentration of the humic substance.
  • the standard substance humic acid (CAS No .: 1415-93-6) was used, and a concentration curve was determined by preparing a calibration curve of LC-OCD.
  • Example 1 Operation was performed for the purpose of obtaining clean water from river surface water using the water treatment apparatus 1 shown in FIG.
  • the humic substance reducing means 2 was an ion exchange resin MIEX resin (manufactured by Maezawa Kogyo), and the flocculant adding means 3 was provided with a polyaluminum chloride addition device. Further, a 10 m 3 buffer tank 7 was provided at the subsequent stage.
  • a polyvinylidene fluoride hollow fiber MF membrane As the filtration membrane module of the separation membrane device 4, a polyvinylidene fluoride hollow fiber MF membrane (Asahi Kasei Co., Ltd.), an average pore size of 0.1 ⁇ m, and an effective membrane area of 50 m 2 was used.
  • the outer dimensions of the filtration membrane module are a diameter of 180 mm and a length of 2000 mm (cylindrical).
  • the humic substance concentration and the biopolymer concentration in the treated water were 1.5 mg / L and 70 ⁇ g / L, respectively.
  • FIG. 3 shows the LC-OCD measurement results by the method of Huber et al.
  • a peak detected at a retention time of about 30 minutes indicates a biopolymer
  • a peak detected at 40 to 45 minutes indicates humic substances.
  • the humic substances can be removed only by the ion exchange treatment, but the biopolymer cannot be removed, but the biopolymer can also be removed by the treatment in the order of the ion exchange treatment and the aggregation treatment. On the other hand, the biopolymer cannot be removed only by the aggregation treatment.
  • the operating membrane filtration flux is set to 1.5 m / D, and the membrane filtration flow rate at this time is 75 m 3 / h.
  • the raw water supply pump 6 supplies a treatment to the ion exchange means 2, performs ion exchange treatment and polymer aggregation treatment, and controls the buffer tank 7 not to be emptied.
  • the retention time of the water to be treated in the ion exchange means 2 is set to 20 minutes, and the addition amount of the flocculant is adjusted and added so that the concentration of polyaluminum chloride in the water to be treated is 10 mg / L.
  • the residence time in the buffer tank 7 was 2 minutes or more.
  • the humic substance concentration in the humic substance-reduced water after the ion exchange resin treatment was 0.5 mg / L.
  • the biopolymer concentration in the aggregate-containing water in the buffer tank 7 after the addition of the flocculant was 30 ⁇ g / L.
  • the separation membrane device 4 continued filtration for 29 minutes using the filtration pump 8, and then performed reverse pressure cleaning with filtered water for 1 minute to clean the membrane surface.
  • the transmembrane pressure difference of the separation membrane device 4 after 14 days could be operated at 50 kPa.
  • Example 2 The humic substance reducing means 2 of Example 1 has the same apparatus configuration except that a color cutter adsorbent (manufactured by Nippon Raw Materials Co., Ltd.) is used, and the coagulant adding means 3 is provided with a ferric chloride addition apparatus. .
  • a filtration test was conducted in the same manner as in Example 1 except that seawater was used as the water to be filtered.
  • the residence time of the water to be treated in the humic substance reducing means 2 was set to 20 minutes, and the amount of flocculant added was Adjustment was made so that the concentration of ferric chloride in the treated water was 10 mg / L, and the residence time in the buffer tank 7 was 2 minutes or longer.
  • the humic substance concentration in the humic substance-reduced water after the color cutter treatment was 0.5 mg / L.
  • the biopolymer concentration in the aggregate-containing water in the buffer tank 7 after the addition of the flocculant was 30 ⁇ g / L.
  • the separation membrane device 4 continued filtration for 29 minutes using the filtration pump 8, and then performed reverse pressure cleaning with filtered water for 1 minute to clean the membrane surface.
  • the transmembrane pressure difference of the separation membrane device 4 after 14 days could be operated at 50 kPa.
  • Example 3 The apparatus configuration was the same except that sodium hypochlorite adding means was used for the humic substance reducing means 2 of Example 1 and ferric chloride adding apparatus was provided for the flocculant adding means 3.
  • a filtration test was conducted in the same manner as in Example 2.
  • the amount of sodium hypochlorite added in the humic substance reducing means 2 was set to 5 mg / l, and the amount of flocculant added was the ferric chloride in the water to be treated.
  • the concentration was adjusted to 10 mg / L and added, and the residence time in the buffer tank 7 was 2 minutes or longer.
  • the humic substance concentration in the humic substance-reduced water after the color cutter treatment was 0.5 mg / L.
  • the biopolymer concentration in the aggregate-containing water in the buffer tank 7 after the addition of the flocculant was 30 ⁇ g / L.
  • the separation membrane device 4 continued filtration for 29 minutes using the filtration pump 8, and then performed reverse pressure cleaning with filtered water for 1 minute to clean the membrane surface.
  • the transmembrane pressure difference of the separation membrane device 4 after 14 days could be operated at 50 kPa.
  • Example 2 Using the same water treatment apparatus 1 and conditions as in Example 1, the ion exchange resin was removed, and the flocculant was added under the same conditions as in Example 1. By these operations, the humic substance concentration and the biopolymer concentration in the water of the buffer tank 7 were 1.2 mg / L, respectively. It was 65 ⁇ g / L. The transmembrane pressure difference after 14 days of operation exceeded 100 kPa.
  • Example 3 Using the same water treatment apparatus 1 and conditions as in Example 1, the ion exchange resin was removed, and the addition of the flocculant was also stopped. By these operations, the humic substance concentration and the biopolymer concentration in the water of the buffer tank 7 were 1.5 mg / L, respectively. It was 70 ⁇ g / L. The transmembrane pressure difference after 14 days of operation exceeded 150 kPa.
  • Example 4 Using the same water treatment apparatus 1 and conditions as in Example 1, the position of the flocculant addition means 3 was installed in front of the ion exchange means 2. The ion exchange treatment and the amount of flocculant added were the same as in Example 1. By these operations, the humic substance concentration and the biopolymer concentration in the water of the buffer tank 7 were 0.5 mg / L, respectively. It was 60 ⁇ g / L. The transmembrane pressure difference after 14 days of operation was 90 kPa.
  • the subsequent membrane filtration could be stably operated by performing the ion exchange treatment and the aggregation treatment in this order.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
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  • Separation Using Semi-Permeable Membranes (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)
  • Treatment Of Water By Ion Exchange (AREA)

