WO2000023382A1

WO2000023382A1 - Method and apparatus for preventing scaling in electrodeionization units

Info

Publication number: WO2000023382A1
Application number: PCT/CA1999/000882
Authority: WO
Inventors: David Florian Tessier; Robert Glegg; John H. Barber
Original assignee: E-Cell Corporation
Priority date: 1998-10-16
Filing date: 1999-09-24
Publication date: 2000-04-27
Also published as: EP1133449B1; CN101195081B; DE69912985D1; CN1323279A; MXPA01003822A; JP4805455B2; US6149788A; CA2347473C; BR9914586A; IL142488A0; AU5843899A; CN101195081A; ATE254581T1; DE69912985T2; JP2002527238A; CA2347473A1; EP1133449A1

Abstract

A method and apparatus is provided for inhibiting scaling in an electrodeionization system and, more particularly, for increasing tolerance to hardness in the feed water to an electrodeionization unit by inhibiting precipitation of scale-forming metallic cations contained in the feed water and thereby increasing efficiencies of the electrodeionization system. Water to be purified is passed through an electrodeionization unit in which the flow in the diluting compartment is countercurrent to the flow in the concentrating compartment. This is to impede the migration of scale-forming metallic cations from the diluting compartment, through the cation exchange membrane, into the concentrating compartment and towards the concentrating compartment side of the anion exchange membrane, thereby preventing scale formation on the anion exchange membrane. The electrodeionization unit may be further modified by dividing the concentrating compartments into first and second compartments by a porous diaphragm or ion-conducting membrane. The porous diaphragm or ion-conducting membrane effectively eliminates convective transport of scale-forming metallic cations from the cation exchange membrane side of the concentrating compartment to the anion exchange membrane side of the concentrating compartment, thereby inhibiting scale formation on the anion exchange membrane.

Description

METHOD AND APPARATUS FOR PREVENTING SCALING IN ELECTRODEIONIZATION UNITS

(i) Field of the Invention

The present invention relates to a method and apparatus for inhibiting scaling in

an electrodeionization system or in a combined reverse osmosis/electrodeionization

system for water treatment and, more particularly, for manipulating the flow conditions

within the electrodeionization system to inhibit precipitation of scale-forming metallic

cations and consequent scaling of concentrate-chamber side of associated anion exchange

membranes.

(ii) Description of the Related Art

The purification of liquid has become of great interest in many industries. In

particular, pure water is used for many industrial purposes such as, in processes for

producing semiconductor chips, in power plants, in the petrochemical industry and for

many other purposes.

Ion exchange resins, reverse osmosis filtration and electrodialysis techniques have

been used to reduce the concentration of ions in a liquid.

Electrodeionization apparatus have recently been used with more frequency to

reduce the concentration of ions in a liquid. The term "electrodeionization" generally

refers to an apparatus and a process for purifying liquids which combine ion exchange

resins, ion exchange membranes and electricity to purify the liquids. An

electrodeionization module comprises alternating arrangements of cation permeable

membranes and anion permeable membranes defining compartments therebetween. In alternating compartments, there is provided ion exchange resin beads. Those

compartments are known as diluting compartments. The compartments which generally

do not contain ion exchange resin are known as the concentrating compartments. Ions

migrate from the diluting compartments through ion exchange beads and ion permeable

membranes into the concentrating compartments by the introduction of current. The

liquid flowing through the concentrating compartments is discarded or partially recycled

and the purified liquid flowing through the diluting compartments is recovered as

demineralized liquid product.

Scaling of electrodeionization equipment is of particular concern as it reduces

membrane efficiencies and fouls electrode surfaces. Scaling has been found to occur in

localized regions of electrodeionization equipment, and particularly those where high pH

is typically present. Such regions include those on the surface of the concentrate-

chamber side of anion exchange membranes, due to the flux of hydroxyl ions resulting

from the regenerative water splitting process in the diluting chambers. Localized regions

of high pH are also typically present on the cathode surface due to the evolution of

hydrogen gas and concomitant production of hydroxyl ion according to the cathodic

electrode reaction:

