[go: up one dir, main page]

WO2020094463A1 - Élimination d'ions métalliques d'une eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane - Google Patents

Élimination d'ions métalliques d'une eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane Download PDF

Info

Publication number
WO2020094463A1
WO2020094463A1 PCT/EP2019/079507 EP2019079507W WO2020094463A1 WO 2020094463 A1 WO2020094463 A1 WO 2020094463A1 EP 2019079507 W EP2019079507 W EP 2019079507W WO 2020094463 A1 WO2020094463 A1 WO 2020094463A1
Authority
WO
WIPO (PCT)
Prior art keywords
process according
membrane
metal ions
water
polymer membrane
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/EP2019/079507
Other languages
English (en)
Inventor
Martin Heijnen
Christian STAAKS
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.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of WO2020094463A1 publication Critical patent/WO2020094463A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • 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
    • B01D61/58—Multistep processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2623—Ion-Exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/02—Elements in series
    • B01D2317/025—Permeate series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/08—Use of membrane modules of different kinds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/04—Backflushing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/12—Use of permeate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/16—Use of chemical agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/42—Ion-exchange membranes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/14—Maintenance of water treatment installations
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/20—Prevention of biofouling

Definitions

  • the invention relates to a process for cleaning a polymer membrane comprising the steps of (A) filtering an aqueous liquid through the polymer membrane to yield a filtrate; (B) reducing the concentration of metal ions in the filtrate by nanofiltration or ion exchange to yield a purified filtrate; (C) backwashing the polymer membrane with a chemical washing solution made from the purified filtrate; and (D) continuing the filtering of the aqueous liquid through the polymer membrane.
  • A filtering an aqueous liquid through the polymer membrane to yield a filtrate
  • B reducing the concentration of metal ions in the filtrate by nanofiltration or ion exchange to yield a purified filtrate
  • C backwashing the polymer membrane with a chemical washing solution made from the purified filtrate
  • D continuing the filtering of the aqueous liquid through the polymer membrane.
  • Membrane fouling is a very complex process, which is not yet fully understood. Most of the deposits consist of material not belonging to one single chemical“class” but, depending on the feed water conditions such as temperature, time of the year or intensity of rainfall, showing strong variations of its composition. For example, such fouling deposit may contain major components of:
  • Object of the present invention was to identify a process for cleaning a polymer membrane which can restore a high permeability of the membrane, which avoids the development of new cleaning agents and works with the established cleaning agents, which is environmentally friendly or cost efficient, or which works on the available filtration systems.
  • the object was solved by a process for cleaning a polymer membrane comprising the steps of
  • Typical filtration processes are operated at a constant flux rate.
  • the membrane resistance may increase and result in an increased transmembrane pressure (TMP).
  • TMP transmembrane pressure
  • the fouling of the polymer membrane results in a reduced permeability.
  • the permeability may be calculated by flux rate (given e.g. in the unit liter / (m 2 x h)) divided by transmembrane pressure (given e.g. in the unit bar).
  • the cleaning of a polymer membrane typically means that foulants are removed from the polymer membrane.
