CN101472847A - Low scale potential water treatment - Google Patents
Low scale potential water treatment Download PDFInfo
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- CN101472847A CN101472847A CN200780023054.8A CN200780023054A CN101472847A CN 101472847 A CN101472847 A CN 101472847A CN 200780023054 A CN200780023054 A CN 200780023054A CN 101472847 A CN101472847 A CN 101472847A
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Images
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- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
公开了具有低水垢潜在性的电化学处理设备。该设备具有各种涉及层化的阴离子交换和阳离子交换的构型。该处理设备也可包含非均一粒度的离子交换树脂珠粒和/或具有至少一个的室，该室提供导致贯穿该装置的均匀电流分布的主要电阻。
An electrochemical treatment device with low scaling potential is disclosed. The device has various anion-exchange and cation-exchange configurations involving stratification. The processing device may also contain ion exchange resin beads of non-uniform size and/or have at least one chamber that provides a primary electrical resistance resulting in uniform current distribution throughout the device.
Description
Background of invention
1. invention field
The present invention relates to have low scale forms the water treatment system and the method for potentiality and especially relates to the potentiality that the reduction incrustation scale forms in the system that adopts electricity driving tripping device.
2. correlation technique discussion
The electricity that has been used for treating water drives tripping device and includes, but not limited to electrodialysis and electric deion equipment.For example people such as Liang is at U.S. patent No.6, and 649,037 disclose a kind of electric deionizer and by removing the method that ionisable substance is used for purification of fluids.
Summary of the invention
One or more aspect of the present invention relates to the electric deionizer with anolyte compartment and cathode compartment.This electric deionizer comprises the first consumption chamber between anolyte compartment and cathode compartment, with the concentration compartments that consumes the chamber ionic communication, consume the chamber with second of concentration compartments's ionic communication, and in the first consumption chamber and anolyte compartment and cathode compartment, completely cut off the unit between at least one and with first of their ionic communication.
Others of the present invention relate to a kind of electric deionizer, comprise consume the chamber and with consume the chamber ionic communication, and to first concentration compartments that small part is determined by anion-selective membrane and cation selective film.First concentration compartments comprises usually, comprises first district that comprises cation exchange medium basically that separates basically by second district and the anion-selective membrane that comprises anionic exchange medium basically at least partially.
Others of the present invention relate to a kind of electric deionizer, comprise consuming the chamber, with first concentration compartments that consumes the chamber ionic communication and with second concentration compartments that consumes the chamber ionic communication.First concentration compartments comprises have first virtual resistance medium of (current resistance) usually, and the part of second concentration compartments comprises the medium that has greater than second virtual resistance of first virtual resistance.
Others of the present invention relate to a kind of electric deionizer, comprise consume the chamber and with the concentration compartments that consumes the chamber ionic communication.The concentration compartments comprises the mixture of anionite-exchange resin and Zeo-karb usually, the flow-path-length of anionite-exchange resin and the amount relative concentration compartments of Zeo-karb in mixture and changing.
Others of the present invention relate to a kind of electric deionizer with at least one chamber, and described chamber has at least one outlet port of being determined by the divider with a plurality of holes.Electric deionizer can comprise the first layer particle in the chamber that with the ion selective membrane is the boundary.Described particle can comprise and has the medium that is lower than undersized first effective diameter of Kongzui.Electric deionizer further comprises second layer particle in the chamber in the first layer downstream.Second layer particle has usually greater than first effective diameter with greater than undersized second effective diameter of Kongzui.
Further aspect of the present invention relates to the electrodeionization system, comprises water source to be processed, comprises the processing components that consumes chamber and concentration compartments, and described processing components fluid is connected to water source to be processed; Comprise acid and generate salt brine solution source on the inlet that the electrolysis unit of chamber and acid that fluid is connected to electrolysis unit generates the chamber.The electrolysis unit fluid is connected the upstream of concentration compartments.
Some aspect of the present invention relates to a kind of electric deionizer, comprises the chamber of the mixture of anion exchange resin-containing and Zeo-karb.The mean diameter of anionite-exchange resin is at least 1.3 times of mean diameter of Zeo-karb.
Some aspect of the present invention relates to a kind of electric deionizer, comprises the chamber of the mixture of anion exchange resin-containing and Zeo-karb.The mean diameter of Zeo-karb is at least 1.3 times of mean diameter of anionite-exchange resin.
Others of the present invention relate to a kind of water treatment system, comprise water source to be processed, comprise a plurality of concentration compartmentss and consume the chamber and fluid be connected to the electric deion equipment on the water source to be processed, the water cooler that is communicated with hydro-thermal at least one concentration compartments that will be introduced into electric deion equipment, be configured to provide the water that will be introduced in the concentration compartments and leave the transmitter that at least a temperature in the water of concentration compartments shows and be designed to receive temperature and show and produce and promote cooling will be introduced into the controller of the signal of the water in the concentration compartments.
Others of the present invention relate to electric deionizer, comprise the consumption chamber of being determined by cation selective film and anion-selective membrane to small part, with determined by anion-selective membrane to small part and comprise the first layer anionic exchange medium and be positioned at the concentration compartments of the second layer medium in the first layer downstream that the described second layer comprises anionic exchange medium and cation exchange medium.
Others of the present invention relate to a kind of in having the electric deion equipment that consumes chamber and concentration compartments the method for the treatment of water.This method comprises the temperature of measuring the logistics in the concentration compartments, be introduced into the temperature of the logistics in the concentration compartments and leave one of the temperature of the logistics of concentration compartments; The temperature that will be introduced into the water in the concentration compartments is reduced to preset temperature; Institute's water to be processed is introduced the consumption chamber; With at least a non-required material of removal at least a portion from institute's water to be processed of electric deion equipment.
Others of the present invention relate to a kind of in electric deion equipment the method for the treatment of water, the consumption chamber that comprises the water introducing electric deion equipment that will have negatively charged ion and cationic substance, promote at least a portion cationic substance to be transferred to, and promote at least a portion anionic species to be transferred in the consumption chamber of electric deion equipment and the second isolated unit between the anolyte compartment in the consumption chamber of electric deion equipment and the first isolated unit between the cathode compartment.
Others of the present invention relate to a kind of in having the electric deion equipment that consumes chamber and concentration compartments the method for the treatment of water.This method comprise with the water to be processed consumption chamber of introducing electric deion equipment, promote non-required material to be transferred to the concentration compartments of electric deion equipment from consuming the chamber.The concentration compartments can comprise the first layer anionic exchange medium usually and be positioned at the second layer medium in the first layer downstream, and the second layer can comprise the mixture of anionic exchange medium and cation exchange medium.
Others of the present invention relate to a kind of method for the treatment of water, comprise with the water to be processed consumption chamber of introducing electric deion equipment, described consumption chamber has the sub-exchang medium of at least one leafing; Be introduced at least a portion anionic species that consumes the water in the chamber with promotion and be transferred to first concentration compartments has first intermediate mass with generation water from the first layer Ion Exchange Medium.First concentration compartments is determined by anion-selective membrane and cation selective film at least in part.First concentration compartments comprises first district that comprises cation exchange medium that second district by comprising anionic exchange medium separates with anion-selective membrane basically at least in part.
Others of the present invention relate to a kind of in electric deion equipment the method for the treatment of water.This method comprise with comprise non-required material the water to be processed consumption chamber of introducing electric deion equipment, promote non-required material to transfer to the concentration compartments of electric deion equipment to generate treating water from consuming the chamber; Electrolysis produces acid solution and at least a portion acid solution is introduced the concentration compartments in accessory part.
Others of the present invention relate to a kind of water treatment system, comprise institute water source to be processed and comprise that first consumes the electric deion equipment of the chamber and the second consumption chamber, and first and second consume chambers is connected on the institute water source to be processed with split flow configuration fluid respectively; With with first consume first concentration compartments of chamber ionic communication and second concentration compartments that fluid is connected to downstream, first concentration compartments.