2e- + 2H₂O = H₂ (gas) + 2OH-

These localized regions of high pH provide conditions under which scales

harmful to the performance of the electrodeionization device can form. Generally, these

scales form in the presence of polyvalent metal cations such as Ca²⁺, Mg²⁺, Sr²⁺, Ba²⁺,

Fe³⁺, Al³⁺ and the like which can precipitate under local high pH conditions as

hydroxides, oxides, sulphates and phosphates when these anions are present, carbonates when carbonate, bicarbonate or carbon dioxide is present, mixed oxides such as spinels,

mixed carbonates, and fluorides when fluoride ions are present. Due to the low solubility

products of these compounds, and to the high local pH, even trace amounts of these metal

cations and counter anions in the concentrate streams will be sufficient to cause

undesirable precipitation.

Prior art methods for preventing scale formation typically focus on removing

polyvalent cations from the supply stream to the concentrate chamber by adding water

softeners. This necessarily requires the addition of chemicals to the system, which

potentially compromises the quality of associated effluent streams, thereby raising

environmental concerns.

Another prior art method, disclosed in European Patent Application Serial No.

97118847.9 teaches acid injection to the concentrate chamber supply stream to neutralize

the basic conditions particularly arising at the concentrate chamber side of associated

anion exchange members. To be effective, this method requires the addition of

significant amounts of acid, sometimes generated on-site with additional ancillary

equipment. Such features render this method relatively expensive.

Summary of The Invention

In its broad aspect, the present invention provides a method for inhibiting

formation of scale in an electrodeionization unit for deionizing water having an anode

compartment at one end of the unit, a cathode compartment at the opposite end of the

unit, and a plurality of diluting compartments alternating with concentrating

compartments positioned between the anode and cathode compartments, which comprises passing feed water to be deionized through the diluting compartments, passing water or

an aqueous solution for accepting ions from the feed water through at least one of the

concentrating compartments in a direction opposite to that of the feed water, passing

water in an aqueous solution through the anode and cathode compartments, and applying

an electrical voltage between the anode and the cathode whereby ions in the feed water

migrate to the water or aqueous solution in the concentrating compartments. Prior to

introduction to the concentrating compartment, the water or aqueous solution may be

treated for removal of scale-forming metallic cations by a suitable unit operation, such

as reverse osmosis or water softening. Alternatively, a bleed of purified water from the

discharge of the diluting compartments in the electrodeionization unit can supply water

to the concentrating compartment. Salt can be inj ected into the water or aqueous solution

being supplied to the concentrating compartment for increasing electrical conductivity

within the concentrating compartment.

In another aspect, the present invention provides an electrodeionization unit for

deionizing water having an anode compartment at one end of the unit, a cathode

compartment at the opposite end of the unit, and a plurality of diluting compartments

alternating with concentrating compartments between the said anode and cathode

compartments, each of said diluting and concentrating compartments defined by anion

and cation exchange membranes, each of said concentrating compartments further

comprising a porous diaphragm or ion-conducting membrane for dividing said

concentrating compartment into first and second compartments such that the first

compartment is defined by an anion exchange membrane and the porous diaphragm or

ion-conducting membrane and the second compartment is defined by the cation exchange membrane and the porous diaphragm or ion-conducting membrane wherein liquid in the

first compartment is prevented from mixing with liquid in the second compartment and

wherein ions can migrate under the influence of the applied electric field between the first

and second compartments through the porous diaphragm or ion-conducting membrane.

In yet a further aspect, the present invention provides a method for inhibiting

scale formation in an electrodeionization unit for deionizing water having an anode

unit, and a plurality of diluting compartments alternating with concentrating

compartments positioned between the anode and cathode compartments, each of the

concentrating compartments further comprising a porous diaphragm or ion-conducting

membrane for dividing the concentrating compartment into first and second

compartments such that the first compartment is defined by an anion exchange

membrane and the porous diaphragm or ion-conducting membrane and the second

compartment is defined by the cation exchange membrane and porous diaphragm or ion-

conducting membrane wherein liquid in said first compartment is prevented from mixing

with liquid in the second compartment and wherein ions can migrate between the first

and second compartments through the porous diaphragm or ion-conducting membrane,

such method comprising passing feed water to be deionized through the diluting

compartments, passing water or an aqueous solution for accepting ions from the feed

water through the concentrating compartments in a direction opposite to that of the feed

water, passing water in an aqueous solution through the anode and cathode

compartments, applying an electrical voltage between the anode and the cathode whereby

ions in the feed water migrate to the water or aqueous solution in the concentrating compartments. Prior to introduction to the concentrating compartment, the water or

aqueous solution can be treated for removal of metallic cations by a suitable unit

operation, such as reverse osmosis or water softening. Alternatively, the water being

passed through the concentrating compartment can be supplied from a bleed of purified

water from the discharge of the diluting compartments in the electrodeionization unit.

