WO2006022719A1 - Procédé et appareil de déminéralisation parallèle - Google Patents

Procédé et appareil de déminéralisation parallèle Download PDF

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Publication number
WO2006022719A1
WO2006022719A1 PCT/US2004/026693 US2004026693W WO2006022719A1 WO 2006022719 A1 WO2006022719 A1 WO 2006022719A1 US 2004026693 W US2004026693 W US 2004026693W WO 2006022719 A1 WO2006022719 A1 WO 2006022719A1
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WO
WIPO (PCT)
Prior art keywords
concentrate
membrane
water
permeate
storage tank
Prior art date
Application number
PCT/US2004/026693
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English (en)
Inventor
Anthony Pipes
Original Assignee
Anthony Pipes
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 Anthony Pipes filed Critical Anthony Pipes
Priority to EP04781398A priority Critical patent/EP1838421A4/fr
Priority to PCT/US2004/026693 priority patent/WO2006022719A1/fr
Publication of WO2006022719A1 publication Critical patent/WO2006022719A1/fr

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Classifications

    • 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
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • 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
    • B01D61/04—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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/08—Apparatus therefor
    • B01D61/081—Apparatus therefor used at home, e.g. kitchen
    • 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
    • B01D61/12—Controlling or regulating
    • 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
    • B01D61/147—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
    • B01D61/22—Controlling or regulating
    • 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
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0036—Crystallisation on to a bed of product crystals; Seeding
    • 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
    • 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
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • 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
    • B01D2311/18—Details relating to membrane separation process operations and control pH control
    • 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
    • B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
    • 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
    • B01D2321/168—Use of other chemical agents
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents

Definitions

  • TDS total dissolved solids
  • Water salinity poses a problem that may in the future be resolved through regulation and public oversight.
  • the problem created by the conflicting use of ion exchange for the treatment of hard water supplies can also be addressed through technological innovation.
  • Parallel desalting is proposed as a means to service residential soft water demand in a competitive, environmentally sensitive and socially responsible manner.
  • the existing residential use of water softeners by water utility customers in Southern California and other water-limited, hard-water regions varies by locality, with the home use of ion exchange (salt) softeners estimated to be between 10 and 40 percent of the residential customers.
  • USP No. 6103125 discloses several designs for a residential or commercial water desalination and softening system using a softening membrane element. The operation of the system is based upon the recycling and storage of rejected membrane concentrate. The rejected concentrate is mixed with source water for servicing 'other 1 (non-soft) water uses, and becomes the feed water for subsequent processing.
  • USP No. 4207183 discloses a method for preventing the formation of deposits caused by precipitating solutes upon membrane barriers in liquid phase separation units.
  • the method comprises providing an effective amount of small nucleation crystals in the fluid stream passing through the separation unit. Based upon the selection of the amount and size of the nucleation crystals and the process conditions, the precipitation of the slightly soluble solutes will occur upon the nucleating crystals rather than the membrane barrier.
  • the nucleating crystals containing precipitated solute are separated from the units and returned to the circulating fluid by various means.
  • USP No. 5152904 discloses a process for softening hard water by precipitation of calcium carbonate.
  • the invention teaches that the crystallization of calcium carbonate by the mere addition of a base to natural hard water is slow in spite of over-saturation because of very slow crystal growth. This is because with a small amount of crystals initially formed in dilute solutions, the chance of crystal growth by the deposition of ions on the already formed crystals is small.
  • the hard water is rendered alkaline with the addition of sodium hydroxide, and is then contacted with calcium carbonate crystal seeds to induce a rapid precipitation of dissolved calcium carbonate on to the suspended particles.
  • the process includes steps for the separation of the soft water and the re-circulation of the seed crystals to soften more hard water.
  • Chemicals are added to the feed water to increase the permeability of suspended solids and to enhance the hydrodynamic shear effects.
  • apparatus further may include a concentrate storage tank including seed crystals, the storage tank being in fluid communication between the reverse osmosis (RO) membrane and the microfiltration (MF) membrane for receiving (RO) concentrate at a pH that is conducive to metastable precipitation of calcium carbonate on the seed crystals.
  • the hydraulic pathways may include a permeate storage tank interconnected between the (RO) membrane and the delivery lines.
  • a line interconnecting the (MF) membrane and said concentrate storage tank may be provided for enabling the recirculation of the stored concentrate from said concentrate storage tank.
  • the control system may be operable for causing the circulate pump to operate so as to recycle portion of the (RO) concentrate to the potable water and to recirculate stored concentrate from the concentrate storage tank through the (MF) membrane.
  • the treated concentrate discharge volume can be reduced from 20 to 30 percent (conventional MS plant operation) to about 10 percent of the originating water.
  • Parallel desalting may be implemented on several scales of application.
  • PDS may be effectively deployed as a satellite treatment system - being dependent upon and compatible with centralized water treatment, while also maintaining a high-level functionality as a stand-alone system.
  • residential PDS systems may be integrated with conventional drinking water plant operations: (1 ) to meet the demand for residential water softening, and (2) to improve the effluent water quality discharged to centralized wastewater treatment plants and water reclamation and water reuse facilities.
  • the functioning of the PDS apparatus is governed by a microprocessor-controlled operating system.
  • the PDS system has the means to produce or supply soft water under three conditions. (1) Under conditions of high soft water demand (HD-mode of operation), the rate of soft water consumption exceeds the rate of soft water production by the RO membrane unit. A delivery pump provides soft water at the user demand rate. Rates of soft water supply in excess of the RO permeate flux are supplied from soft water storage. (2) Under conditions of low or short-interval demand (LD-mode of operation), the RO permeate production pump is not required, and the soft water is drawn from storage and supplied by the delivery pump.
  • HD-mode of operation high soft water demand
  • LD-mode of operation Low-interval demand
  • PT-mode of operation soft water produced by the prior operation of pump 20 and stored in the cold permeate tank 32, is provided as the feed water for the RO membrane unit 24.
  • the closed loop used to isolate permeate re-processing with a PT-mode of operation is provided by re-circulation line 78.
  • Delivery pump 62 is used instead of pressure pump 20, to provide a pressure increase at the inlet to RO membrane unit 24.
  • the pressure boost from pump 62 is sufficient to provide a low-level flow separation of the stored soft water through the RO membrane unit.
  • the RO membrane unit Based on the operation of delivery pump 62, the RO membrane unit produces a super-soft permeate (desalted soft water) stream in line 30 and a soft-water concentrate
  • the PT-mode of operation causes the soft water stored in container 32 to be desalted for a second time by the RO membrane unit 24.
  • the "second pass" RO-concentrate (slightly concentrated soft water) is recombined with a mixed "second pass” RO-permeate (slightly desalted soft water) from storage tank 32 to provide an essentially unaltered original blend of soft water inflow to pump 62.
  • the inflow to pump 62 is then recycled 0 via line 78 to the inlet of RO membrane unit 24.
  • the PDS control system is comprised of electronic hardware and software components.
  • a microprocessor MCP
  • MCP microprocessor
  • the printed circuit board also interfaces with an electrical power supply and with a triac board containing couplings and circuitry for switching pump motors off and on, in accordance with product water demands and the state of the PDS system.
  • the MCP also interfaces with an instrumentation display panel and LED 's that indicate the operating status of the PDS system (hydrodynamics, water storage and product quality parameters).
  • Rotary vane pump/motors suitable for Pressure Boost Pump 20 are widely available from industrial component suppliers, for example, under the trade name Fluid-O-Tech (Models PA- 70/80/90).
  • Circulation pump/motors suitable for Circulation Pump 40 are available from Laing Thermotech, Inc., (Model SM-909-B26) of San Diego, California. Pump/motors suitable for
  • TDS (mg/L) 567 105 4756 90 4374 Hardness (mg/L as CaCO3) 274 22.5 2556 16.2 2169
  • Example 2 The influence of the precipitation reaction dynamics on the attainment of desired pH levels for the seeded concentrate solution, and the stabilization of the pH during the PDS soft water supply operation, are examined in Example 2.
  • This example illustrates the exponential rate of decline of the PCC reaction (seed precipitation of calcium carbonate) with reduced pH and alkalinity.
  • the PDS90 operation is based on a pH 8.1 supply of hard alkaline water, and a 84 percent recycling of precipitated concentrate.
  • the concentrate is conditioned for longer periods of time to achieve increasingly lower levels of calcium hardness and increasingly lower re-initialed pH levels for the stored concentrate.
  • the duration required for the extended conditioning of the concentrate stored in the PDS apparatus is tabulated below.
  • Example 2 a seed precipitation reaction is used to provide recycled concentrate pH adjustments from minus 0.05 to minus 0.35.
  • the required duration of the seed precipitation reaction, and the rate of reduction of solution pH depends upon the crystal seed properties, hydrodynamic factors, and activation levels (temperature). Data are provided for solution temperatures of about 35 degrees Celcius.
  • the recycling of RO concentrate at pH 8.70, and the mixing of MF permeate stream with source water in the ratio 1 :2 would produce a RO concentrate at pH 8.75.
  • the time needed for the seed precipitation reaction to cause the solution pH to decline from pH 8.75 to pH 8.70 is about 45 seconds.
  • the attainment of the PDS target for product water quality (70 mg/L TDS) must, however, be qualified to include efficiency ratings with which product water is produced.
  • anticipated performance of the PDS system using TFC ULP4821 RO membrane elements with MWD imported water is expected to be less than about 50 mg/L TDS, with system recoveries (conversion of source water to product water) in the range 80 to 90 percent.