Others of the present invention relate to electric deionizer, comprise a plurality ofly being designed to make liquid to consume chamber and concentration compartments a plurality of and at least one consumption chamber ionic communication along the parallel flow paths mobile therein, and wherein arrange in turn the partial concentration chamber at least.
Accompanying drawing is briefly described
Accompanying drawing has no intention to draw in proportion.In the accompanying drawings, each that shows in each figure element identical or much at one is represented with same numbers.For clarity sake, be not each element all can be in each accompanying drawing mark.
In the accompanying drawings:
Fig. 1 illustrative is according to the part that comprises at least one isolated unitary electric deionizer of one or more embodiments of the invention;
Fig. 2 illustrative has the part of the media bed electric deionizer of stratification according to one or more embodiments of the invention in its at least one concentration compartments;
Fig. 3 illustrative comprises the part of the electric deionizer of the concentration compartments that at least one has dielectric area according to one or more embodiments of the invention;
Fig. 4 illustrative is according to the part of the system for handling of one or more embodiments of the invention;
Fig. 5 illustrative is according to the part of the electric deionizer of one or more embodiments of the invention, and it has at least one and is changed chamber to reduce virtual resistance (resistance) or improve distributions (current distribution) in other chamber;
Fig. 6 illustrative is according to the part of the electric deionizer of one or more embodiments of the invention, and it has the effective liquidate speed of increase in its at least one concentration compartments;
Fig. 7 A and 7B illustrative comprise the chamber that comprises the resin beads with different size according to the part of the electric deionizer of one or more embodiments of the invention; With
Fig. 8 shows the relation of the relative current temperature of Langelier saturation index value of current;
Fig. 9 A and 9B illustrative are right according to the concentrated and consumption chamber unit in the electric deion equipment of one or more embodiments of the invention, and wherein the chamber of Fig. 9 A demonstration comprises medium layer, and the chamber that Fig. 9 B shows comprises the floor and the district of medium; With
Figure 10 shows the performance according to the electric deionizer of one or more embodiments of the invention.
Describe in detail
The invention provides electricity and drive tripping device, such as but not limited to filled chamber electrodeionization (CEDI) equipment, as for example being disclosed in U.S. patent 4,632,745,6,649,037,6,824,662 and 7,083, those of 733 are incorporated the present invention into as a reference at this respectively.Especially, the embodiment that realizes one or more aspects of the present invention can be characterised in that in some cases and have low potentiality or the low possibility that forms incrustation scale.Although each side of the present invention presents by the embodiment that comprises electric deion equipment, these aspects of the present invention can be implemented in can helping to handle other electricity driving of fluidic with at least a non-required material or the tripping device that drives.Especially, related fields of the present invention can comprise the electric deionizer that is used for handling or removing from current or water body at least a dissolved substance.Therefore, each side of the present invention can advantageously provide and be configured or operate the electric deionizer that has the water of high incrustation scale potentiality with processing.
One aspect of the present invention can be implemented in exemplary shown in Figure 1, wherein schematically shows the part of electric deionizer 100.This electric deionizer generally includes at least one concentration compartments 112 and at least one consumes chamber 114, and their constitute unit to 115 and ionic communication mutually, and preferred and anolyte compartment 120 and cathode compartment 122 ionic communication be positioned between the two.In favourable embodiment of the present invention, this electric deionizer can comprise further that at least one can capture the isolated unit 130 of migration material.For example, electric deionizer 100 can have the isolated or temporary location (neutral cell) 130 and 132 adjacent to anolyte compartment 120 and cathode compartment 122.Isolated unit is generally electrode vessel provides buffer zone to isolate or to prevent that material from forming local incrustation scale.Electric deionizer produces hydroxide ion usually, can be in localized areas, and pH especially raises on point that electrolytic reaction is conducted electricity or surface.These localized areas, or even at the electrode vessel place, have obviously pH condition usually greater than fluid bulk.Because isolated unit is used in the process for the treatment of water these high pH zones are separated with the dirt material that becomes from the transmission of one or more consumption chamber, thereby suppress or reduce at least the potentiality of incrustation scale formation.As Fig. 1 exemplary illustration, electric deionizer 100 can comprise isolated unit 130, and it is with at least a precipitable component, as Ca
2+, with the component that contributes to incrustation scale formation, as OH
-Ion separates.Usually, one or more isolated unit 130 can be at least in part by allowing anionic species such as OH
-Migration also suppresses the anion-selective membrane 140A that cationic substance further moves in the adjacent chamber simultaneously and limits.According to shown in, isolated unit 130 can be provided with adjacent to concentration compartments 112.One or more these isolated unit also can further partly be limited by cation selective film 140C.Like this, for example, can suppress the component of precipitable compound, as Ca
2+, enter the chamber that has high pH regional area usually because the oxyhydroxide material generates, as electrode vessel 120.
Other embodiment of the present invention can comprise separate neutrality or light current from or ionisable substance at least, as, but be not limited to silica, SiO
2Isolated unit.Silica can precipitate from bulk liquid, if concentration is enough high or pH wherein takes place change, as when high pH changes to neutral pH.In electric deionizer, silica is removed under high pH usually in its state of ionization.The anolyte compartment 122 of one or more isolated unit 132 with ion isolation electric deionizer 100 can be set, wherein generate hydrogen ion and therefore can have low therein or the neutral pH liquid-flow.At silica by anion-selective membrane 140A from consuming after chamber 114 moves to concentration compartments 112, the isolated unit 132 that it is comprised high pH liquid-flow is therein caught and is suppressed and further moves in the low or neutral pH chamber with neutrality or nearly neutral pH, thereby reduces the possibility that aggregates into the silica incrustation scale.Unit 132 as unit 130, can be limited by cation selective film 140C and anion-selective membrane 140A at least in part.The precipitation that therefore isolated unit 132 can be used to capture the pH-settleable matter and prevent or suppress at least these materials.Isolated unit 132 also can comprise anionic exchange medium and cation exchange medium or both mixtures at least in part.In addition, one or more isolated unit can further comprise the assembling that can help electric deionizer or for example install inert media or other filler material that Ideal Characteristics such as resistance or flow distribution are provided in the operating process.Equally, the one or more mixtures that can comprise negatively charged ion and cation exchange medium at least in part in concentration compartments, consumption chamber and the electrode vessel.Really, the negatively charged ion in concentration compartments and electrode vessel and the mixture of cation exchange medium can leave selective membrane and further reduce the fouling potentiality by promoting the settleable matter transmission, and this has been avoided the gathering of contingent ionic species in the zone of chamber of using the active exchang medium of single kind or chamber.
In some embodiments of the present invention, the anolyte compartment can comprise the medium of being made up of the resistance to oxidation base material basically at least in part.Therefore, for example, the highly cross-linked ion exchange resin of weather resistance as commercially available resin cation (R.C.), can be used for wherein can existing the anolyte compartment of well-oxygenated environment.In addition, Zeo-karb can prevent or suppress chlorion and transfer to anode surface when being used for the anolyte compartment, and these materials can be converted to oxidisability chlorine at anode surface.
Apparatus of the present invention can handle hardness greater than 1mg/L (with CaCO
3Meter) and/or silica content greater than the water of 1mg/L, or both.Therefore, device of the present invention and technology are not limited to routine operation restriction, if be used for system for handling, can save the unit operation that at least one is intended to softening institute's water to be processed or removal silica.This advantageously can reduce capital and running cost, improves the reliabilty and availability and the capacity of system for handling simultaneously.For example, the system for handling of the present invention that comprises one or more electric deion equipments described herein can need not round trip reverse osmosis (RO) subsystem and treating water, simultaneously with adopt round trip RO equipment to compare the water with identical or suitable quality is provided with the system of before electric deion equipment, removing or reduce the concentration of the component that causes hardness and silica.