Abstract

L'invention concerne un procédé de traitement de l'eau et un dispositif associé tels, que l'eau à traiter, ladite eau contenant des substances humiques et des biopolymères, peut être filtrée de manière stable par passage par une membrane sans provoquer le colmatage de la membrane de filtration. Le procédé de traitement de l'eau destiné à clarifier l'eau à traiter, qui contient des substances humiques et des substances de poids moléculaire élevé, comprend : une étape d'élimination des substances humiques qui soumet l'eau à traiter à un traitement d'élimination des substances humiques pour obtenir une eau à teneur réduite en substances humiques ; une étape d'agrégation des substances de poids moléculaire élevé pour agréger les substances de poids moléculaire élevé dans l'eau à teneur réduite en substances humiques par un traitement faisant appel à un agent d'agrégation pour obtenir une eau contenant des agrégats ; et une étape de filtration sur membrane pour filtrer l'eau contenant des agrégats par passage par une membrane.
PCT/JP2017/043524 2016-12-05 2017-12-04 Procédé de traitement de l'eau et dispositif associé Ceased WO2018105569A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110951492A (zh) * 2019-11-19 2020-04-03 西北农林科技大学 一种基于改性泥煤的土壤修复药剂胡敏素的制备方法及其应用
CN114641342A (zh) * 2019-10-25 2022-06-17 株式会社钟化 聚合物水分散液的制造方法

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WO2009020157A1 (fr) * 2007-08-07 2009-02-12 Kurita Water Industries Ltd. Procédé de séparation par membrane et dispositif de séparation par membrane
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WO2016185788A1 (fr) * 2015-05-19 2016-11-24 栗田工業株式会社 Coagulant et procédé de traitement de l'eau

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10504995A (ja) * 1994-09-09 1998-05-19 サウス オーストラリアン ウォーター コーポレイション 水処理法
WO2009020157A1 (fr) * 2007-08-07 2009-02-12 Kurita Water Industries Ltd. Procédé de séparation par membrane et dispositif de séparation par membrane
JP2016040030A (ja) * 2014-08-12 2016-03-24 株式会社クラレ 水処理システム
WO2016185788A1 (fr) * 2015-05-19 2016-11-24 栗田工業株式会社 Coagulant et procédé de traitement de l'eau

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Title
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CN110951492A (zh) * 2019-11-19 2020-04-03 西北农林科技大学 一种基于改性泥煤的土壤修复药剂胡敏素的制备方法及其应用

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