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)
  • Crystallography & Structural Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La déminéralisation parallèle (PDS) fait appel à un système hybride d’adoucissement de membrane (MS) pour déminéraliser l’eau d’usage résidentiel et commercial. La déminéralisation parallèle produit de l’eau 'douce' sans utiliser de sel, ou d’autre réactif chimique liquide utilisé normalement pour réaliser l’ajustement de l’acidité pH dans des processus industriels à membrane et à précipitation. Le processus PDS équilibre le fonctionnement d’une unité à membrane RO (eau potable) avec le fonctionnement d’une unité à membrane tubulaire MF (eaux usées), assurant ainsi une technologie de traitement des eaux hautement efficace et régénérative : (1) Le fonctionnement optimal du système PDS transforme environ 90 pour cent d’une eau potable, légèrement saumâtre en < 50 mg/L d’eau TDS avec une dureté d’eau < 1 grain (10 -15 mg/L comme carbonate de calcium) ; et (2) le fonctionnement du système PDS produit, en termes de salinité, en un effluent réutilisable à 100 pour cent pour recyclage en aval. Les résultats virtuels du prototype suggèrent qu’avec une eau de source Colorado River Aqueduct (570 - 620 mg/L TDS et une dureté d’eau de 16 grains), la déminéralisation parallèle peut produire un effluent avec un TDS 40 - 70 mg/L inférieur à l’alimentation d’origine (à l’exclusion de TDS fourni directement par le type particulier d’utilisation de l’eau douce).
PCT/US2004/026693 2004-08-17 2004-08-17 Procédé et appareil de déminéralisation parallèle WO2006022719A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP04781398A EP1838421A4 (fr) 2004-08-17 2004-08-17 Procédé et appareil de déminéralisation parallèle
PCT/US2004/026693 WO2006022719A1 (fr) 2004-08-17 2004-08-17 Procédé et appareil de déminéralisation parallèle

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2004/026693 WO2006022719A1 (fr) 2004-08-17 2004-08-17 Procédé et appareil de déminéralisation parallèle

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010012691A1 (fr) * 2008-07-31 2010-02-04 Otv Sa Procede de traitement d'eau par osmose inverse incluant une decarbonatation d'un concentrat et une remineralisation d'un filtrat
WO2012079740A1 (fr) * 2010-12-14 2012-06-21 Anlagen- Und Energietechnik Inh. A. Hartig Système et procédé pour purification d'eau
WO2013066842A1 (fr) * 2011-10-31 2013-05-10 Ut-Battelle Llc Prétraitement à écoulement continu de biomasse lignocellulosique par des membranes nanoporeuses inorganiques
CN106922240A (zh) * 2017-03-06 2017-07-07 江苏省农业科学院 一种滨海盐碱土地耕作层快速脱盐方法与应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4207183A (en) * 1978-05-11 1980-06-10 Resources Conservation Company Prevention of solute deposition fouling in membrane processes
US5393433A (en) * 1992-03-11 1995-02-28 Aquasource, Societe En Nom Collectif Method using separation membranes to treat a fluid containing matter in suspension and in solution
US5501798A (en) * 1994-04-06 1996-03-26 Zenon Environmental, Inc. Microfiltration enhanced reverse osmosis for water treatment
US6074551A (en) * 1998-04-30 2000-06-13 Culligan Water Conditioning Of Fairfield County Automatic cleaning system for a reverse osmosis unit in a high purity water treatment system

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL9202017A (nl) * 1992-11-19 1994-06-16 Tno Werkwijze en inrichting voor het uit een oplossing verwijderen van tenminste één bestanddeel.

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4207183A (en) * 1978-05-11 1980-06-10 Resources Conservation Company Prevention of solute deposition fouling in membrane processes
US5393433A (en) * 1992-03-11 1995-02-28 Aquasource, Societe En Nom Collectif Method using separation membranes to treat a fluid containing matter in suspension and in solution
US5501798A (en) * 1994-04-06 1996-03-26 Zenon Environmental, Inc. Microfiltration enhanced reverse osmosis for water treatment
US6074551A (en) * 1998-04-30 2000-06-13 Culligan Water Conditioning Of Fairfield County Automatic cleaning system for a reverse osmosis unit in a high purity water treatment system

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010012691A1 (fr) * 2008-07-31 2010-02-04 Otv Sa Procede de traitement d'eau par osmose inverse incluant une decarbonatation d'un concentrat et une remineralisation d'un filtrat
FR2934584A1 (fr) * 2008-07-31 2010-02-05 Otv Sa Procede de traitement d'eau par osmose inverse incluant une decarbonatation d'un concentrat et une remineralisation d'un filtrat.
WO2012079740A1 (fr) * 2010-12-14 2012-06-21 Anlagen- Und Energietechnik Inh. A. Hartig Système et procédé pour purification d'eau
EP2474506A1 (fr) * 2010-12-14 2012-07-11 Anlagen- und Energietechnik Système et procédé de préparation d'eau
WO2013066842A1 (fr) * 2011-10-31 2013-05-10 Ut-Battelle Llc Prétraitement à écoulement continu de biomasse lignocellulosique par des membranes nanoporeuses inorganiques
US9932648B2 (en) 2011-10-31 2018-04-03 Ut-Battelle, Llc Flow-through pretreatment of lignocellulosic biomass with inorganic nanoporous membranes
CN106922240A (zh) * 2017-03-06 2017-07-07 江苏省农业科学院 一种滨海盐碱土地耕作层快速脱盐方法与应用

Also Published As

Publication number Publication date
EP1838421A4 (fr) 2009-12-16
EP1838421A1 (fr) 2007-10-03

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