Others of the present invention can comprise electric deionizer, and it comprises that at least one consumes the chamber and/or at least one wherein comprises the concentration compartments of stratification medium.For example, one or more consumption chamber 112 of electric deion equipment 100 can comprise the first granular layer 112A, and it includes to small part and helps first target, the normally transmission of ionization material or the active media of migration.Consume chamber 112 and can further comprise second layer 112B, it includes the active media that helps first target substance and second target substance or both transmission at least in part.The first layer 112A can comprise the particle with first effective diameter, and second layer 112B can have the particle of second effective diameter.Further embodiment can be included in the 3rd floor 112C that consumes in the chamber 112.The 3rd layer of 112C can have activity or inert media, or both mixtures, and this medium has the 3rd effective diameter.Effective diameter can be the particulate minimum size.Perhaps, effective diameter can be all particulate mean diameters and be the calculated diameter with similar ball of comparable volume and surface-area.For example, the particulate effective diameter in the layer can be the function of ratio of particle volume and granule surface area or the mean value of particulate minimum size.In preferred configuration, the particulate effective diameter in the downstream layer is lower than the particulate effective diameter in the upstream layer.For example, the particle that constitutes layer 112C can be a spheroidal particle, and its effective diameter is greater than the particulate effective diameter that constitutes layer 112B.Optionally, the particulate effective diameter of formation layer 112A can be greater than the particulate effective diameter among layer 112B or the 112C.One or more concentration compartmentss can be by similar stratification.
In a preferred embodiment, the particulate effective diameter in the upstream layer is the size in gap between the downstream layer particle at least.In other embodiment, the effective diameter of upstream particle or minimum size are lower than the minimum size in the hole of the divider 160 of determining consumption chamber 112 outlet ports.Divider 160 can be to be used for medium is retained in indoor screen cloth.Therefore, the consumption chamber and the concentration compartments that comprise medium can have at least one divider respectively, make fluid therefrom flow through, and keep medium and its size simultaneously and are kept particulate medium layer in the upstream layer.
Usually the hole of design divider or opening have the resin of the about 500 μ m of diameter to about 700 μ m with reservation.Adopt configuration of the present invention, can use negatively charged ion and the Zeo-karb of size, the mass transfer dynamics when this has improved through this device less than hole dimension.In addition, less ion exchange resin can improve in indoor filling and reduce along locular wall channelizing or bypass mobile possibility.Closelypacked ball or almost the clearance space of spheroidal particle be about 0.414 times of the radius of a ball.Therefore, the effective diameter of upstream resin preferably is not less than this size.For example, the about 62 μ m of effective diameter can be used for having the upstream layer of about 300 μ m to the layer of the resin beads of about 400 μ m diameters to the fine mesh resin beads of about 83 μ m.Any floor can account for any suitable mark of chamber.Providing of desired properties is provided the degree of depth of upstream layer.In addition, favourable configuration is considered and will be had the resin cation (R.C.) bead of less effective diameter or size with using to help the cation transport activity than the macroanion resin beads.Noticeable arrangement is not limited to use the downstream media of reactive resin as the below, and the present invention can adopt inert media and implements in one or more downstream layers.
Interface between the layer can form the gradient of little and big resin beads.Therefore, the border between the layer need not to describe especially.In addition, other configuration can comprise the mixture of fine mesh resin beads and big resin.
Another aspect of the present invention can comprise electric deionizer, and it comprises that at least one wherein comprises the concentration compartments of stratification medium.As shown in Figure 2, electric deion equipment 200 can have at least one concentration compartments 214 and at least one consumption chamber 212.At least one concentration compartments 214 can have the first layer 215 and the second layer 216.Handling purer water relatively, as the RO penetrant, electric deion equipment in, current efficiency is usually less than 100%, this it is believed that it is because water splitting and the hydrogen that is generated and the transmission of hydroxyl ion.This can produce local pH fluctuation and can promote incrustation scale to form, thereby especially forms the place of carbanion formation lime scale at hydroxylated material and bicarbonate radical material or carbon dioxide reaction.
For example, in the typical electrical deionizer, bicarbonate ion shifts by the anion-exchange membrane near chamber inlet, but can be suppressed further migration from film.If the generation water splitting, transmission can form carbonate with the bicarbonate radical substance reaction by the hydroxylated material of anion-exchange membrane, and carbonate forms lime scale with the calcium reaction subsequently.
They form the place of incrustation scale not too easily by adopting layer, target substance can be directed to wherein in one or more concentration compartmentss.As shown in Figure 2, the layer 215 of anionic exchange medium can place around the inlet of concentration compartments 214, to promote the migration of bicarbonate radical material.By after the anion-exchange membrane 240A, it is promoted the resin anion(R.A) by layer 215 and is shifted to cation selective film 240C in the bicarbonate radical mass transfer.Even there is hardness ions to pass through cation selective film 240C, the fluidic pH around this film is also relatively low, and this has reduced the possibility that forms carbonate.
Other one or more floor 216 that consume chamber 212 and concentration compartments 214 can comprise blended anionresin and cation exchange medium.
Form in order further to reduce or to suppress incrustation scale, medium layer can be along the flow-path-length setting of concentration compartments.As shown in Figure 3, one or more upgrading units can comprise first district 314A of Ion Exchange Medium and the second district 314B of Ion Exchange Medium at least in part.First and second districts can maybe can be along the length linear distribution (represented) of chamber as border 350 the increasing or decreasing amount among district 315C and the 315D various Ion Exchange Mediums gradient and described by gradient boundaries 351.First or second district can comprise anionic exchange medium or cation exchange medium, or by or constitute by anionic exchange medium or cation exchange medium basically.For example, district 314A can comprise cation exchange medium so that comprise the district 314B and the cation selective film 340C substantial barrier of anionic exchange medium.Substantial barrier is meant, in some cases, so that isolated area comprises certain type medium or is made of certain type medium, this medium can be negatively charged ion, positively charged ion or inert between district and film.
In some cases, first district or second district can be the mixtures of the various Ion Exchange Mediums of different amounts.For example, district 315C can comprise the cation exchange medium adjacent to cation selective film 340C, by or constitute by this medium basically, district 315D can comprise anionic exchange medium, by or constitute by this medium basically, wherein the amount of the relative cation exchange medium of amount of anionic exchange medium makes that along flow-path-length or lengthwise dimension increase or decline the border between the district is determined by gradient boundaries 351.In another embodiment, the 3rd dielectric area (not shown) can be between first and second districts.The 3rd district can comprise inert media, cation exchange medium, anionic exchange medium, blending agent or its mixture, or by or constitute by above-mentioned medium basically.In addition, one or more screen clothes can use between the district or in the district to help to fill the chamber of this device, and this also can improve flow distribution and further suppress incrustation scale and form in operating process.Also can help assembling and filling by the medium that adopts binding agent to fix each district.For example, the medium in first district can mix with water-soluble binder such as starch.Mixture can be placed in the chamber subsequently.Second mixture of the medium in second district can similar preparation and is arranged in the chamber.
District 314B helps anionic species, and anion-selective membrane 340A is left in transmission as bicarbonate ion, and district 315C helps cationic substance, and anion-selective membrane 340C is left in transmission as calcium ion.Therefore these isolated areas are reduced in the possibility of film surface incrustation scale formation on every side.
As shown in Figure 3, consume the chamber and can comprise the first medium layer 312A, the second medium layer 312B and, optionally, the 3rd medium layer 312C.The first layer can comprise the mixture of anionic exchange medium, cation exchange medium or inert media.The second layer can comprise anionic exchange medium or inert media or its mixture or be formed or be made up of it basically by it.The 3rd layer can comprise anionic exchange medium, cation exchange medium, inert media or its mixture or formed or be made up of it basically by it.
Others of the present invention comprise system and the technology of change pH of mobile logistics at least one concentration compartments of electric deionizer.The pH of logistics can be lowered by producing and add acidic solution in one or more enriched materials and electrode vessel, to reduce the possibility that incrustation scale forms.Acidic solution can be by adopting electrolysis unit to produce or preparing.Further, incrustation scale inhibition or tolerance can realize by the degassing of enriched material liquid.Can use any sour generation component, as can be available from those of the Dionex company of California Sunnyvale.