  • the cleaning of a polymer membrane should inrease its permability.
  • the process for cleaning according to the invention is often initiated when the permeability of the polymer membrane is below 50%, preferably below 35%, and in particular below 20% of the initial permeability of the clean membrane.
  • the process for cleaning may be initiated after a preset duration of time (e.g. in the range from 4 times per day to once per months), which usually depends on the membrane type and process conditions.
  • the steps (A) to (D) are usually made in the alphabetic order.
  • step (A) an aqueous liquid is filtered through the polymer membrane.
  • the filtration may yield the filtrated, and it may be made by conventional filtration processes and parameters, which are known to experts.
  • the aqueous liquid is forced through the membrane from the feed side to the filtrate side.
  • the liquid may contain at least 80 wt%, preferably at least 90 wt%, and in particular at least 95 wt% water.
  • the liquid is industrial waste water, sea water, salt water, surface water, ground water, process water, drinking water, liquid food (e.g. a beverage, such as beer, wine, juices, dairy products, or soft drinks).
  • liquid food e.g. a beverage, such as beer, wine, juices, dairy products, or soft drinks.
  • the liquid is sea water.
  • the liquid is ground water or surface water.
  • the liquid is industrial waste water or process water.
  • the liquid is a beverage, such as beer.
  • the liquid may comprise up to 1000 ppm, preferably up to 100 ppm and in particular up to 20 ppm of metal ions, such as of the multivalent cations of iron and manganese.
  • the filtrate may comprise 0.01 to 100 ppm, preferably up to 0.1 ppm to 10 ppm of metal ions, such as of the multivalent cations of iron and/or manganese.
  • the liquid is salt water which may comprise at least one salt selected from the group consisting of an alkaline metal salt, an alkaline earth metal salt and mixtures thereof.
  • the salt water is process water, ground water, river water, brackish water, or sea water, wherein sea water is preferred. Suitable process water is cooling water in industrial plants or in power plants.
  • the salt water usually comprises the salt in a range from 0.001 to 10 % by weight, preferably from 0.005 to 7.5% by weight, particularly preferably from 0.01 to 5% by weight, and in particular from 0.02 to 4% by weight.
  • the salt water may comprise up to 2000 ppm, preferably up to 1000 ppm and in particular up to 400 ppm of calcium.
  • the salt water may comprise up to 3000 ppm, preferably up to 2000 ppm and in particular up to 1200 ppm of magnesium.
  • Suitable alkaline metal salts are for example sodium sulfate (Na 2 S0 4 ), sodium chloride (NaCI), sodium bromide (NaBr), sodium iodide (Nal), sodium carbonate (Na2COs), potassium chloride (KCI), potassium bromide (KBr) and potassium iodide (Kl).
  • Suitable alkaline earth metal salts are for example calcium fluoride (CaF2), calcium sulfate (CaS0 4 ), calcium carbonate (CaCC ⁇ ), magnesium fluoride (MgF 2 ), magnesium chloride (MgCh), magnesium bromide (MgBr2), magnesium iodide (Mgl 2 ), magnesium sulfate (MgS0 4 ), magnesium carbonate (MgCOs) and magnesium hydroxide (Mg(OH) 2 ).
  • alkaline metal salts and alkaline earth metal salts generally dissociate in water.
  • sodium chloride (NaCI) dissociates in water to give a sodium cation (Na + ) and a chloride anion (Cl ⁇ ), sodium
  • Na2CC>3 dissociates in an aqueous medium to form two sodium cations (Na + ) and a carbonate anion (CO3 2 -) and calcium carbonate (CaCOs) dissociates to give a calcium cation (Ca 2+ ) and a carbonate anion (CO3 2 ).
  • a carbonate anion can also form
  • alkaline metal salts and alkaline earth metal salts in water are usually present in their ionic form.
  • Step (B) is reducing the concentration of metal ions in the filtrate by nanofiltration or ion exchange to yield a purified filtrate.
  • the metal ions preferably multivalent metal cations, such as multivalent cations of iron, manganese, copper, cobalt, titanium, chromium, vanadium, nickel, molybdenum, palladium, platinum, zinc, cadmium, mercury.
