DEVICE AND METHOD FOR THE REGENERATION OF MIXED ION EXCHANGE RESIN BEDS

Abstract: A device and a method for the regeneration of ion exchange resin mixed beds, used for the desalination of water or of aqueous solutions deriving from industrial processes (process solutions), that use two columns: the first treatment column (C1), containing a mixed bed of ion exchange resins, in which the cation exchange resins are regenerated, and a second column (C2) into which the anion exchange resins are transferred and regenerated, to be then reintroduced from the bottom into the above mentioned first column (C1), where they rise through the cation exchange resins intimately mixing themselves with them.

Description: DEVICE AND METHOD FOR THE REGENERATION OF MIXED ION EXCHANGE RESIW BEDS This invention concerns a new device for regenerating mixed beds of ion exchangers used for the desalination of water or aqueous solutions deriving from industrial processes (process solutions) and the method of carrying out this regeneration. The technique of desalination by means of mixed beds of ion exchanger resins, described for the first time in 1951 (US patent 2,578,937), is now widely used for the production of very low ion content water: among the most important applications are the production of steam-boiler feed water and water for the electronic and pharmaceutical industries. Another application of mixed bed processes concerns the desalination of process solutions containing non- ionic organic compounds, as, for example, molecules of pharmaceutical or foodstuffs interest. What characterizes mixed bed processes is the fact that water or the solution to be desalinated is percolated through an intimate mixture of a cation exchanger and an anion exchanger. Mixed bed treatment allows the reduction of the residual saline content of treated water to quite lower levels as compared with desalination through separate beds of two ion exchangers; in fact, whereas in the case of separate beds, the fraction of ions removed is limited by the equilibrium value corresponding to the maximum degree of regeneration of the ion exchangers and hardly exceeds 99%, in the case of a mixed bed there are no theoretical limits to the fraction of ions removed. Furthermore, whereas during the treatment, for example, through separate beds of cationic and anionic exchangers connected in series, the pH of the treated solution falls to very low levels in the column containing the cationic resin, in the mixed bed pH remains near to neutral. This characteristic allows, for example, the desalination of solutions of pH sensitive molecules. Opposed to theεe advantages, the regeneration of mixed beds after use is unfortunately till now much more complex and costly than with separate beds, because the cation exchangers and the anion exchangers must be separated before regeneration, which is carried out with acids and bases respectively and then they must be homogeneously remixed after regeneration. Separation and regeneration of exhausted mixed beds has been described for the first time in US 2,771,424 (1956). A monography of recent processes was reported by B. Coulter, Ultrapure Water, Nov. 1987. In all regeneration processes, the resins are separated by hydraulic classification by utilizing the different densities and granulometries of the two exchangers. Once separated, the resins can be regenerated in the same column which contained the mixed bed (internal regeneration) or one or both of them can be transferred into one or more different columns where regeneration is carried out (external regeneration); they are then mixed in a special mixer (or even in the column used for the regeneration of the cation exchanger) and then transferred into the column used for the mixed bed. Another possibility consists in transferring said resins, after regeneration, into the column used for the mixed bed and mixing them therein. The external regeneration procedure requires a much more complex plant, and is therefore normally used only for the final desalination of water to be fed to steam- boilers in thermoelectric or thermonuclear power stations. The most widely used process for small or medium sized units is the internal regeneration. In this latter case the reagents for regeneration of the anion and the cation exchangers enter the column from the top and bottom respectively, either simultaneously or at different times (regeneration of the anionic exchanger is normally carried out first), while the exhausted regenerating solutions are collected from the same discharge line provided with devices (strainers) able to retain the portion of resin situated near the interface between the resins. This system is less costly but has two significant disadvantages: 1) the interface between the resins must be exactly maintained at the level of the discharge line, otherwise a part of the anionic exchanger will be saturated by the acid used for the regeneration of the cationic exchanger or, vice versa, a part of the cationic exchanger will be saturated by the base used for the regeneration of the anionic exchanger . This fact implies that it is not possible to handle a mixed bed with quantities of cationic resin different from those of the original design and that