Salt can be inj ected into the water or aqueous solution being supplied to the concentrating

compartment for increasing electrical conductivity within the concentrating compartment.

Brief Description of The Drawings

The method and apparatus of the invention will now be described with reference

to the accompanying drawings, in which:

Figure 1 is a schematic flowsheet of a first embodiment of the present

invention;

Figure 2 is a schematic flowsheet of a second embodiment of the present

invention;

Figure 3 is a schematic flowsheet of a third embodiment of the present

invention;

Figure 4 is a schematic flowsheet of a fourth embodiment of the present

invention;

Figure 5 is a detailed schematic drawing of an electrodeionization unit of any

of the Figures 1, 2, 3 and 4;

Figure 6 is a schematic flowsheet of a fifth embodiment of the present

invention; and Figure 7 is a detailed schematic drawing of a section of the electrodeionization

unit of Figure 6.

Description of the Preferred Embodiment

The processes of the present invention will be described with reference to the

accompanying drawings. In general, the invention is applicable to water purification

processes which are carried out using an electrodeionization unit or with an

electrodeionization unit and reverse osmosis unit in series.

Referring first to Figures 1 and 5, the electrodeionization unit 10 in accordance

with the present invention comprises the anode compartment 20 provided with an anode

24 and the cathode compartment 22 provided with a cathode 26. A plurality of cation

exchange membranes 28 and anion exchange membranes 30 are alternately arranged

between the anode compartment 20 and the cathode compartment 22 to form diluting

compartments 32 each defined by anion exchange membrane 30 on the anode side and

by a cation exchange membrane 28 on the cathode side and concentrating compartments

18 each defined by a cation exchange membrane 28 on the anode side and by an anion

exchange membrane 30 on the cathode side. Electrolyte solution is supplied to anode

compartment 20 and to cathode compartment 22 via flowstreams 36 and 38 respectively

with respective discharges 60 and 62.

Ion exchange material such as ion exchange resin beads designated by numeral

40 preferably are provided in diluting compartments 32. These may comprise either

anion or cation exchange resins or a mixture thereof, mixed bed, layers,

continuous/discontinuous phases, and the like, such as disclosed in PCT Application Serial No. PCT/CA97/00018, incorporated herein by reference. Such media enhance

water purification by removing unwanted ions by ion exchange. Further, such media

facilitate migration of ions towards membranes 28 and 30 for subsequent permeation

therethrough, as will be described herein below.

Water to be treated is introduced into the diluting compartments 32 from supply

stream 42. Similarly, water or an aqueous solution is introduced into the concentrating

compartments 18 from a supply stream 44. Stream 44 can also supply flowstreams 36

and 38 for supplying water or aqueous solution to anode compartment 20 and cathode

compartment 22 respectively. A predetermined electrical voltage is applied between the

two electrodes whereby anions in diluting compartments 32 permeate through anion

exchange membranes 30 and into concentrating compartments 18 while cations in

streams in diluting compartments 32 permeate through cation exchange membranes 28

and into concentrating compartments 18. The above-described migration of anions and

cations is further facilitated by the ion exchange material 40 present in diluting

compartments 32. In this respect, driven by the applied voltage, cations in diluting

compartments 32 migrate through cation exchange resins using ion exchange

mechanisms, and eventually pass through cation exchange membranes 28 which are in

direct contact with the cation exchange resins. Similarly, anions in diluting

compartments 32 migrate through anion exchange resins using ion exchange

mechanisms, and eventually pass through anion exchange membranes 30 which are in

direct contact with the anion exchange resins. Aqueous solution or water introduced into

concentrating compartments 18 from stream 44, and anion and cation species which

subsequently migrate into these compartments, are collected and removed as a concentrated solution from discharge stream 48, while a purified water stream is

discharged from diluting compartments 32 as discharge stream 50.