Usually, electric deion equipment can be handled the liquid with soft.The feed water that this restriction will be fed to electric deion equipment is limited to 1ppm or lower firmness level, in lime carbonate.In order to handle the water of hardness value, must use pretreatment technology such as round trip RO or RO post softening agent greater than 1ppm.Additional pretreatment unit operation increases system complexity and cost and refuse.But electric deion equipment of the present invention can reliably be located in the water that reason has higher hardness, thereby elimination or reduction are to the dependency of these pretreatment operation.
The known concentration compartments of electrodialysis appts that acidic solution is added is to reduce calcium deposit; But in fact acidic solution is not added electric deion equipment, because the logistics flow velocity in the enriched material chamber, especially thick element cell is low.In addition, need the acid of a large amount usually.As shown in Figure 4, system for handling 400 of the present invention can comprise electrochemical apparatus 435 generate be introduced into be arranged to from the source 411 receive chamber, the acid solution of concentration compartments 414 normally of electric deion equipment 445 of water to be processed.A part for the treatment of product water from electric deion equipment 445 can be used for promoting to produce acid solution in the acid generation chamber 472 of electrochemical apparatus 435.At least a portion treating water can be transferred into and use point 413.Can be introduced into electrolysis unit 435 from the source 462 of the bag saliniferous salt brine solution of for example tenderizer brine tank generates to promote acid solution.Electrochemical apparatus 435 can be the part of electric deion equipment 445.Salt brine solution comprises sodium-chlor usually.
In some cases, acidic solution can be introduced into one or more consumption of electric deion equipment 445 and concentration compartments 412 and 414 and electrode vessel.Preferably, the add-on of acidic solution makes the pH of the logistics solution of leaving away leave described chamber between about 2.5 to 4.3 units.Further embodiment can comprise the one or more logistics of neutralization from electric deion equipment 445.For example the basic solution that generates by the chamber 472 of electrolysis unit 435 can be merged with in and the outlet logistics that has low pH usually of concentration compartments 414, be disposed to discharge outlet 463 or environment then.
The enriched material logistics degassing that is used for removing carbonic acid gas can further reduce or eliminate the precipitation potentiality of concentration compartments.The degassing can be by adding degassing equipment or realizing by membrane process or other method.If adopt acidic solution in the concentration compartments, the degassing can be correlated with, can be to returning the carbon dioxide that diffuses through film and reduce quality product because might form.In addition, logistics flowing in the chamber can be adverse current to help gas to remove.
Use pump and optionally use jar recirculation enriched material chamber further to strengthen the incrustation scale restraining effect by acidifying as herein described and degassing technology.
Element of the present invention, setting and technology also are provided at improved distribution of current in the electric deion equipment.As Fig. 5 illustrative, can be characterized by a series of chambers resistance 573,575 and 577 by the resistance of electric deionizer 500 between electrode 520 and 522, their representatives consume and concentration compartments 512 and 514, with be characterized by membrane resistance 584,586 and 588, they represent anion-selective membrane 540A and cation selective film 540B.Run through electric deionizer 500 improved distribution of current can by adopt at least one its realize to the virtual resistance 580 of small part concentration compartments 516 greater than the virtual resistance of other chamber such as concentration compartments.
The virtual resistance of chamber or its part can change by mixed inert resin beads in the concentration compartments or low conduction or non-conducting material.Optionally increase virtual resistance and realized passing through the more uniform distribution of current of other chamber.Reduce the variation that runs through the electric current that consumes the chamber and for example can improve overall performance.
In electric deion equipment, resistance can be depending on the kind of the medium in this equipment and the activity chemistry form of these media, that is, which kind of ion is just moving through medium.In stratification bed chamber, resistance changes between different layers usually, because the form of the kind of resin and resin is different.Usually, strong band isoelectric substance or ion are excited, and water splitting phenomenon and weak ion propulsion take place subsequently.Therefore, the dielectric resin of the inlet of close chamber can exchange with the target substance in the reinforced water, and the medium great majority of close outlet are hydrogen and hydroxide form.Usually, most of strong band electron ion must be removed, if if reinforced concentration and/or mobile enough height or electric current are enough low, this may not can realize.
If the resistance in the chamber can the floor in the chamber between or change along the length of bed, therefore current density also can change so.But the resistance by whole assembly may not only depend on the resistance that consumes the chamber.Consume chamber and film and can or also can be along concentration compartments that its length generation resistance changes with electrode vessel is electric does not connect.If the resistance of consumption chamber is the sub-fraction by the total electrical resistance of assembly, even so this resistance noticeable change, total electrical resistance can be more even by other factors decision and distribution of current.If compare other resistance height but consume chamber resistance, then distribution of current is subjected to consuming the influence of indoor resistance difference.
The typical electrical deionization apparatus is combined with the concentrated and/or electrode vessel that screen cloth is filled.In these configurations, in most of the cases obviously greater than the resistance of resin in consuming the chamber, therefore, distribution of current is not generally consumed the control of the resistance of chamber to the resistance of water in these chambers.Fill to concentrate and electrode vessel and use than the low resistance ion-exchange membrane and obviously reduce overall assembly resistance with resin.But in some cases, this can cause uneven distribution of current, because the resistance decision that the electrical component resistive is served as reasons and consumed the chamber.
Therefore in some embodiments of the present invention, the concentrated and electrode vessel of screen cloth filling can be tried one's best and at utmost be reduced uneven distribution of current.But in using behind most of RO, glassware for drinking water has low-down electric conductivity, causes high assembly resistance.This high resistance further produces restriction, if there is the electromotive force limitation.On the contrary, the present invention need not salt solution is injected the logistics that flows into the concentration compartments and suitable performance is provided, and reduces running cost and process complexity like this.
Can notice, one or more concentrate and/or electrode vessel in the mixed inert resin can be increased in resistance in these chambers as filler, improved distribution of current like this by assembly.As shown in Figure 5, one or more concentration compartmentss 516 can comprise inert plastic so that the higher virtual resistance 580 that therefrom passes through to be provided, and this has determined the set resistance of other chamber and film.Because dominant resistance control total electrical resistance rate, the watt current by other chamber distributes and becomes more even.The amount of inert plastic can be changed to increase virtual resistance and to change the distribution of current of passing through this device.Inert plastic also can be used for one or more concentrate and electrode vessel in layer increase with the part and wherein dilute resistance and be confirmed as resistance in some low part.Therefore, as shown in Figure 5, can be by distinguishing 512 distribution of current by in chamber 515, adopting the higher electric resistivity floor to make the virtual resistance 573 of floor of chamber 515 increase to mate or make it to be equivalent to electric current by the district 511 of installing.But can determine by the virtual resistance of measuring the relative inertness resin demand on the amount experience of resistance.
Other material with low electrical conductivity, as polymer mesh or filamentary material, can be used for increasing along with the resistance of inert plastic bead.
Electric deionizer can be restricted to the rate of recovery of maximum 90-95% in case limited solubility material in the reinforced water such as hardness and silica form incrustation scale.If reinforced water comprises these materials of very low amount, this equipment should be able to be operated under higher recovery.Some aspect of the present invention comprises electric deionizer, and it has a plurality of approach by its concentration compartments, thereby the rate of recovery is provided.The multipass configuration helps to keep the speed of being scheduled to and need not recirculating pump and loop.But the present invention can be preferred for having the occasion of recirculation loop, and wherein reinforced water concentration is low and need the very high rate of recovery in order to avoid waste or discharge high-purity water and/or increase replenish the operating time of system.In some embodiments of electric deionizer of the present invention, rate of flow of fluid is enough to reduce and produces dead volume, channelizing and in the possibility of indoor local superheating.For example, the required rate of flow of fluid in the chamber can be at least about 2 gallon per minute/square feet in the concentration compartments.Other rate of flow of fluid can be depending on other factors, includes but not limited to precipitate the component concentrations of compound, fluidic temperature and fluidic pH.Can induce channelizing than low rate.