each variation of volume of the cationic resin, either due to the normal swelling occuring during regeneration or to a possible loss of resin, will have negative effects on the following performance of the bed; 2) even if the level of the interface is maintained at the level at which the discharge line has been installed, there will always be a certain mixing between the two regenerating liquids or between one regenerating liquid and the barrier water, in a substantial volume around the interface between the resins. Both problems 1 and 2 cause incomplete regeneration of that portion resins which is near to the interface; it means that a part of the anionic resin will be saturated with the cationic resin regeneration liquid and vice versa. This implies a lower exchange capacity in the regenerated resins at equal volumes and consumption of regenerating liquid; furthermore, the portion of saturated anionic resin will release sulphate or chloride ions and the portion of saturated cationic resin will release sodium ions, so affecting the quality of water produced in the successive desalination process (see e.g. G.J. Crits, Ion Exchange, Technology of Mixed Beds, Ultrapure Water, Nov. 1984). These disadvantages can be reduced by introducing into the mixed bed, other than the two ion exchange resins, an inert separator consisting, for example of inert small beads with an intermediate density between those of the two resins. During hydraulic classification, the separator positions itself between the two resins distancing them from the zone where mixing of the two regeneration reagents takes place. In this way, the partial saturation of the anionic resin is reduced as well as the criticality of the level of the cationic resin, but the desalination capacity per unit volume of bed will be inferior because the inert separator occupies a portion of the column volume. On the contrary, external regeneration eliminates all of the problems related to imperfect separation of the regenerating reagents in such way assuring greater exchange efficiency, an improved degree of purity of the treated water and better repeatability of the desalination process: a recent mixed bed process with external regeneration is, for example, described in US 4,472,282. On the other hand, transferring the resins involves, as has already been pointed out, complex equipments and troublesome handling of the same and long overall regeneration times, thus making this method economically feasible only for the treatment of big volumes of water, already with a very low salt content. Consequently, the equipment complexity iε justified only for big plants and such operational work and long regeneration times are only acceptable when infrequent regeneration cycles (see e.g. B.L. Coulter, art. cit. ) are required. Another critical point in all mixed bed processes is the homogeneous mixing of the ion exchange resins once the regeneration is carried out. It is well known that the quality of water produced and the working capacity of the bed, largely depend on the quality of the mixing which must be as homogeneous as possible (see e.g. E.G. Baeva et al., Development of a System for Mixing Ion Exchangers, Teploenergetika, 1968). In the devices known in the state of the art, mixing is always obtained by fluidizing the bed by counter-washing with water and then blowing air from the bottom of the column. This method is also applied in external regeneration units, with the sole difference that in the latter case, mixing is sometimes effected in a special apparatus instead of in the column dedicated to the mixed bed. Mixed beds obtained by this procedure can be, and usually are, lacking in homogeneity: in general, the upper part of the bed consists almost exclusively of the lighter anionic resin and the lower part almost exclusively of the cationic resin (data concerning lack of homogeneity in mixed beds are given by Baeva and S. Fisher, Trouble Shooting in Mixed Bed Ion Exchange, Ultrapure Water, July-August, 1992). Only the central portion contains both resins mixed in quantities approaching the optimal ratio; however, if, for example, transparent columns are used, a simple optical analysiε shows that even in this portion, homogeneity is not optimal: relatively large portions (of the order of 0.5 in a 40 bed) in which cation exchangers prevail, alternate with zones of the same size in which anion exchangers prevail. In conclusion, available mixed bed techniques at the current state of the art, have disadvantages as compared to the conventional treatment with two or more separate beds, which are tied on the one hand to greater plant and operational complexity (above all if external regeneration is used) and on the other hand to high handling costs and, as a consequence, are competitive for the production of ultrapure water or of process solutions with very low ionic content, only in the case of solutions with already very low saline content, usually lower than that found in well water. On the other hand, separate bed processes are not normally usable to produce water or process solutions with a conductivity of less than 0.5 μS/cm. Consequently, the production of water with very low conductivity (that iε less than 0.5 μS/cm, preferably less