By virtue of the current flowing between the cathode 26 in the cathode

compartment 22 and the anode 24 in the anode compartment 20, water is ionized into

hydrogen and hydroxyl ions. Hydroxyl ions migrate through the anion exchange

membrane 30 and become locally concentrated on the surface 52 of the concentrate

compartment side of the anion exchange membrane 30. This creates a localized region

of high pH near this surface 52 of the anion exchange membrane 30, thereby promoting the formation of scale.

To prevent the formation of scale on the surfaces 52 of the anion exchange

membrane 30, the water or aqueous solution in the concentrating compartment 18 flows

in the opposite direction, or in counterflow manner, relative to the water being purified

in diluting compartment 32. The thermodynamic tendency of scale-forming metallic

cations, such as Mg²⁺, to be removed from the water being treated in diluting

compartment 32 and adsorbed on ion exchange material 40 is greater than for other

passive cations, such as Na⁺. As a result, scale-forming metallic cations such as Mg²⁺

tend to be removed by ion exchange material located proximate to the supply side of the

diluting compartment 32 and, consequently, migrate towards and through the associated

cation exchange membrane 28 and into the water or aqueous solution of the concentrating

compartment 18 proximate to the discharge side of the concentrating compartment 18.

In order to cause scale formation on the concentrate compartment 18 side of anion

exchange membrane 30, such scale-forming metallic cations must be successfully

transported to the concentrate compartment side surface 52 of such anion exchange membrane 30. The success of such transport depends on the amount of flow distance

and, hence, residence time such scale-forming metallic cations are provided within the

concentrate compartment 18 and the operative transport phenomena occurring therein

which causes transport of the metallic cations to the compartment side surface 52 of the

anion exchange membrane 30. Because the scale-forming metallic cations tend to exist

in the concentrating compartment 18 proximate to the discharge side of the concentrating

compartment 18, the flow distance and residence time of such scale-forming metallic

cations in the concentrating compartment 18 is relatively short, thereby reducing the risk

of scale formation. Most notably, such flow distance and residence time is much shorter

than for the case where the aqueous solution or water in the concentrating compartment

18 flowed in the same direction, or co-currently, as the water in the diluting compartment

32.

In the embodiment of the present invention illustrated in Figure 2, supply stream

44 comprises of a bleed from discharge stream 50 from the diluting compartment 32.

Such supply stream 44 is relatively free of scale-forming metallic cations, and therefore

does not contribute to conditions which favour scale formation on the concentrate

compartment side surface 52 of the anion exchange membrane 30. Because the discharge

stream 50 comprises of water purified by the electrodeionization unit 10, the dissolved

salt concentration of the discharge stream 50 is substantially non-existent. Such water,

left untreated, would be highly resistant to current flow through the electrodeionization

unit 10. Accordingly, to mitigate this problem, it is desirable to inject saline solution into

supply stream 44 to increase the conductivity of the water in the concentrating

compartment 18. This can involve injecting a solution of an inert salt from storage vessel 45, such as sodium chloride or potassium chloride, into supply stream 44 by means of a

metering pump 47. As an example, metred injection of 100 g/L sodium chloride solution

can be employed to add 50 to 500 mg/L of sodium chloride to the concentrate

compartment supply stream 44.

In the embodiment of the present invention illustrated in Figure 3,

electrodeionization unit 10 is operated in series with reverse osmosis unit 62 for the

purification of water. Water to be treated is supplied into the reverse osmosis unit 62 by

supply stream 64, wherein the supplied water is separated into permeate stream 66 and

retentate stream 68 by membrane 70, well known in the art. The permeate stream 66 is

connected to supply stream 42 for further treatment in the electrodeionization unit 10,

whereas retentate stream 68 either is discharged to drain or is used for other purposes,

such as in cooling towers. A bleed is taken from the permeate stream 66 and connected

to supply stream 44 for supply of aqueous liquid to concentrating compartment 18, anode

compartment 20 and cathode compartment 22.