  • multivalent metal cations such as multivalent cations of iron, manganese, copper, cobalt, titanium, chromium, vanadium, nickel, molybdenum, palladium, platinum, zinc, cadmium, mercury.
  • Specific examples are Fe 2+ , Mn 2+ , Cu 2+ , or Co 2+ .
  • the metal ions are multivalent cations of iron and manganese.
  • the concentration of the metal ions in the backwash may be reduced by at least 50 mol%, preferably at least 75 mol%, and in particular at least 95%. In another form the concentration of the metal ions in the backwash may be reduced by at least 50, 60, 70, 80, 90, 97, 98, 99, 99.5, or 99.9 mol%.
  • the filtrate may comprise up to 1000 ppm, preferably up to 100 ppm and in particular up to 20 ppm of metal ions, such as of the multivalent cations of iron and manganese.
  • the filtrate may comprise 0.01 to 100 ppm, preferably up to 0.1 ppm to 10 ppm of metal ions, such as of the multivalent cations of iron and manganese.
  • the purified filtrate may comprise less than 100 ppm, preferably less 10 ppm, and in particular less than 1 ppm of the sum of all metal ions, preferably multivalent metal cations, such as multivalent cations of iron and manganese.
  • the purified filtrate may comprise less than 0.5 ppm, preferably less 0.2 ppm, and in particular less than 0.1 ppm of the sum of all metal ions, preferably multivalent metal cations, such as multivalent cations of iron and manganese.
  • the purified filtrate usually comprises at least 99 wt%, preferably at least 99.5 wt%, and in particular at least 99.9 wt% of water.
  • the nanofiltration (NF) is usually achieved with a nanofiltration membrane, which may have a molecular weight cutoff (MWCO) below 2000 g/mol, preferably below 1000 g/mol, and in particular below 500 g/mol.
  • MWCO molecular weight cutoff
  • the nanofiltration (NF) is usually achieved with a nanofiltration membrane, which may have a molecular weight cutoff (MWCO) below 5000,
  • nanofiltration membrane may have a pore size between 1 and 10 nm, such as up to 8, 6, 4, or 3 nm.
  • NF membranes may comprise as the main component at least one polyamide (PA), polyvinylalcohol (PVA), Cellulose Acetate (CA), Cellulose Triacetate (CTA), CA-triacetate blend, Cellulose ester, Cellulose Nitrate, regenerated Cellulose, aromatic , aromatic/aliphatic or aliphatic polyamide, aromatic, aromatic/aliphatic or aliphatic polyimide, polybenzimidazole (PBI), polybenzimidazolone (PBIL), Polyacrylonitrile (PAN), PAN-poly(vinyl chloride) copolymer (PAN-PVC), PAN-methallyl sulfo- nate copolymer, polyetherimide (PEI), Polyetheretherketone (PEEK), sulfonated polyether- etherketone (SPEEK), Poly(dimethylphenylene oxide) (PPO), Polycarbonate, Polyester, Polytetrafl
  • PA polyamide
  • PVA polyvinyl
  • NF membranes comprise as the main component at least one polysulfone, polyphenylenesulfone and/or polyethersulfone.
  • the main components of a NF membrane are positively or negatively charged.
  • NF membranes comprise as the main component polyamides, poly-imides or polyimide urethanes, Polyether- etherketone (PEEK) or sulfonated polyetheretherketone (SPEEK).
  • the nanofiltration membranes are made of polyamide, e.g. polyamide composite membranes, which may be based on polystyrene.
  • Nanofiltration apparatuses are know and commercially available. Nanofiltration membranes are normally used in crossflow filtration processes.
  • the ion exchange is usually achieved with a ion exchange resin made of polymer matrix which contains functional groups.
  • the matrix often consists of polystyrene or of acrylic polymers, both cross-linked e.g. by means of divinylbenzene (DVB).
  • the functional groups may be acidic (e.g. -SO 3 H, -COOH) or basic (e.g. -N(CH 3 ) 3 0H), where acidic functional groups are preferred.
  • the ion exchange is preferably achieved with a cationic exchange resin, which usually has strong (e.g. sulfonic groups) or weak acidic (e.g. carboxylic acid groups) functional groups.