than 0.25 μS/cm or even 0.08 μS/cm, such as for example for thermonuclear plants) normally requires two treatment steps, in which only the second iε carried out with a mixed bed. Furthermore, internal regeneration processes are normally used for small mixed beds and aε has been previously stated, they are rather unsatisfactory, even for the quality of the deionized water produced in each successive phase. It is to the subject of this invention a new device for the regeneration and mixing of ion exchangers resins in a mixed bed and method for operating it. This handling is much simpler in comparison to the units with external regeneration of the present state of the technology, it maintains all of their advantages and even increases their performance, in particular thanks to the greater homogeneity of the mixed bed obtained by said method. A further object of this invention is the method described below for the preparation of a mixed bed of ion exchangers, characterized by great homogeneity. This procesε does not require the use of air for mixing the resins and is applicable to units with external regeneration. The simplicity and versatility of the plant object of this invention, make it usable even for small or medium sized applications and even in processes which require frequent regeneration, for the first time rendering posεible, and economic, to obtain purified water with a purity degree similar to those obtained by the beεt unitε with external regeneration, even when starting from well-water or even from sea-water. The mixed bed obtained by the method and the plant object of this invention, is furthermore able to reduce inorganic and organic ionic impurities to extremely low levels in aqueous solutions of neutral organic products (for example, molecules of pharmaceutical interest and their intermediates or sugar solutions or food products) . The scope and advantages of the device and the method according to the invention are reached with the characteristics listed respectively in independent claims 1 and 6. Advantageous applications of the invention appear in the dependent c . ms. Substantially, according to - ie invention, two columns are foreseen: a first treatment column containing the mixed bed of ion exchange resins, in which the cation exchange resins are regenerated after the treatment/desalination process, and then a second column into which the anion exchange resins are transferred and regenerated, to be then reinserted at the bottom of the first column where they rise through the cation exchange resins present therein, intimately mixing themselves with these, to give a reconstituted homogeneous mixed bed. Further characteristics of the invention will be made clear by the detailed description which follows, which refers to one of its purely exemplary forms, therefore not limitative, and which iε illustrated in the annexed Fig. 1, in which: Fig. 1 is a scheme of the device for the regeneration of fluidized beds according to the invention. Referring to this figure, the device object of this invention, consists substantially of two columns, one of which, indicated by Cl is dedicated to contain the mixed bed and to the regeneration of the exhausted cationic exchanger. The other, indicated by C2, is dedicated to the regeneration of the exhausted anionic exchanger, said columns being joined according to the diagram in Fig. 1. In the device of Fig. 1 in which the salient characteristics are shown, the open and close type valves are indicated with the term V, the regulation valves with the term VR and the circulation pump with the term P. The functioning of the device of the invention substantially follows the operations described below. Initially, the anionic exchange resin is loaded into column C2 and the cationic exchange resin into column Cl. Both of the exchange resins are regenerated separately and according to the supplier's instructions (for example, for the regeneration of the anionic exchanger a strong base is used, usually εodium hydroxide at 4% w/w, whereas for the regeneration of the cationic exchanger, a strong acid is used, normally hydrochloric acid at 8 to 12% w/w or sulphuric acid at the same concentration). For the cation exchanger, the acid solution is fed to Cl through valve V4, simultaneously discharging the exhausted regenerating solution through valve V5 and regulating VR4 to maintain the liquid just above the level of the resin. Similarly, for the anion exchanger, the alkaline solution is fed to C2 through V6, discharging the exhausted regenerating solution through V7 and regulating VR5 to maintain the liquid just above the level of the resin. After regeneration, the ion exchangers are thoroughly washed with deionized water through the same hydraulic circuits. Upon completion of the washing (which can be determined on the basis of the conductivity of the eluate or on the total volume of water used), both resins are counter-washed with the flow recommended by the supplier for an expansion of between 25% and 100% of the initial volume, supplying deionized water through valves V8 and V9 respectively and first discharging the air and then the water through valves V10 and Vll respectively. At the end of this phase, the counter-waεhing is continued m C2, whereas