The part of Fig. 6 illustrative electric deionizer 600 is included in consumption chamber 614 and concentration compartments 612 between electrode vessel 630 and 632.This arrangement and configuration in treatment unit of the present invention and system, provide one consume the chamber by way of with relevant a plurality of concentration compartmentss approach.These configurations make and can be increased in rate of flow of fluid in the concentration compartments, 5 times of the preferred the highest flow velocity that is increased to one way equipment.As shown in Figure 6, the water in source 615 is introduced concentration compartments 612 in proper order with guiding downstream concentration chamber 612B and subsequently to chamber 612C with to discharge outlet or to downstream unit operations 625.
Water to be processed be introduced into and consume chamber 614 and guiding and use point and need not to follow or follow the trail of flowing of water by chamber 612,612A and 612B.But the present invention does not limit with respect to the relevant concentration compartments volume number that consumes chamber volume number, and any ratio of concentration compartments and consumption chamber can be used for providing the required high rate of flow of fluid by the chamber.
The transfer rate that different sized cation in mixolimnion or the chamber and anion exchange resin beads can be used for further reducing than the macrobead counter ion is transmitted than the beads counter ion with helping.
Ion transport occurs by ion exchange resin usually.Therefore successful transmission can depend on whole paths of the similar substance between bead and the film.Cationic substance is diffused on the resin cation (R.C.) bead usually and negative electrode is shifted in the path of often following cationic medium, arrives cation selective film and feeds the concentration compartments until its.If interrupt in the path, cationic substance must diffuse out and enter bulk solution from last bead, and it the chance of (end up) appears in chance of in bed it having been picked up after therefore having reduced and increase in product water.This path can badly make bead not have excellent contact and interrupts because of filling, or it can interrupt because of the bead oppositely charged.
Use thin relatively unit or tight potting resin can increase the possibility that keeps desired paths.Positively charged ion and anionite-exchange resin that employing has the relative uniform-dimension of class Sihe also increase the possibility that keeps desired paths.But use the positively charged ion and the anionite-exchange resin transfer capable of blocking of different size.
In some cases, can advantageously suppress positively charged ion or anionic transmission.By optionally reducing the size of a kind of type of resin in the mixed bed, be enhanced owing to path more completely than the transfer of beads counter ion, and be delayed owing to path not too completely than the transfer of macrobead counter ion, because along with than the size of beads near a certain mark than the size of macrobead, less resin beads often is filled in than around the macrobead, this separation and interrupting from a macrobead to Next path.This phenomenon also can be depending on the relative ratios of big and small ion exchange resin bead.For example, the mixture of 50 volume % beads obviously is different from the mixture of 25 volume % or 75 volume % beads to the influence of ion transport.
In case the size of medium and mixture ratio are selected suitably to slow down target or selected type ionic transmission and increase different types of transmission, hydrogen or hydroxyl ion must be transferred to keep electric neutrality.For example, if the bed of being made up of resin cation (R.C.) is used for consumption chamber shown in Fig. 7 A basically, cationic substance can move by cation exchange resin beads grain 731 and cationic membrane 740C and enter adjacent concentration compartments.Water can split in 766 punishment of the position of anion-selective membrane 740A, produces hydrogen ion and consumes the cationic substance migration of chamber (not shown) to move to adjacent concentration compartments's neutralization from another to substitute the migration positively charged ion that consumes in the chamber and to produce hydroxyl ion.This phenomenon depends on the ability of division water on the surface of anionic membrane, and the contact area between less anionic membrane and the positively charged ion bead is arranged herein.Adopt less cation exchange resin beads grain 733 and, shown in Fig. 7 B, reduced the transfer rate of anionic species than macroanion exchange resin bead 734.In addition, the use of different resins bead size provides additional water splitting position 766 on the tangent line between Zeo-karb 733 and the anion exchange resin beads 734, and this improves performance by the resistance that reduces by assembly again.
For example, electric deionizer of the present invention can comprise the chamber of the mixture of anion exchange resin-containing and Zeo-karb, and the mean diameter of described Zeo-karb is at least 1.3 times of mean diameter of anionite-exchange resin.Perhaps or in addition, electric deionizer can comprise the chamber of the mixture of anion exchange resin-containing and Zeo-karb, the mean diameter of described Zeo-karb is at least 1.3 times of mean diameter of anionite-exchange resin.
Embodiment
The function of these and other embodiment of the present invention and advantage can further be understood according to following examples, and these embodiment illustrate the benefit of one or more systems of the present invention and technology and/or advantage but do not exemplify four corner of the present invention.
Embodiment 1
This embodiment describes the influence of temperature to Langelier saturation index (LSI).
Calculating LSI value known in the art is used to measure the potentiality that incrustation scale forms.LSI is pH, total dissolved solidss (TDS), temperature, the function of total hardness (TH) and basicity.Use following assessment for these parameters of concentration compartments's logistics of electric deionizer, the stream temperature of LSI value can be determined with representative relationship and provide in Fig. 8 relatively, based on having pH9.5 unit, and TDS 30ppm, TH 15ppm is with CaCO
3Meter and the about 25ppm of basicity are with CaCO
3The logistics of meter.
If the LSI value of logistics is positive, fouling often takes place.In order to suppress fouling, the LSI value of logistics is reduced to and is preferably negative value.Fig. 8 shows that along with temperature descends, the LSI value is brought down below zero about 12.5 ℃.Therefore, for above-mentioned condition, the logistics that enters the concentration compartments of electric deion equipment is cooled to is lower than 12.5 ℃ of possibilities that should be able to reduce or prevent to form incrustation scale.
Cooling can be undertaken by upstream heat coupling heat exchanger or the water cooler at electric deionizer.Can use other element and the subsystem that help from the one or more logistics that enter this device, to remove heat energy.For example, one or more transmitters and controller can be used for determining temperature control loop and impel stream temperature is retained to target temperature or even reduces to required effective LSI value or aim parameter.
Target temperature can be by determining to be introduced into the electric deion equipment concentration compartments logistics temperature and experience ground is determined, or calculate based on the LSI value that calculates at least in part.For example, the target temperature established of experience can be with or without do not observe fouling under the situation on other border on the history temperature to guarantee that fouling is further suppressed.LSI base target temperature can be determined based on deutero-LSI-temperature relation, calculates the relevant target temperature of setting decline with the LSI value subsequently.
Embodiment 2
In this embodiment, research resin beads size is to the Effect on Performance according to the electric deionizer of one or more aspects of the present invention.
In a test, the electrodeionization assembly makes up by the resin anion(R.A) of the average bead diameter 575 μ m of use in consuming the chamber and the equal portions mixture of the resin cation (R.C.) of average bead diameter 350 μ m.These resins all have the single-size size according to industrial standards.
Assembly is added into prior with reverse-osmosis treated with comprise about 0.5ppm Mg and 1.5ppm Ca (all with CaCO
3Meter) and the water of pH about 6.1.Assembly is almost being operated under 100% current efficiency, and quality product is about 1-2M Ω-cm, does not have almost zero silica removal.
Product water hardness level is lower than that (＜the detected value and the pH that 10ppb) measure is reduced to about 5.7 by the Hach spectrophotometer.This shows that this assembly is just preferentially removed positively charged ion but not negatively charged ion.
Embodiment 3
In this embodiment, research has which floor electric deionizer of different bead size to Effect on Performance according to the one or more aspects of the present invention in its chamber.
Assembly makes up by use three leafing sub-exchange resins in consuming the chamber.First and final layer form by the positively charged ion with the about 600 μ m of single-size diameter and the uniform mixture of resin anion(R.A).The middle layer is made up of the cationic exchange with particle diameter 150-300 μ m and the uniform mixture of anionite-exchange resin.The assembly partition has the slit in fluidic distributor, is used for the resin fix in position, and its width is 254 μ m.Assembly is operated some months under the situation that does not change pressure drop, show in the middle layer some less than the resin in partition hole not by the resin bottom with leave assembly.