By virtue of pre-treatment in the reverse osmosis unit 62, permeate stream 66 and,

therefore, supply stream 44, contain sufficiently low scale-forming metallic cation

concentrations such that their contribution to scale formation in the concentrating

compartment 18 may be insubstantial. Preferably, the concentration of scale-forming

metallic cations in supply stream 44 is less than 5 ppm as calcium carbonate, and more

preferably less than 1 ppm as calcium carbonate. However, for these same reasons,

supply stream 44 may contain low salt concentrations and, as a result, may not be

sufficiently conductive for use in the concentrating compartment 18 of the

electrodeionization unit 10. Accordingly, to mitigate this problem, it may be desirable to inject saline solution into supply stream 44 to increase the conductivity of the water

in the concentrating compartment 18, anode compartment 20, and cathode compartment 22 as in the manner with respect to the embodiment illustrated in Figure 2.

In the embodiment illustrated in Figure 4, instead of being treated in a reverse osmosis unit 62 as in accordance with the embodiment in Figure 3, the supply stream 44

may comprise of water which has been bled from reverse osmosis unit supply stream 64

and then softened by softening unit 80 to remove unwanted scale-forming metallic

cations. The bleed from supply stream 64 can be subjected to upstream pre-treatment by

separator 65 wherein pre-treatment means include mechanical filtration, classification, or activated carbon adsorption. Water bled from supply stream 64 is supplied into

softening unit 80 by supply stream 82. Softening is usually accomplished by means of ion exchange. In this respect, softening unit 80 can comprise of a sodium-cycle softener

having a pressure vessel containing strong acid cation exchange resin in the sodium form. Scale-forming metallic cations in stream 82 to the softening unit 80 are taken up by the

cation exchange resin with the concomitant release of sodium ions. As a result, the discharge stream 84 from the softening unit 80 is depleted in scale-forming metallic

cations. When exhausted, the strong acid cation exchange resin is regenerated using

sodium chloride brine. Similar ion exchange softeners may employ other regenerating chemicals, such as potassium chloride or mineral acids, or other types of ion exchange

resins, such as weak acide cation exchange resin.

The discharge stream 84 from the softening unit 80 may be connected to the

supply stream 44 for supply of aqueous liquid to the concentrating compartment 18, anode compartment 20, and cathode compartment 22. Dissolved salt concentrations in discharge stream 84 are sufficiently high such that additional salt injection is typically

not necessary for purposes of increasing conductivity of the aqueous liquid in

concentrating compartment 18, anode compartment 20, and cathode compartment 22.

Figures 6 and 7 illustrate a further embodiment of the present invention wherein

an electrodeionization unit 100 has concentrating compartments 118 which are divided

into first and second compartments 119a and 119b by a porous diaphragm or ion-

conducting membrane (hereinafter "separator") 120. Porous diaphragm can be composed

of mesh or perforated sheet made from polyolefin material, or can comprise of felts or

non-woven sheets. A suitable commercially available porous diaphragm is MF™

Membrane No. 1147027, MF™ Membrane No. 1147028, or MF™ Membrane No.

1147029, all of which are manufactured by Osmonics of Minnetonka, MN, U.S.A., or

Celgard™ 3401 Microporous Flat Sheet Membrane, or Celgard™ 3501 Microporous Flat

Sheet Membrane, both of which are manufactured by Hoechst Celanese Corporation,

13800 South Lakes Drive, Charlotte, N.C., U.S.A. Ion-conducting membranes can be

either permselective or non-permselective. Non-permselective membranes include

dialysis membranes, membranes with both positive and negative fixed ionic groups,

examples of which comprise sulfonates, quaternary amines, and carboxylates. Suitable

commercially available perm-selective membranes include SELEMION AME™ and

SELEMION CME™, both manufactured by Asahi Glass Co. of Japan.

Aqueous solution or water introduced into each of first compartment 119a and

second compartment 119b by supply line 44, and anion and cation species which

subsequently migrate into these compartments, are collected and removed as a

concentrate solution from discharge stream 48. In all other aspects, electrodeionization unit 100 is identical to electrodeionization unit 10 illustrated in Figure 5.

First compartment 119a is defined by anion exchange membrane 30 and separator

120, and second compartment 119b is defined by cation exchange membrane 28 and

separator 120. Separator 120 prevents mixing of liquids in first compartment 119a with

liquid in second compartment 119b, but permits dissolved ions to migrate between the

first compartment 119a and second compartment 119b under the influence of the applied

electric field.