it is stopped in Cl by closing V8 and V10. The cation exchange resin bed in Cl is again fluidized by opening valves V12 and V13, starting the pump P and regulating the valve VRl to obtain the flow necessary to expand the bed of cation exchange resin up to 200% - 400% of its initial volume. Valves V9 and Vll are then closed and VI is opened to presεurize the columns. Valve V12 is closed then valve V14, which changes the flow of pumped water from Cl to C2, iε opened simultaneously to V3, which cauεes the anionic resin to be transferred from C2 to Cl. In this way, the flow of water pumped through V14 pushes the fluidized bed of the anion exchanger through V3 and into column Cl where the anionic resin, which is lighter than the cationic resin, rises through the fluidized bed of the cation exchanger mixing itself intimately with it. When the anion exchanger has been transferred into Cl, the pump P is stopped, valves V13, V14 and V3 are closed and the fluidized mixed bed, just obtained after the tranεfer of the anion exchanger from C2 to Cl, is compacted by rapidly discharging water through valve V5. Valve V5 is closed when the level of water in the column is just a little above the level of the resin. The mixed bed obtained by this process results extraordinarily homogeneous as compared with thoεe obtained by known methodε (such as, for example, counter-washing with water and blowing air into the bottom of the column). The two resins are found to be homogeneously mixed for at leaεt 80% of the column length (preferably for at least 90%); minimal non- homogeneous residual zones are observed only at the top of the column. At this point, column Cl contains the regenerated mixed bed onto which the solution to be desalinated can be loaded (through V4); the resulting desalinated water (ultra-pure water or deεalinated εolution of organic compounds) is collected through valve V16. When the conductivity of the desalinated solution iε above the level of acceptability eεtabliεhed for the type of occuring purification, or when a predetermined volume of solution has been treated, the desalination phaεe is εtopped and the separation of the reεinε iε begun for the regeneration of the εa e. To this effect, column Cl is filled with water, through V8 for example, closing VI and venting the air through V10; when the column is full, V10 is closed and valves VI, V2, V15, and V12 are opened; the pump P iε started and valve VRl is gradually opened. In this way, the mixed bed in Cl iε fluidized and the lighter anionic reεin gradually εeparateε out, above the cationic reεin. When the flow, regulated by VRl iε increaεed, the upper part of the anionic fluid bed reacheε the reεin tranεfer line and begins to pass over into column C2 through valve V2, together with the flow of fluidization water. Valve VRl is gradually opened to give the flow neceεεary to expand the cation exchanger to a level just below the transfer opening of the anion exchanger (indicated by A in Fig.l): valve V13 can be opened (partially or completely) to reach the maximum flow without excesεive loss of load in the anion resin bed in C2. When all of the anion exchanger is transferred into C2, the step is terminated by stopping the pump P and closing the valveε which were opened at the beginning of the transfer. The technicians can then proceed with emptying excess water from the columnε and with the regeneration of the ion exchangerε by the procedure which has already been described. In a variant of the invention, before the separation of the resins is started, a quantity of 4-12% w/w hydrochloric acid, greater than that required for the regeneration of the cation exchanger, is fed into the mixed bed in Cl. In this case, after the separation, there will be no need to regenerate the cation exchanger. Apart from an increased acid consumption, this variant brings an easier and more complete separation of the ion exchangers and is often advantageous in cases of desalination of concentrated solutions of organic molecules. The device and the method object of this invention, are very useful in the pharmaceutical field, for example, because they consent to reduce the amount of inorganic and organic ionic impurities to extremely low levels in aqueouε solutionε of drugε and of diagnosticε agents. Among these, it iε worthwhile to mention compounds of non-ionic type, such as, for example, iodinated contrast agents for radiography or paramagnetic contrast agents for magnetic resonance imaging (MRI), productε which often uεt be adminiεtered in particularly high concentrationε and for which an high degree of purity iε essential. Among the neutral iodinated contrast agents for radiography, the following can be, by way of an example, mentioned iopamidol, iomeprol, iohexol, ioversol, iopentol, iopromide, ioxilan, iotriside, iobitridol, iodixanol, iofratol, iotrolan, iodecimol, iopirol, iopiperidol. Among the neutral paramagnetic contrast agents for MRI particularly preferred resulted to be the gadolinium complex of 10-(2-hydroxypropyl)-l,4,7,10-tetraazacyclo- dodecane-l,4,7-triacetic acid (gadoteridol) . The following exampleε are intended to illuεtrate the best experimental conditions in which to apply the method, subject of the invention. Experimental Section