In addition, the adding in the middle layer of less resin has improved suitable electric deion equipment, the contrast assembly, performance.This assembly and another electrodeionization assembly parallel running, the chamber of back one assembly comprises the cationic exchange of the about 600 μ m of particle diameter and the uniform mixture of anionite-exchange resin.Use having the about 30 μ S/cm of electric conductivity and comprising 3.75ppm CO with reverse-osmosis treated in advance
2Reinforced water, the assembly that comprises the layer of less ion exchange resin generates the water of resistivity 16.4M Ω-cm, does not have another typical components of the layer of less ion exchange resin then to generate the water of resistivity 13.5M Ω-cm.In addition, the assembly that comprises the layer of less exchange resin demonstrates 96.6% silica removal, and the contrast assembly is 93.2%.
Embodiment 4
In this embodiment, research has the electric deionizer of the several or a plurality of strokes by its concentration compartments to Effect on Performance.
The electrodeionization assembly consumes the chamber by four, three concentration compartmentss and two electrode vessel assemblings.
All consumption chambers are by reinforced with water to be processed in parallel to each other.
Concentration compartments and electrode vessel are connected to feed in raw material makes the logistics that is introduced into the concentration compartments at first enter cathode compartment, and order flows through the concentration compartments and passes through the anolyte compartment at last subsequently.This is different from conventional configuration, and wherein current are fed to electrode vessel usually, and current enter the concentration compartments simultaneously.Therefore assembly has five effective concentration compartments approach.
The performance data (being designated as the parallel enriched material ＂ of ＂) of the standard package of data of this assembly (being designated as ＂ series enriched material ＂) and the operation of use split flow is listed in following table 1.Data show, by order logistics are set and concentrate and electrode vessel to flow through, when rate of flow of fluid is similar to operation under obviously lower defective flow velocity.Therefore can in enriched material, keep minimum speed to obtain the very high rate of recovery simultaneously.
Table 1 has the assembly and the comparison with assembly of five strokes of one way enriched material.
| Assembly | Parallel enriched material | The series enriched material |
| Reinforced, μ S/cm | 30.3 | 30.3 |
| Resistance, ohm | 4.3 | 4.2 |
| Quality product, M Ω-cm | 3.1 | 3.6 |
| Product flows, gpm | 2.25 | 2.25 |
| Enriched material flows, gpm | 7.2 | 1.2 |
| The rate of recovery, % | 94.9 | 99.1 |
| Enriched material speed, gpm/ft 2 | 2.0 | 1.7 |
In this embodiment, in the research concentration compartments electric deionizer of band level and perpendicular layers to Effect on Performance.
Two assemblies use as Fig. 9 A and the different layer configuration assembling shown in the 9B.Each assembly by four repeating units that illustrated respectively to forming.In the drawings, ＂ MB ＂ is meant mixture or resin; ＂ A ＂ and ＂ C ＂ are meant district or the floor that comprises anionite-exchange resin and Zeo-karb respectively; ＂ AEM ＂ and ＂ CEM ＂ are meant anion-selective membrane and cation selective film.Assembly uses reinforced water 2 and 3 weeks of operation that have the about 10 μ S/cm of electric conductivity and comprise 2ppm total hardness (in lime carbonate) respectively.
After this time, they are opened, do not observe incrustation scale.On the contrary, consume and the concentration compartments in comprise mixed bed resin non-stratification assembly after identical reinforced water operation 2 is all on the anionic membrane in enriched material incrustation scale appears.
Embodiment 6
In this embodiment, research in its chamber band perpendicular layers and the electric deionizer that is added with acidic solution to Effect on Performance.
Three assemblies are assembled into to be had horizontal stratification and along flow-path-length vertical orientated district or floor are arranged in the concentration compartments in the concentration compartments.Isolated unit is set in addition adjacent to two electrode vessels.Reinforced water was operated 90 days after assembly used the RO that comprises about 2ppm total hardness.Acidic solution is injected the concentration compartments, and the feasible pH that leaves the current of concentration compartments of rate of injection is about 2.5-3.5.
Figure 10 has provided stable performance in whole 90 days.In the drawings, ＂ FCE ＂ is meant reinforced electric conductivity equivalent, its by the reinforced electric conductivity (μ S/cm) with reality add reinforced carbonic acid gas (ppm) multiply by 2.67 and reinforced silica (ppm) multiply by 1.94 and calculate; The reinforced TH ＂ of ＂ is meant reinforced total hardness.
The controller of system of the present invention can use one or more computer architectures and realize.Computer architecture can be, for example, multi-purpose computer is as based on Intel PENTIUM
The type treater, Motorola PowerPC
Treater, Sun UltraSPARC
Treater, Hewlett-PackardPA-RISC
Treater, or those of any other type processor or its combination.Perhaps, computer architecture can comprise the special purpose hardware of separate procedureization, and for example, application specific type unicircuit (ASIC) or expection are used for the controller of analysis system.
Computer architecture can comprise the one or more treaters that are connected to usually on one or more holder equipment, and it can comprise, for example, any or multiple disc driver internal memory, flash memories equipment, RAM holder equipment, or be used for the miscellaneous equipment of storage data.Holder is usually used in stored routine and data in system for handling and/or computer architecture operating process.Software comprises the programming code of implementing embodiment of the present invention, can be stored in computer-readable and/or can write on the nonvolatile recording medium, and be copied to usually subsequently in the holder, and wherein it can be carried out by treater subsequently.The element of computer architecture can connect by interconnection mechanism, and it can comprise one or more buses (as being integrated between the interior element of same equipment) and/or network (as between the element on the different discrete device).Interconnection mechanism can make usually exchange message between the element of computer architecture (as, data, instruction).Computer architecture also can comprise one or more input units, keyboard for example, and mouse, the cursor ball, microphone, touch screen and one or more output equipment, for example, printing equipment, display screen, or loud speaker.In addition, computer architecture can comprise one or more interfaces, and it can be connected to computer architecture on the network of communication and (substitute except that the network that can form by one or more elements of computer architecture or as it).
According to one or more embodiments of the present invention, one or more input unit can comprise the transmitter that is used for measuring parameter.Perhaps, transmitter, metering valve and/or pump, or these all assemblies can be connected to operability and be connected on the connected network that computer body fastens.Controller can comprise one or more computer storage media such as readable and/or can write nonvolatile recording medium, wherein can store the signal that is used for determining the program carried out by one or more treaters.Storage medium can for example be disk or flash memory.Although computer architecture can be one type a computer architecture can realizing each side of the present invention, should be appreciated that, the invention is not restricted to fasten realization exemplifying the software or the computer body that provide.Really, replace for example implementing on the multi-purpose computer system, controller or its element or branch can use as specialized system or as special-purpose programmable logic controller (PLC) or on the hierarchy of control of distributing in addition.In addition, should be appreciated that one or more characteristics of the present invention or aspect can be at softwares, hardware or firmware, or realize in any its combination.For example, but one or more parts of the algorithm that controlled device is carried out can on different computers, carry out, these computers can pass through one or more network-in-dialings again.
Those skilled in the art should be appreciated that parameter as herein described and configuration are exemplary, and actual parameter and/or configuration depend on the specific occasion of using system of the present invention and technology.Those skilled in the art it should further be appreciated that or can use normal experiment to confirm the equivalent of particular of the present invention at the most.Therefore, embodiment as herein described is appreciated that to only providing as an example, and in the scope of claims and equivalent thereof; Other modes outside the present invention can specially describe realize.
Be also to be understood that each characteristic as herein described, the system of the present invention relates in addition, subsystem, or technology and two or more characteristics described herein, system, as long as subsystem, or any combination of technology are these characteristics, system, subsystem and technology be contradiction not mutually, so two or more characteristics, system, subsystem, and/or any combination of method is considered to embody within the scope of the present invention in claim.In addition, the behavior of when relating to an embodiment, discussing, element and characteristics have no intention to be excluded outside the similar in other embodiments role.