  • a cationic exchange resin which usually has strong (e.g. sulfonic groups) or weak acidic (e.g. carboxylic acid groups) functional groups.
  • the ion exchange may be made with any known apparatuses, e.g. ion exchange columns.
  • Step (C) is the backwashing the polymer membrane with a chemical washing solution made from the purified filtrate.
  • backwash or backwashing are also termed BW in the following.
  • Polymer membranes are often backwashed with water (a“normal" backwash).
  • the water for a normal BW may be permeate, fresh water, feed water or any other clean water source.
  • a first rinsing (e.g. by opening the retentate path during the active feed flow) step is performed for a short period of time (e.g. 10 to 60 seconds);
  • the flow rate of permeate during the back wash is much higher as the filtration rate.
  • the feedflow in filtration typically more than 80 l/m 2* h (higher flow rate is advantageous, but the mechanical membrane stability and the system costs have to be considered);
  • the amount of back wash per m 2 is preferably at least 1 I/m 2 per BW.
  • the optimum typically depends on the feed water/wastewater quality, and is a compromise between the optimal membrane regeneration and the highest possible permeate yield.
  • T o complete the back wash, higher pressure in permeate than in the feed should to be established in order to induce a high flow rate in reverse direction.
  • the feed inlet is closed and the retentate outlet is opened; a permeate buffer tank is advantageous.
  • step (C) is the backwashing the polymer membrane is made with a chemical washing solution (also called a chemical enhanced backwash CEB).
  • a chemical washing solution also called a chemical enhanced backwash CEB.
  • the chemical washing solution comprises a cleaning chemical selected from an acid, a base, and/or an oxidant.
  • the chemical washing solution comprising an cleaning chemical selected from alkaline hydroxide, alkaline earth hydroxide, mineral acid, H2O2, ozone, peracid, CIO2, KMn0 4 , chlorate perchlorate or hypochlorite.
  • the cleaning chemical is hypochlorite.
  • the concentration of the cleaning chemical into chemical washing solution is known to an expert, and can be adapted to the polymer membranes or cleaning purpose.
  • the chemical washing solution may comprise up to 40 wt%, preferably up to 20 wt%, and in particular up to 10 wt% of the cleaning chemical.
  • cleaning liquid ranges between 0.5 and 2.5.
  • Base solution mostly NaOH as the cheapest base, typically in a concentration of 0.03 N or higher, so that the pH of cleaning solution ranges between 10.5 and 12.5.
  • Oxidizing agents such as NaOCI, typically in a concentration between 3 and 50 ppm in alkaline solution.
  • Other oxidizing chemicals such as H2O2 can also be used.
  • the chemical washing solution is made from the purified filtrate.
  • the chemical washing solution is made by mixing the purified filtrate and cleaning chemical.
  • the chemical washing solution may contain at least 50 wt%, preferably at least 80 wt%, and in particular at least 90 wt% of the purified filtrate.
  • a separate chemical back wash system is usually applied, especially to avoid permeate contamination and/or to allow separate cleaning of different membrane sections. It may contain:
  • Dosing equipment of concentrated chemicals to the back wash permeate such as dosing pumps, flow meters, pressure transmitters
  • Mixing device like for instance Venturi injector, pump injector or static mixer
  • a CEB sequence for optimal membrane regeneration may be as follows: a) Rinsing of the modules using feed by opened retentate path (10-30 seconds);
  • step d may be combined with aforesaid step b);
  • step c by a pH or redox sensor (alternatively to be combined with step c);
  • washing with a chemical washing solution comprising an acid, typically sulphuric acid, e.g. by filling H2SO4 solution into the module and steeping it for about 30-60 minutes;
  • CEB is advantageously started, when the TMP increases above a certain value, or after a predefined operation time, for instance every 8 hrs.