Example 1 In a device according to the preceding description and to Fig.l, the columns Cl and C2, which have effective volumes (meaεured from the εupport plate to the height of the feed diεtributor) of 36 and 22 L, were loaded reεpectively with 12 L of εulphonic cation exchanger Rohm & Haaε Amberjet (R) 1200 Na and with 22 L of strong anion exchanger, type I Rohm & Haas Amberjet (R) 4200 Cl. The ion exchangers were regenerated respectively with 26 kg HCl 10% w/w at a flow of 40 L/h and with 135 kg of sodium hydroxide 4% w/w at a flow of 90 kg/h. Both of the ion exchangers were then washed with deionized water until the eluate conductivity fell below 50 μS/cm. Then the anion exchanger waε tranεferred to Cl and mixed with the cation exchanger according to the method subject of this invention. To the mixed bed εo prepared, were fed 100 L of a solution of 1.3 kg (22 mol) of NaCl in 100 L of water (conductivity 28,000 μS/cm) at a rate of 100 L/h. The conductivity of the treated water waε, at the beginning, a little less than 1 μS/cm but rapidly fell, becoming stable, at 0.1 μS/cm until 80 L of water had been treated. The conductivity then rose very rapidly until it went out of the limit of the instrument (3,000 μS/cm) indicating that the bed waε exhausted. In order to have a measure of the total capacity up to saturation of the ion exchangers, feeding of the saline solution was continued until the end and the eluate was collected in a second fraction. Then the mixed bed was washed with deionized water to a conductivity of 100 μS/cm, still collecting the eluate in fraction 2. The total capacity of the anion and cation exchangers was determined by dividing the molar quantity of exchanged ions by the volume of the anion and cation exchangers. The molar quantity was obtained deducting from the total quantity of sodium chloride fed, respectively, the total quantity of chloride ions determined with silver nitrate in fraction 2 and the difference between the total quantity of chloride ionε and the free acidity titrated with caustic soda. The total capacity of the anion exchanger resulted to be 0.84 mol/L (referred to the exchanger volume in the form of chlorine) and that of the cation exchanger 1.7 eq/L (referred to the exchanger volume in the form of Na), in accordance with what declared from the ion exchanger manufacturer. The effective capacity of the mixed bed (defined as the quantity of ions fixed before the conductivity rises above 0.5 μS/cm) resulted to be 17.6 eq. , which, when referred to the quantity of anion exchanger correspondε to 0.8 eq/L. Thiε value iε very high, in fact better than that foreseen on the baεis of the data supplied by Rohm & Haas for a unit which uses separate beds (Amberjet 4200 Cl co-flow engineering data). Example 2 For purposes of comparison, the same ion exchangers from Example 1 were loaded into two separate columns, regenerated in the same conditions, counter-washed and washed with deionized water to the same final conductivity. The two columns were joined in series in such a way that the anion exchanger followed the cation exchanger. A solution of sodium chloride in water in the same quantities as in Example 1 was fed to the two columns at a rate of 100 L/h. The conductivity of the treated water was initially a little lesε than 50 μS/cm, but rose moving up to 100 and then to 300 μS/cm up to 70 L of treated water (pH alkaline). The conductivity then went out of the limit of the inεtrument (3,000 μS/cm) indicating that the deionizer was exhausted. As in the previous example, in order to have a measure of the total capacity up to saturation of the ion exchangers, feeding of the saline solution was completed the eluate was collected in a second fraction. Then the in series beds were washed with deionized water to a conductivity of 100 μS/cm εtill collecting the eluate in fraction 2. Whereas the total capacity of the exchangers, determined by the same method as in Example 1, resulted practically identical to that of Example 1, the effective bed capacity (defined in this case as the quantity of ions fixed before the conductivity rises above 400 μS/cm) resulted to be 0.68 eq/L. This value is near to that expected, based on data supplied by Rohm & Haas for a separate bed unit like the one in thiε example (A berjet 1200 Na co-flow engineering and Amberjet 4200 Cl co-flow engineering). The considerable advantages assured by the unit of Example 1 appear evident, both in terms of quality of the treated water and of capacity before exhaustion, at equal reagent consumption. Example 3 Desalination of a concentrated solution of N.N'-bis(2.3- dihvdroxvpropvl -5-rfhvdroxvacetvl)methvlaminol-2.4.6- triiodo- .3-benzenedicarboxamide A) Solution of N ; N'-bis(2,3-dihydroxypropγl)-5- [(hydroxyacetyl)methylamino]-2,4,6-triiodo-l,3-benzene- dicarboxamide. 90 kg of N,N'-bis(2,3-dihydroxypropyl)-5-[ (hydroxy¬ acetyl)-methylamino]-2,4,6-triiodo-l,3-benzenedicarbo- xa ide obtained by the procedure described in EP 185130 were suspended in 400 L of deionized water and heated under reflux. 