The present invention will be described in further detail with reference to the

following non-limitative examples.

EXAMPLE 1

An electrodeionization device (effective area 507 cm² [width (^diluting and

concentrating compartment spacer width) 13 cm, length (=diluting and concentrating

compartment spacer length) 39 cm] x 30 cell pairs) comprised a filter press type

electrodeionization stack, having diluting compartments alternating with concentrating

compartments, each of these compartments being bounded by a cation exchange

membrane (strong acid type heterogeneous membrane, thickness 0.05 cm, ion exchange

capacity 4.5 meq/g-dry resin) and an anion exchange membrane (strong base type

heterogeneous membrane, thickness 0.05 cm, ion exchange capacity 3.5 meq/g-dry resin)

arranged and fixed by way of diluting compartment spacer frames (made of

polypropylene) and concentrating compartment frames (made of polyolefin). The

thickness of the demineralizing compartments was 0.8 cm. The open areas of the

concentrating compartments consisted of a sequential layered arrangement of two layers

of 0.56 mm thick polypropylene fused mesh, one (middle) layer of 0.18 mm thick porous membrane (MF membrane #1147027 from Osmonics, Minnetonka, MN, U.S.A.) and two

layers of 0.56 mm thick polypropylene fused mesh. The middle layer functioned as a

separator membrane and serve to limit the convective mixing in the concentrating

compartments.

The diluting compartments were packed with cation exchange resin and anion

exchange resin, each resin in the form of a sheet-like product consisting of a mixture of

ion exchange resin and a binder in a dry state. The above two ion exchange resins were

of a sulfonic acid type cation exchange resin (Diaion SK-1B™ manufactured by

Mitsubishi Chemical Corporation) and a quaternary ammonium salt anion exchange resin

Diaion SA-10A™ manufactured by Mitsubishi Chemical Corporation) and were used in

an anion to cation volumetric ration (dry) of 54:46.

By using this electrodeionization device, a test was carried out in the following

manner. Feed water to be purified was prepared comprising of 1 ppm hardness as CaCO₃

(0.67 ppm Ca, 0.33 ppm Mg), 0.5 ppm reactive silica as SiO₂, and 13.5 ppm sodium

chloride. The feed water to be purified was passed in a downward direction through the

diluting compartments of the electrodeionization device at a flow rate of 12.5 US gpm.

Low hardness water, whose conductivity was increased to 800 - 1 ,800 microSiemens/cm

by the injection of a low hardness solution of sodium chloride, was passed in an upward

direction (countercurrent flow) through the concentrating and electrode compartments

at a flow rate of 1.0 - 1.1 US gpm and discharged to drain. The concentrate and electrode

feed stream was introduced at a pressure of 5 - 10 psig below that of the outlet stream

from the diluting compartments. The D.C. electric current through the

electrodeionization device was set at 4.3 Amps using a rectifier capable of a maximum output voltage of 600 Volts. During operation, the stack voltage and product water

resistivity were monitored for indications of deleterious scaling (increase in voltage,

decrease in product water resistivity). At the start of the experiment, the maximum

applied voltage of 600 Volts produced a current of 3.2 Amps, but this current increased

to the set point of 4.3 Amps while the voltage dropped to 470 Volts and remained at this

level for the duration of the experiment (386 hours operation). The product water

maintained a resistivity value over 17.3 MOhm.cm for the duration of the experiment.

The constant voltage and consistently high product water resistivity indicate the absence

of significant scaling.

EXAMPLE 2

A comparative experiment was conducted in the manner as in Example 1

described above, with the following exceptions:

a) the open areas of the concentrating compartments consisted of a

sequential layered arrangement of one layer of 0.56 mm thick

polypropylene fused mesh, one (middle) layer of 1.0 mm thick

polypropylene fused mesh, and one layer of 0.56 mm thick polypropylene

fused mesh. The open nature of the middle mesh layer allowed for

convective mixing in the concentrating compartments,

b) the feed to the diluting compartments was directed upward in a co-flow

direction with respect to the concentrate and electrode streams, and

c) the concentrate stream was partially recirculated to the electrodeionization

device, with make-up water to the concentrate loop consisting of feed

water to be treated (including hardness). The target operating current of 4.3 Amps was passed with the available 600 Volts