Many ＂ of term ＂ used herein are meant two or more items or element.No matter in parts such as specification sheets or claim, term ＂ comprises ＂, ＂ and comprises that ＂, ＂ carry ＂, ＂ and have ＂, ＂ and contain ＂ and ＂ to relate to ＂ all be open-ended term, means that promptly ＂ includes but not limited to ＂.Therefore, the use of these terms means and is included in project and the equivalent of listing thereafter thereof, and other project.Only change word ＂ by ... form ＂ and " basically by ... form " be respectively sealing or semiclosed transformation word when relating to claim.The ordinal number term such as ＂ the one ＂, ＂ the 2nd ＂, ＂ the 3rd ＂ and the similar terms itself that are used to modify the claim key element in the claim do not mean that any preferential, precedence, or claim key element order of another key element or the interim order of wherein carrying out a kind of behavior of method relatively, but the claim key element being used for having a certain title of only serving as a mark be different from have identical title another key element (but in order to use the ordinal number term) to distinguish these claim key elements.
The U.S. temporary patent application series No.60/805 that is entitled as ENHANCED HARDNESS TOLERANCEOF CEDI MODULES that on June 22nd, 2006 submitted, on June 22nd, 505 and 2006 submitted is entitled as the U.S. temporary patent application series No.60/805 of METHODS TO REDUCE SCALING IN EDI DEVICES, and 510 incorporate the present invention into as a reference at this.
Claims (64)
1. have the electric deionizer of anolyte compartment and cathode compartment, it comprises: the first consumption chamber between anolyte compartment and cathode compartment; With the concentration compartments that consumes the chamber ionic communication; Consume the chamber with second of concentration compartments's ionic communication; And in the first consumption chamber and anolyte compartment and cathode compartment, completely cut off the unit between at least one and with first of their ionic communication.
2. the electric deionizer of claim 1, wherein the first isolated unit to small part is determined by consuming the cation selective film that the chamber is provided with adjacent to first.
3. the electric deionizer of claim 2, wherein the first isolated unit to small part is determined by anion-selective membrane and adjacent to the cathode compartment setting.
4. the electric deionizer of claim 3, wherein the first isolated unit comprises the medium layer of the mixture that contains anionic exchange medium and cation exchange medium.
5. the electric deionizer of claim 4, wherein cathode compartment comprises the mixture of anionic exchange medium and cation exchange medium.
6. the electric deionizer of claim 1 comprises further and the second isolated unit of the second consumption chamber ionic communication that wherein the second isolated unit consumes between the chamber in anolyte compartment and second.
7. the electric deionizer of claim 6, wherein the second isolated unit to small part is determined by consuming the anion-selective membrane that the chamber is provided with adjacent to second.
8. the electric deionizer of claim 7, wherein the second isolated unit further comprises the cation selective film that is provided with adjacent to the anolyte compartment.
9. the electric deionizer of claim 8, wherein the second isolated unit comprises the medium layer of the mixture that contains anionic exchange medium and cation exchange medium.
10. the electric deionizer of claim 8, wherein the anolyte compartment comprises cation exchange medium.
11. electric deionizer, it comprises: consume the chamber; With with first concentration compartments that consumes the chamber ionic communication, it is determined by anion-selective membrane and cation selective film to small part, and described first concentration compartments to small part comprises first district that is made of cation exchange medium basically that separates with anion-selective membrane basically by second district that is made of anionic exchange medium basically.
12. the electric deionizer of claim 11, further comprise and second concentration compartments that consumes the chamber ionic communication, described second concentration compartments to small part is determined by cation selective film and anion-selective membrane and comprises first part that contains Ion Exchange Medium and the second section that contains Ion Exchange Medium that this first and second part is vertical fragment of partially filled second concentration compartments respectively.
13. the electric deionizer of claim 12, wherein first part mainly is made up of cation exchange medium and is provided with adjacent to the cation selective film of second concentration compartments.
14. the electric deionizer of claim 13, wherein second section is made up of anionic exchange medium basically and is separated basically by the first part of cation exchange medium and the cation selective film of second Room.
15. the electric deionizer of claim 11, wherein at least one in first and second concentration compartmentss further comprises the electrochemistry inert media.
16. the electric deionizer of claim 11 further comprises the acidic solution source that is communicated with the inlet fluid of first concentration compartments.
17. the electric deionizer of claim 11, wherein cation exchange medium comprises weakly acidic cationic exchanger resin.
18. the electric deionizer of claim 11, wherein anionic exchange medium comprises weak basic anion exchange resin.
19. electric deionizer comprises:
Consume the chamber;
With first concentration compartments that consumes the chamber ionic communication, described first concentration compartments comprises the medium with first virtual resistance; With
With second concentration compartments that consumes the chamber ionic communication, wherein a part of second concentration compartments comprises the medium that has greater than second virtual resistance of first virtual resistance.
20. the electric deionizer of claim 19, wherein the virtual resistance of at least a portion second concentration compartments is at least 2 times of first virtual resistance.
21. the electric deionizer of claim 19, wherein second concentration compartments comprises inert media.
22. electric deionizer, it comprises: consume the chamber; With with the concentration compartments that consumes the chamber ionic communication, described concentration compartments comprises the mixture of anionite-exchange resin and Zeo-karb, and wherein anionite-exchange resin and the Zeo-karb amount in mixture is with respect to the flow-path-length of concentration compartments and change.
23. the electric deionizer of claim 22, wherein the relative quantity of anionite-exchange resin is along the flowing-path of concentration compartments and increase.
24. the electric deionizer of claim 22, wherein the relative quantity of Zeo-karb is along the flowing-path of concentration compartments and increase.
25. have the electric deionizer of at least one chamber, at least one outlet port of described chamber is determined by the divider with a plurality of holes, this device comprises: be the first layer particle in the chamber on boundary with the ion selective membrane, described particle comprises the medium of first effective diameter with the minimum size that is lower than described hole; With the second layer particle in the chamber in the first layer downstream, described second layer particle has greater than described first effective diameter with greater than second effective diameter of the minimum size in described hole.
26. the electric deionizer of claim 25 further comprises the 3rd layer of particle that is positioned at the first layer particle upstream.
27. the electric deionizer of claim 26, wherein the 3rd layer of contained particle has and the about identical effective diameter of the particle of the second layer.
28. the electric deionizer of claim 25, wherein the second layer comprises ion exchange resin.
29. the electric deionizer of claim 25, wherein the first layer comprises ion exchange resin.
30. the electric deionizer of claim 25, wherein the 3rd layer comprises ion exchange resin.
31. the electrodeionization system comprises: water source to be processed; Comprise the processing components that consumes chamber and concentration compartments, this processing components fluid is connected on the institute water source to be processed; Comprise that acid generates the electrolysis unit of chamber, this electrolysis unit fluid is connected the upstream of concentration compartments; The acid that is connected to electrolysis unit with fluid generates the salt brine solution source of the inlet of chamber.
32. the electric deionizer of claim 31, the outlet fluid that wherein consumes the chamber is connected to the inlet that acid generates the chamber.
33. the electric deionizer of claim 32, wherein electrolysis unit further comprises the alkali generation chamber that generates the chamber ionic communication with acid.
34. the electric deionizer of claim 33, wherein the outlet fluid of concentration compartments is connected to the outlet that alkali generates the chamber.
35. electric deionizer, it comprises the chamber of the mixture of anion exchange resin-containing and Zeo-karb, and the mean diameter of described anionite-exchange resin is at least 1.3 times of Zeo-karb mean diameter.
36. electric deionizer, it comprises the chamber of the mixture of anion exchange resin-containing and Zeo-karb, and the mean diameter of described Zeo-karb is at least 1.3 times of anionite-exchange resin mean diameter.
37. water treatment system comprises:
Water source to be processed;
Comprise a plurality of concentrate and consume chamber and fluid be connected to the electric deionizer at water source to be processed;
The water cooler that is communicated with the hydro-thermal of at least one concentration compartments that will be introduced into electric deionizer;
Be configured to provide the transmitter of the temperature demonstration of at least a water in water that will be introduced in the concentration compartments and the water that leaves the concentration compartments; With
Being designed to receive described temperature demonstration and producing promotes cooling will be introduced into the controller of the signal of the water in the concentration compartments.