310 g of 30% w/w sodium hydroxide were added to the suspension. It was then heated to 120"C under sealing conditions and this temperature waε maintained for 1 hour. It was then cooled to 50"C and 7.7 kg of 30% w/w sodium hydroxide were added gradually cooling to 40'C over 2 hours. After a further 4 hours at 40"C, it was cooled to 20"C and pH waε adjuεted to 5.5 with hydrochloric acid. The εolution obtained was loaded onto 160 L of absorbent resin R&H A berlite 1600, feeding the eluate to a nanofiltration unit equipped with a Desal DK4040 membrane. When the loading was completed, the resin was washed with 800 L of water at 40 * C collecting the eluate in the tank of the nanofiltration unit. During elution or at the end of it, the nanofiltration unit was started and the operation continued until the volume of the solution in the unit waε reduced to about 200 L. At the same time, the elimination of the greater part of sodium chloride contained in the eluted solution was also obtained. The obtained concentrated solution of N,N'-bis(2,3- dihydroxypropyl)-5-[(hydroxyacetyl)methylamino]-2,4,6- triiodo-l,3-benzene-dicarboxamide, which will from now on be referred to as solution A, contains 80 kg of the deεired product, about 0.05 mol/L of organic ionic impurities (aromatic carboxyiic acidε) and 0.03 mol/L of inorganic salts (prevalently NaCl) B) Desalination of solution A. 200 kg of solution A at 40% w/w were fed at a rate of 40 L/h to the same unit of Example 1, filled with the same quantities of the same ion exchangers, which were previously regenerated by the same method of example 1. The eluate line was equipped with a conductivity analyser and also with a photometer to measure the absorbance at 280 nm, to detect the presence of organic substanceε in the eluant. The eluate was discarded until its absorbance began to rise rapidly, indicating the presence of the organic product in question. From this moment, the eluate was collected in a tank up to exhaustion of solution A. During the collection of this fraction which contains the greater part of the organic product, the conductivity remained below 0.1 μS/cm. When εolution A waε finiεhed, the mixed bed waε waεhed with 30 L of water at the εame flow rate and then again with 150 L of water at a flow rate of 100 L/h alwayε collecting the eluate in the εame tank of the product fraction. Even during this phase, the conductivity of the eluate remained very low. The fraction corresponding with the desalinated product, which is free from chloride ions and carboxyiic acids, was concentrated by evaporation to a viscous residue containing 15% of water. The product was then isolated in a practically pure form (99%) by the addition of absolute alcohol at reflux temperature, followed by cooling and filtration. Example 4 Regeneration of the Mixed Bed aliej; Trea men fif t & Organic Solution of Example 3. The mixed bed to be regenerated was counter-washed with 10 L of water. The water level was lowered to just above the level of the resin and then, through the feed- line were fed, firstly 60 kg of 8.5% w/w HCl at a flow rate of 40 kg/h and then 200 kg of deionized water, the first 30 L at the εame flow rate and the remainder at a rate of 150 kg/h. The cation and anion exchangers were then εeparated and the anion exchanger transferred to column 2, according to the deεcription of this invention: the separation was found to be easy and clean-cut. The anion exchanger was regenerated, washed and then retransferred to column Cl where it was mixed with the cation exchanger, exactly aε deεcribed in Example 1. Example 5 Desalination test eαual to that deεcribed in Example 3 on the regenerated mixed bed of Example 4 As a confirmation of the repeatability and reliability of the method object of this invention, the complete regeneration cycle according to Example 4 and desalination of a solution prepared according to point B of Example 3, were repeated 42 times without significant functional anomaly and with the same deεalination efficiency. Example 6 Desalination of a solution of the non-ionic organic complex of Gadolinium of lQ-(2-hγd.rpxγpropyl)-l ,4.7 ,10- tetraazacvclododecane-1.4.7-triacetic acid. 100 kg of an aqueouε solution containing 25 kg of the compound in question, (solution A'), obtained by the method described in patent application EP 292689, was fed at a rate of 40 L/h to the same unit of Example 1, filled with the same quantities of the εame ion exchangers, previously regenerated according to the εame method of Example 1. The eluate line was equipped with a conductivity analyser and also with a photometer to measure the absorbance at 280 nm, to detect the presence of organic subεtances in the eluate. The eluate was discarded until its absorbance began to rise rapidly, indicating the presence of the organic substance in question. From this moment the eluate was collected in a tank until the solution was finished. During the collection of this fraction which contains the greater part of the organic product, the conductivity remained below 0.1 μS/cm. When solution A' was finished, the mixed bed was waεhed with 30 L of water at the εame flow rate and then finally with 300 L of water at a flow rate of 100 L/h, alwayε collecting the eluate in the εame tank of the product fraction. Even during thiε phaεe, the conductivity of the eluant remained very low and the fraction corresponding to the deεalinated product waε εhown to be free from chloride ions.