D.C. (concentrate feed conductivity of 800 micro Siemens/cm) for the first few hours, and

the current then decreased steadily to 2 Amps (maximum D.C. voltage of 600 Volts) over

the duration of the experiment (300 hours). The product water resistivity had an initial

value of 17.5 MOhm.cm, but decreased to 16 MOhm.cm after 220 hours of operation,

and further decreased to less than 2 MOhm.cm after 300 hours of operation. These

decreases in current (at constant voltage of 600 Volts D.C.) and product resistivity are

typical of the formation of scale on the concentrate chamber side of the anion

membranes.

As indicated in the above Example 1 and Example 2, operation of an

electrodeionization device as described in accordance with the process and apparatus of

the present invention (counter-current flow, separator membrane in concentrate chamber,

low hardness feed water to the concentrate chambers, and no recirculation of concentrate

outlet) enabled an electrodeionization device to operate in the presence of hardness in the

water to be treated without accumulation of scale.

The present invention provides a number important advantages. By effecting

countercurrent flow in the diluting and concentrating compartments, scale-forming

metallic cations which migrate into the concentrating compartments are provided with

and a shorter flow length and, hence, less residence time in the concentrating

compartments. This is particularly due to the fact that the majority of scale-forming

metallic cations in the feed water to the diluting compartments are removed proximate

the inlet end of the diluting compartment and subsequently migrate through the cation

exchange membrane and enter the concentrating compartment proximate the discharge end of the concentrating compartment. By doing so, the amount of flow length and,

hence, time available for transport of scale-forming metallic cations to the surface of the anion exchange membrane is reduced, thereby mitigating scale formation at such surface.

As a further means of impeding transport of metallic cations to the concentrate compartment side surface of the anion exchange membranes, the concentrate

compartment may be divided into first and second compartments by a porous diaphragm

or ion-conducting membrane such that the liquid proximate to the anion exchange membrane is prevented from mixing with the liquid proximate the cation exchange membrane but migration of ions through the above-mentioned diaphragm or membrane

is permitted. In this respect, the diaphragm or membrane effectively reduces the rate of transport of scale-forming metallic cations from the compartment proximate the cation

exchange membrane to the compartment proximate the anion exchange membrane by substantially eliminating the convective element of such transport.

It will be understood, of course, that modifications can be made in the embodiments of the invention described herein without departing from the scope and

purview of the invention as defined by the appended claims.

Claims

We claim:

1. A method for inhibiting formation of scale in an electrodeionization unit for

deionizing water having an anode compartment at one end of the unit, a cathode

alternating with concentrating compartments positioned between the said anode and

cathode compartments, comprising the steps of:

passing feed water to be deionized through the diluting compartments to produce a purified water stream;

passing water or an aqueous solution for accepting ions from the feed water

through at least one of said concentrating compartments in a direction opposite

to that of said feed water;

passing water or an aqueous solution through the anode and cathode

compartments;

applying an electrical voltage between the said anode and the said cathode

whereby ions in the feed water migrate to the water or aqueous solution in the

concentrating compartments.

2. The method as claimed in claim 1 wherein said water or aqueous solution for

accepting ions from the feed water is passed through each of said concentrating

compartments in a direction opposite to that of said feed water.

3. The method as claimed in claim 2 wherein said water or aqueous solution for

accepting ions from the feed water is not recycled.

4. The method as claimed in claim 2 comprising the additional step of removing

scale-forming metallic cations from said water or aqueous solution for accepting ions from the feed water prior to passing said water or aqueous solution through said concentrating compartment.

5. The method as claimed in claim 2 wherein said water or aqueous solution for

accepting ions from the feed water is supplied by a bleed from said purified water stream.

6. The method as claimed in claim 2 wherein said water or aqueous solution for

accepting ions from the feed water has a concentration of scale-forming metallic ions of

less than 5 ppm as calcium carbonate prior to introduction to said concentrating

compartment.

7. The method as claim 6 wherein said concentration of scale-forming metallic

cations is less than 1 ppm as calcium carbonate.