  • step (D) the filtering of the aqueous liquid through the polymer membrane is continued.
  • the aqueous liquid may be the same as used in step (A) or it may be a different aqueous liquid.
  • the filtering may be continued immediately after the end of step (C), or the polymer membrane may be stored for any desired time until filtration of the step (D) is continued.
  • the polymer membrane may be understood to be a thin, semipermeable structure capable of separating two fluids or separating molecular and/or ionic components or particles from a liquid.
  • the membrane acts usually as a selective barrier, allowing some particles, substances or chemicals to pass through, while retaining others.
  • the polymer membranes can be ultrafiltration (UF) membranes or microfiltration (MF) membranes. These membrane types are generally known in the art and are further described below.
  • UF ultrafiltration
  • MF microfiltration
  • UF membranes are normally suitable for removing suspended solid particles and solutes of high molecular weight, for example above 10000 Da.
  • UF membranes are normally suitable for removing bacteria and viruses.
  • UF membranes normally have an average pore diameter of 2 nm to 50 nm, preferably 5 to 40 nm, more preferably 5 to 20 nm.
  • UF membranes comprise as the main component at least one polyamide (PA), polyvinylalcohol (PVA), Cellulose Acetate (CA), Cellulose Triacetate (CTA), CA-triacetate blend, Cellulose ester, Cellulose Nitrate, regenerated Cellulose, aromatic , aromatic/aliphatic or aliphatic Polyamide, aromatic, aromatic/aliphatic or aliphatic Polyimide, Polybenzimidazole (PBI), Polybenzimidazolone (PBIL), Polyacrylonitrile (PAN), PAN-poly(vinyl chloride) copolymer (PAN-PVC), PAN-methallyl sulfonate copolymer, polyetherimide (PEI), Polyetheretherketone (PEEK), sulfonated polyetheretherketone (SPEEK), Poly(dimethylphenylene oxide) (PPO), Polycarbonate, Polyester, Polytetrafluroethylene PTFE, Poly(vinylidene fluor
  • Polydimethylsiloxane aromatic, aromatic/aliphatic or aliphatic polyimide urethanes, aromatic, aromatic/aliphatic or aliphatic polyamidimides, crosslinked polyimides or polyarylene ether, polysulfone, polyphenylenesulfone, or polyethersulfone, or mixtures thereof.
  • UF membranes comprise as the main component at least one polysulfone, polyphenylenesulfone and/or polyethersulfone.“Polysulfones”,“polyethersulfones” and“polyphenylenesulfones” shall include the respective polymers that comprise sulfonic acid and/or salts of sulfonic acid at some of the aromatic moieties.
  • UF mem- branes comprise as the main component or as an additive at least one partly sulfonated polysulfone, partly sulfonated polyphenylenesulfone and/or partly sulfonated polyethersulfone.
  • UF membranes comprise as the main component or as an additive at least one partly sulfonated polyphenylenesulfone.“Arylene ethers”,“Polysulfones”,“polyether- sulfones” and“polyphenylenesulfones” shall include block polymers that comprise blocks of the respective arylene ethers, Polysulfones, polyethersulfones or polyphenylenesulfones as well as other polymer blocks. In one embodiment, UF membranes comprise further additives like polyvinyl pyrrolidones.
  • UF membranes are present as spiral wound membranes, as pillows or flat sheet membranes. In another embodiment of the invention, UF membranes are present as tubular membranes. In another embodiment of the invention, UF membranes are present as hollow fiber membranes or capillaries. In yet another embodiment of the invention,
  • UF membranes are present as single bore hollow fiber membranes. In yet another embodiment of the invention, UF membranes are present as multibore hollow fiber membranes.
  • Multiple channel membranes also referred to as multibore membranes, comprise more than one longitudinal channels also referred to simply as“channels”.
  • the number of channels is typically 2 to 19.
  • multiple channel membranes comprise two or three channels.
  • multiple channel membranes comprise 5 to 9 channels.
  • multiple channel membranes comprise seven channels.
  • the number of channels is 20 to 100.