38. the water treatment system of claim 37, its middle controller be designed to regulate to be introduced into the water in the concentration compartments temperature to target temperature.
39. the water treatment system of claim 38, its middle controller is designed to calculate the water that is introduced into the concentration compartments and leaves effective Langelier saturation index (LSI) value of at least a water in the water of concentration compartments, and is worth target temperature based on the LSI that is calculated to small part.
40. electric deionizer comprises: to the consumption chamber that small part is determined by cation selective film and anion-selective membrane; With determine by anion-selective membrane to small part and comprise the first layer anionic exchange medium and be positioned at the concentration compartments of the second layer medium in the first layer downstream that the described second layer comprises anionic exchange medium and cation exchange medium.
41. the electric deionizer of claim 40, wherein the second layer comprises first district that comprises cation exchange medium that second district by comprising anionic exchange medium separates with anion-selective membrane basically.
42. the electric deionizer of claim 40, wherein the second layer is positioned at the downstream of the first layer.
43. the method for the treatment of water in having the electric deionizer that consumes chamber and concentration compartments comprises: measure the logistics in the concentration compartments temperature, to be introduced into the temperature of the logistics in the concentration compartments and leave one of the temperature of the logistics of concentration compartments; Reduction will be introduced into the temperature of the water in the concentration compartments to preset temperature; Institute's water to be processed is introduced the consumption chamber; With remove in the electric deionizer at least a non-required material of at least a portion in the water to be processed.
44. the method for claim 43 comprises that further the temperature of the logistics that will be introduced into the concentration compartments remains on target value.
45. the method for claim 44, further comprise determine to be introduced into the logistics of concentration compartments and leave in the logistics of concentration compartments at least a Langelier saturation index (LSI) value and to small part based on described LSI value and definite target value.
46. the method for the treatment of water in electric deionizer comprises: the consumption chamber that will have the water introducing electric deionizer of negatively charged ion and cationic substance; Promote at least a portion cationic substance to be transferred in the first isolated unit between the cathode compartment that consumes chamber and electric deionizer; With
Promote at least a portion anionic species to be transferred in the second isolated unit between the anolyte compartment that consumes chamber and electric deionizer.
47. the method for claim 46 wherein promotes transmission at least a portion cationic substance to comprise that the inhibition cationic substance is transferred to the cathode compartment from the first isolated unit.
48. the method for claim 47 wherein promotes transmission at least a portion anionic species to comprise that the inhibition anionic species is transferred to the anolyte compartment from the second isolated unit.
49. the method for claim 48 comprises that further at least a portion is left the water that consumes the chamber to be introduced in cathode compartment and the anolyte compartment at least one.
50. the method for claim 46 further comprises keeping passing through the rate of flow of fluid of concentration compartments greater than 2 gallon per minute/square feet.
51. the method for the treatment of water in having the electric deionizer that consumes chamber and concentration compartments comprises: in the consumption chamber with institute's water introducing to be processed electric deionizer; Promote non-required material to be transferred to the concentration compartments of electric deionizer from consuming the chamber, described concentration compartments comprises the first layer anionic exchange medium and is positioned at the second layer medium in described the first layer downstream, and the described second layer comprises the mixture of anionic exchange medium and cation exchange medium.
52. the method for the treatment of water comprises: with water to be processed introduce in the consumption chamber of electric deionizer, described consumption chamber has the sub-exchang medium of at least one leafing; Being introduced at least a portion anionic species that consumes the water in the chamber with promotion is transferred to first concentration compartments from the first layer Ion Exchange Medium, the water that has first intermediate mass with generation, described first concentration compartments determines by anion-selective membrane and cation selective film to small part, and described first concentration compartments to small part comprises first district that comprises cation exchange medium that second district by comprising anionic exchange medium separates with anion-selective membrane basically.
53. the method for claim 52 further comprises keeping passing through the rate of flow of fluid of first concentration compartments greater than 2 gallon per minute/square feet.
54. the method for the treatment of water in electric deionizer comprises: will comprise non-required material water to be processed introduce in the consumption chamber of electric deionizer; Promote non-required material to transfer to the concentration compartments of electric deionizer to generate treating water from consuming the chamber; Electrolysis produces acid solution in accessory part; With at least a portion acid solution is introduced the concentration compartments.
55. the method for claim 54, wherein electrolysis produces acid solution and comprises halide salt aqueous solution is introduced accessory part.
56. the method for claim 55 further is included in and produces basic solution when producing acid solution in accessory part.
57. the method for claim 56 further comprises the outlet logistics with in the described basic solution and concentration compartments.
58. the method for claim 57 further comprises and a part for the treatment of water is mixed with described salt brine solution and mixture is introduced described accessory part.
59. the method for claim 58 is wherein introduced acid solution the concentration compartments and is comprised that pH is lower than 4.3 acidic solution introduces the concentration compartments.
60. the method for claim 59 further comprises at least a portion liquid in the concentration compartments is outgased.
61. water treatment system comprises: water source to be processed; With comprise that first consumes chamber and second and consume the electric deionizer of chamber, described first and second consume chambers with the split flow configuration respectively fluid be connected to water source to be processed; With with described first consume first concentration compartments of chamber ionic communication and second concentration compartments that fluid is connected to downstream, first concentration compartments.
62. the method for claim 61, wherein electric deionizer comprises that further fluid connects first electrode vessel of upstream, first concentration compartments.
63. electric deionizer comprises: a plurality of liquid that are designed to consume the chamber along the parallel flow paths mobile therein; With concentration compartments a plurality of and at least one consumption chamber ionic communication, wherein arranged in turn to the concentration compartments of small part.
64. the electric deionizer of claim 63, wherein said a plurality of concentration compartmentss determine the single flowing-path by described electric deionizer.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US80550506P | 2006-06-22 | 2006-06-22 | |
| US80551006P | 2006-06-22 | 2006-06-22 | |
| US60/805,505 | 2006-06-22 | ||
| US60/805,510 | 2006-06-22 | ||
| PCT/US2007/014622 WO2007149574A2 (en) | 2006-06-22 | 2007-06-22 | Electrodeioni zation apparatus and low scale potential water treatment |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410053593.8A Division CN103739044B (en) | 2006-06-22 | 2007-06-22 | Low scale potentiality water processes |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101472847A true CN101472847A (en) | 2009-07-01 |
| CN101472847B CN101472847B (en) | 2014-10-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200780023054.8A Expired - Fee Related CN101472847B (en) | 2006-06-22 | 2007-06-22 | Electrodeionization device and method for treating water |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN101472847B (en) |
| CA (1) | CA2850777A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102939266A (en) * | 2010-06-03 | 2013-02-20 | 奥加诺株式会社 | Electric device for production of deionized water |
| CN111646582A (en) * | 2020-07-16 | 2020-09-11 | 西安交通大学 | Circulating water electrochemical treatment system and method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5868915A (en) * | 1996-09-23 | 1999-02-09 | United States Filter Corporation | Electrodeionization apparatus and method |
| US6284124B1 (en) * | 1999-01-29 | 2001-09-04 | United States Filter Corporation | Electrodeionization apparatus and method |
| EP1308201B1 (en) * | 2001-10-31 | 2005-01-05 | Kurita Water Industries Ltd. | Electrodeionization apparatus |
-
2007
- 2007-06-22 CA CA2850777A patent/CA2850777A1/en not_active Abandoned
- 2007-06-22 CN CN200780023054.8A patent/CN101472847B/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102939266A (en) * | 2010-06-03 | 2013-02-20 | 奥加诺株式会社 | Electric device for production of deionized water |
| CN111646582A (en) * | 2020-07-16 | 2020-09-11 | 西安交通大学 | Circulating water electrochemical treatment system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101472847B (en) | 2014-10-29 |
| CA2850777A1 (en) | 2007-12-27 |
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