8. The method as claimed in claim 7 wherein said scale-forming metallic cations are

selected from the group consisting of: Ca²⁺, Mg²⁺, Sr²⁺, Ba²⁺, Fe³⁺, and Al³⁺.

9. The method as claimed in claim 4 wherein said scale-forming metallic cations are

removed by a water softening process.

10. The method as claimed in claim 4 wherein said water or aqueous solution for

accepting ions from the feed water is supplied by a bleed from a permeate stream of a

reverse osmosis unit.

11. The method as claimed in claim 5 comprising the additional step of injecting

saline solution to said water or aqueous solution for accepting ions from the feed water

prior to passing through said concentrating compartment.

12. The method as claimed in claim 10 comprising the additional step of injecting

prior to passing through said concentrating compartment.

13. An electrodeionization unit for deionizing water having an anode compartment

at one end of the unit, a cathode compartment at the opposite end of the unit, and a

plurality of diluting compartments alternating with concentrating compartments between

the said anode and cathode compartments, each of said diluting and concentrating

compartments defined by anion and cation exchange membranes, at least one of said

membrane for dividing said concentrating compartment into first and second

compartments such that said first compartment is defined by an anion exchange

membrane and said porous diaphragm or ion-conducting membrane and said second

compartment is defined by said cation exchange membrane and said porous diaphragm

or ion-conducting membrane wherein liquid in said first compartment is prevented from

mixing with liquid in said second compartment and wherein ions can migrate between

said first and second compartments through said porous diaphragm or ion-conducting

membrane.

14. A method for inhibiting formation of scale in an electrodeionization unit for

deionizing water having an anode compartment at one end of the unit, a cathode

alternating with concentrating compartments between the said anode and cathode

and cation exchange membranes, at least one of said concentrating compartments further

comprising a porous diaphragm or ion-conducting membrane for dividing said

concentrating compartment into first and second compartments such that said first

compartment is defined by an anion exchange membrane and said porous diaphragm or ion-conducting membrane and said second compartment is defined by said cation

exchange membrane and said porous diaphragm or ion-conducting membrane wherein

liquid in said first compartment is prevented from mixing with liquid in said second

compartment and wherein ions can migrate between said first and second compartments

through said porous diaphragm or ion-conducting membrane, comprising the steps of:

passing feed water to be deionized through the diluting compartments to produce

a purified water stream;

passing water or an aqueous solution for accepting ions from the feed water

through the first and second concentrating compartments;

passing water or an aqueous solutions through the anode and cathode

compartments;

applying an electrical voltage between the said anode and the said cathode

whereby ions in the feed water migrate to the water or aqueous solution in the

first and second concentrating compartments.

15. The method as claimed in claim 14 wherein said water or aqueous solution for

accepting ions from the feed water is passed through at least one of said second

concentrating compartment of said concentrating compartments in a direction opposite

to that of said feed water.

16. The method as claimed in claim 15 wherein said water or aqueous solution for

accepting ions from the feed water is passed through each of said second concentrating

compartment of said concentrating compartments in a direction opposite to that of said

feed water.

17. The method as claimed in claim 16 wherein said water or aqueous solution for accepting ions from the feed water is not recycled.

18. The method as claimed in claim 16 comprising the additional step of removing

scale-forming metallic cations from said water or aqueous solution for accepting ions

from the feed water prior to passing said water or aqueous solution through said

concentrating compartment.

19. The method as claimed in claim 16 wherein said water or aqueous solution for

20. The method as claimed in claim 16 wherein said water or aqueous solution for

compartment.

21. The method as claim 20 wherein said concentration of scale-forming metallic

cations is less than 1 ppm.

22. The method as claimed in claim 21 wherein said scale-forming metallic cations

are selected from the group consisting of: Ca²⁺, Mg²⁺, Sr²*, Ba²⁺, Fe³⁺, and Al³⁺.

23. The method as claimed in claim 18 wherein said scale-forming metallic cations

are removed by a water softening process.

24. The method as claimed in claim 18 wherein said water or aqueous solution for

reverse osmosis unit.

25. The method as claimed in claim 19 comprising the additional step of injecting

prior to passing through said concentrating compartment.

26. The method as claimed in claim 24 comprising the additional step of injecting

prior to passing through said concentrating compartment.