  • the shape of such channels also referred to as“bores”, may vary.
  • such channels have an essentially circular diameter.
  • such channels have an essentially ellipsoid diameter.
  • channels have an essentially rectangular diameter.
  • such channels may deviate from the idealized circular, ellipsoid or rectangular form.
  • such channels have a diameter (for essentially circular diameters), smaller diameter (for essentially ellipsoid diameters) or smaller feed size (for essentially rectangular diameters) of 0.05 mm to 3 mm, preferably 0.5 to 2 mm, more preferably 0.9 to 1.5 mm.
  • such channels have a diameter (for essentially circular diameters), smaller diameter (for essentially ellipsoid diameters) or smaller feed size (for essentially rectangular diameters) in the range from 0.2 to 0.9 mm.
  • these channels can be arranged in a row.
  • these channels are in a preferred embodiment arranged such that a central channel is surrounded by the other channels.
  • a central channel is surrounded by the other channels.
  • a central channel is surrounded by the other channels.
  • a central channel is surrounded by the other channels.
  • a central channel is surrounded by the other channels.
  • a central channel is
  • membrane comprises one central channel and for example four, six or 18 further channels arranged cyclically around the central channel.
  • the wall thickness in such multiple channel membranes is normally from 0.02 to 1 mm at the thinnest position, preferably 30 to 500 pm, more preferably 100 to 300 pm.
  • the membranes and carrier membranes have an essentially circular, ellipsoid or rectangular diameter.
  • membranes are essentially circular.
  • membranes according to the invention have a diameter (for essentially circular diameters), smaller diameter (for essentially ellipsoid diameters) or smaller feed size (for essentially rectangular diameters) of 2 to 10 mm, preferably 3 to 8 mm, more preferably 4 to 6 mm.
  • membranes have a diameter (for essentially circular diameters), smaller diameter (for essentially ellipsoid diameters) or smaller feed size (for essentially rectangular diameters) of 2 to 4 mm.
  • the rejection layer is located on the inside of each channel of said multiple channel membrane.
  • the channels of a multibore membrane may incorporate an active layer with a pore size different to that of the carrier membrane or a coated layer forming the active layer. Suitable materials for the coated layer are polyoxazoline, polyethylene glycol, polystyrene, hydrogels, polyamide, zwitterionic block copolymers, such as sulfobetaine or carboxybetaine.
  • the active layer can have a thickness in the range from 10 to 500 nm, preferably from 50 to 300 nm, more preferably from 70 to 200 nm.
  • multibore membranes are designed with pore sizes between 0.2 and 0.01 pm.
  • the inner diameter of the capillaries can lie between 0.1 and 8 mm, preferably between 0.5 and 4 mm and particularly preferably between 0.9 and 1.5 mm.
  • the outer diameter of the multibore membrane can for example lie between 1 and 26 mm, preferred 2.3 and 14 mm and particularly preferred between 3.6 and 6 mm.
  • the multibore membrane can contain 2 to 94, preferably 3 to 19 and particularly preferred between 3 and 14 channels. Often multibore membranes contain seven channels.
  • the permeability range can for example lie between 100 and 10000 L/m 2 hbar, preferably between 300 and 2000 L/m 2 hbar.
  • MF membranes are normally suitable for removing particles with a particle size of 0.1 pm and above.
  • MF membranes normally have an average pore diameter of 0.05 pm to 10 pm, preferably 1.0 pm to 5 pm.
  • Microfiltration can use a pressurized system but it does not need to include pressure.
  • MF membranes can be capillaries, hollow fibers, flat sheet, tubular, spiral wound, pillows, hollow fine fiber or track etched. They are porous and allow water, monovalent species (Na+, CI-), dissolved organic matter, small colloids and viruses through but retain particles, sediment, algae or large bacteria.
  • M Microfiltration systems are designed to remove suspended solids down to 0.1 micrometers in size, in a feed solution with up to 2-3% in concentration.
  • MF membranes comprise as the main component at least polyamide (PA), polyvinylalcohol (PVA), Cellulose Acetate (CA), Cellulose Triacetate (CTA), CA-triacetate blend, Cellulose ester, Cellulose Nitrate, regenerated Cellulose, aromatic, aromatic/aliphatic or aliphatic Polyamide, aromatic, aromatic/aliphatic or aliphatic Polyimide, Polybenzimidazole (PBI), Polybenzimidazolone (PBIL), Polyacrylonitrile (PAN), PAN-poly(vinyl chloride) copolymer (PAN-PVC), PAN-methallyl sulfonate copolymer, polyetherimide (PEI), Polyetheretherketone (PEEK), sulfonated polyetheretherketone (SPEEK), Poly(dimethyl- phenylene oxide) (PPO), Polycarbonate, Polyester, Polytetrafluroethylene PTFE, Poly(vinyl- idenol-
  • MF membranes comprise as the main component or as an additive at least one polysulfone, polyphenylenesulfone and/or polyether- sulfone. In one embodiment, MF membranes comprise as the main component or as an additive at least one partly sulfonated polysulfone, partly sulfonated polyphenylenesulfone and/or partly sulfonated polyethersulfone. In one embodiment, UF membranes comprise as the main component or as an additive at least one partly sulfonated polyphenylenesulfone.
  • the polymer membranes may be based on at least one polymer selected from polyamide (PA), polyvinylalcohol (PVA), Cellulose Acetate (CA), Cellulose Triacetate (CTA), CA-triacetate blend, Cellulose ester, Cellulose Nitrate, regenerated Cellulose, aromatic, aromatic/aliphatic or aliphatic Polyamide, aromatic, aromatic/aliphatic or aliphatic Polyimide, Polybenzimidazole (PBI), Polybenzimidazolone (PBIL), Polyacrylonitrile (PAN), PAN-poly(vinyl chloride) copolymer (PAN-PVC), PAN-methallyl sulfonate copolymer, polyetherimide (PEI), Polyetheretherketone (PEEK), sulfonated polyetheretherketone (SPEEK), Poly(dimethylphenylene oxide) (PPO), Polycarbonate, Polyester, Polytetrafluroethylene (PTFE), Poly(vinylidene flu
  • polymer is selected from poly(vinylidene fluoride) (PVDF), polyarylene ether, polysulfone (PSU), polyphenylenesulfone (PPSU) or polyethersulfone (PESU).
  • PVDF poly(vinylidene fluoride)
  • PSU polysulfone
  • PPSU polyphenylenesulfone
  • PESU polyethersulfone
  • polymer is polyethersulfone.
  • the polymer membrane is based on polyvinyl pyrolidone, polyvinyl acetates, polyurethanes, cellulose acetates, polyacrylonitriles, polyamides, polyolefines, polyesters, polysulfones, polyethersulfones, polycarbonates, polyether ketones, sulfonated polyether ketones, polyamide sulfones, polyvinylidene fluorides, polyvinylchlorides, polystyrenes and polytetrafluorethylenes, copolymers thereof, and mixtures thereof, which polymer or mixture thereof preferably makes up 80 percent or more of the membrane weight.
  • the polymer membrane is based on polysulfones, polyethersulfones, copolymers thereof, and mixtures thereof, which polymer or mixture thereof preferably makes up 80 percent or more of the membrane weight.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Nanotechnology (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'élimination d'ions métalliques à partir d'eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane. L'invention concerne un procédé de nettoyage d'une membrane polymère comprenant les étapes consistant à (A) le filtrage d'un liquide aqueux à travers la membrane polymère pour produire un filtrat; (B) la réduction de la concentration d'ions métalliques dans le filtrat par nanofiltration ou échange d'ions pour produire un filtrat purifié; (C) le lavage à contre-courant de la membrane polymère avec une solution de lavage chimique réalisée à partir du filtrat purifié; et (D) la poursuite du filtrage du liquide aqueux à travers la membrane polymère.
PCT/EP2019/079507 2018-11-06 2019-10-29 Élimination d'ions métalliques d'une eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane Ceased WO2020094463A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP18204526.0 2018-11-06
EP18204526 2018-11-06

Publications (1)

Publication Number Publication Date
WO2020094463A1 true WO2020094463A1 (fr) 2020-05-14

Family

ID=64267477

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2019/079507 Ceased WO2020094463A1 (fr) 2018-11-06 2019-10-29 Élimination d'ions métalliques d'une eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane

Country Status (1)

Country Link
WO (1) WO2020094463A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114470959A (zh) * 2022-03-18 2022-05-13 内蒙古科泰隆达环保科技有限公司 一种采用膜技术的浓缩分离系统
WO2024145515A1 (fr) 2022-12-29 2024-07-04 Dupont Safety & Construction, Inc. Pré-filtre intégré pour système de membrane uf/mf

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH119972A (ja) * 1997-06-20 1999-01-19 Japan Organo Co Ltd 膜濾過装置及び膜濾過方法
WO2018200434A1 (fr) * 2017-04-26 2018-11-01 Bl Technologies, Inc. Système à uf/oi intégré, à haute récupération

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH119972A (ja) * 1997-06-20 1999-01-19 Japan Organo Co Ltd 膜濾過装置及び膜濾過方法
WO2018200434A1 (fr) * 2017-04-26 2018-11-01 Bl Technologies, Inc. Système à uf/oi intégré, à haute récupération

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
LI S ET AL: "Impact of backwash water composition on ultrafiltration fouling control", JOURNAL OF MEMBRANE SCIENCE, ELSEVIER BV, NL, vol. 344, no. 1-2, 15 November 2009 (2009-11-15), pages 17 - 25, XP026601973, ISSN: 0376-7388, [retrieved on 20090722], DOI: 10.1016/J.MEMSCI.2009.07.025 *
OLGA FERRER ET AL: "REVERSIBILITY OF FOULING ON ULTRAFILTRATION MEMBRANE BY BACKWASHING AND CHEMICAL CLEANING: DIFFERENCES IN ORGANIC FRACTIONS BEHAVIOUR", 15 March 2016 (2016-03-15), pages 1 - 26, XP055647781, Retrieved from the Internet <URL:https://www.tandfonline.com/doi/abs/10.1080/19443994.2015.1022807?journalCode=tdwt20> [retrieved on 20191129] *
S. G. J. HEIJMAN ET AL: "An innovative treatment concept for future drinking water production: fluidized ion exchange - ultrafiltration - nanofiltration - granular activated carbon filtration", DRINKING WATER ENGINEERING AND SCIENCE, vol. 2, no. 2, 26 August 2009 (2009-08-26), pages 41 - 47, XP055647765, DOI: 10.5194/dwes-2-41-2009 *
SHENG LI ET AL: "Practical experience of backwashing with SWRO permeate for UF fouling control", DESALINATION AND WATER TREATMENT : SCIENCE AND ENGINEERING ; DWT, vol. 51, no. 1-3, 13 January 2013 (2013-01-13), UK, pages 432 - 436, XP055647907, ISSN: 1944-3994, DOI: 10.1080/19443994.2012.704708 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114470959A (zh) * 2022-03-18 2022-05-13 内蒙古科泰隆达环保科技有限公司 一种采用膜技术的浓缩分离系统
WO2024145515A1 (fr) 2022-12-29 2024-07-04 Dupont Safety & Construction, Inc. Pré-filtre intégré pour système de membrane uf/mf

Similar Documents

Publication Publication Date Title
Singh Hybrid membrane systems for water purification: technology, systems design and operations
US5997745A (en) Method for producing high purity water using triple pass reverse osmosis (TPRO)
US6120689A (en) High purity water using triple pass reverse osmosis (TPRO)
US20140048483A1 (en) Method for cleaning membrane module
WO1995017241A1 (fr) Systeme de nettoyage in situ pour membranes encrassees
JP2018065114A (ja) 濃縮方法および濃縮装置
US20160051937A1 (en) Method for cleaning hollow fiber membrane module
JP2016128142A (ja) 半透膜の阻止率向上方法
Nataraj et al. Cellulose acetate-coated α-alumina ceramic composite tubular membranes for wastewater treatment
Freger et al. Boron removal using membranes
Chen et al. Membrane separation: basics and applications
WO2012098969A1 (fr) Procédé de nettoyage d&#39;un module à membrane, procédé de génération d&#39;eau douce, et générateur d&#39;eau douce
JP4923428B2 (ja) 膜分離方法および膜分離装置
Zazouli et al. Retention of humic acid from water by nanofiltration membrane and influence of solution chemistry on membrane performance
WO2020094463A1 (fr) Élimination d&#39;ions métalliques d&#39;une eau de lavage à contre-courant améliorée chimique pour le nettoyage de membrane
JP5346784B2 (ja) 分離膜の製造方法、分離膜およびイオン排除性能を有する分離膜モジュール
JP6648695B2 (ja) 半透膜分離装置の運転方法
Oh et al. Effect of ozone on microfiltration as a pretreatment of seawater reverse osmosis
JP4923427B2 (ja) 膜分離方法および膜分離装置
KR101197022B1 (ko) 역세척이 가능한 역삼투 수처리 설비
US20180264410A1 (en) Method for improving inhibition performance of semipermeable membrane, semipermeable membrane, and semipermeable membrane water production device
US20170296974A1 (en) Method of cleaning microfiltration and ultrafiltration membranes
JP2020099870A (ja) 水処理システム及びその運転方法
WO2019025242A1 (fr) Processus de nettoyage d&#39;une membrane comprenant le séchage de la membrane
EP3056258B1 (fr) Procédé de nettoyage chimique pour systèmes de membrane

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19790566

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 19790566

Country of ref document: EP

Kind code of ref document: A1