Claims: CLAIMS 1. Device for the regeneration of mixed beds of ion exchange resins, including cation exchange resins and anion exchange resins, contained in a first treatment column (Cl), characterized by comprising: means for the separation of the anion exchange resins from the cation exchange resins in said column (Cl); - eanε for the transfer of the anion exchange resins into a εecond column (C2) which is in communication with said first column (Cl) by a conduit with valves; meanε for the regeneration of the cation exchange resinε directly in column (Cl); meanε for the regeneration of the anion exchange reεinε in εaid column (C2) and means for the transfer of the regenerated anionic resinε from column (C2) to column (Cl) and for the homogeneouε reconεtitution of the mixed bed in (Cl). 2. Device according to claim 1, characterized by the fact that said means for the separation of the anion exchange resins from the cation exchange resins are means of fluidization of the mixed bed which consent the im ission of water from the bottom of column (Cl), so that the lighter anion resins shift themselveε on top of the cation reεinε. 3. Device according to claim 1, characterized by the fact that the εaid meanε for the transfer of the anionic resinε from the firεt column (Cl) to the second column (C2) include a transfer opening (A) in the column (Cl), at a level above that of the mixed bed, a conduit connecting εaid opening (A) to column (C2), intercepted by a valve (V2), and further comprise means of expanding the cationic resin in column (Cl) up to a level just below said opening (A). 4. Device according to claim 1, characterized by the fact that said means for the regeneration of the cationic resin in column Cl consiεt of an acid solution fed through a valve (V4), whereas the exhausted solution after regeneration is discharged through a valve (V5) and that εaid meanε for the regeneration of the anionic resin in column (C2) consist of an alkaline solution fed through a valve (V6), whereas the exhausted εolution after regeneration iε discharged through a valve (V7). 5. Device according to claim 1, characterized by the fact that said meanε for transferring the regenerated anionic reεinε from column (C2) to column (Cl) comprise a conduit intercepted by a valve (V3), which joins said columns in the region of their respective bases and water pumped in column (C2) which transfers the bed of anionic resins into column (Cl) where it riseε through the fluidized bed of the cationic reεins mixing itself intimately with them. 6. Method for the regeneration of mixed beds of ion exchange reεinε, compriεing cation exchange reεinε and anion exchange resins, contained in a first treatment column (Cl), characterized by the following stepε: separation of the anion exchange resin from the cation exchange resin in said column (Cl); tranεfer of the anion exchange reεin into a εecond column (C2) through a conduit with valveε; regeneration of the cation exchange reεin directly in said column (Cl); regeneration of the anion exchange resin in said column (C2); tranεfer of the regenerated anion resin from column (C2) to column (Cl) and ho ogeneouε reconεtitution of the mixed bed. 7. Method according to claim 6 in which regeneration of the cation exchange reεins precedeε the εeparation of the anion exchange reεinε from the cation exchange resins. 8. Method according to claims 6 and 7, characterized by the fact that the said separation step of the anion exchange resinε from the cation exchange reεins, takes place through fluidization of the mixed bed with the introduction of water from the bottom of column (Cl), εo that the lighter anionic reεinε rise above the cationic reεinε. 9. Method according to claims 6 and 7, characterized by the fact that the tranεfer of the anionic reεins from the firεt column (Cl) to the εecond column (C2) takeε place through a conduit with valves connecting said columns (Cl) and (C2) and situated at a higher level than that defined for the mixed bed and further the cationic reεin bed in said column (Cl) is expanded to a level just below that of the transfer line. 10. Method according to claims 6 and 7, characterized by the fact that the regeneration of the cationic resinε in column (Cl) consiεtε in introducing an acid solution and in discharging the exhausted solution, maintaining the liquid level just ibove that of the resins. 11. Method according to claim 7, characterized by the fact that the regeneration of the cation exchange resins takes place by the introduction into column (Cl) of an acid solution in quantities greater than those necessary for the regeneration of said cationic resins. 12. Method according to claims 10 and 11, characterized by the fact that said acid solution contains hydrochloric acid or sulphuric acid at 8% to 12% w/w. 13. Method according to claim 6, characterized by the fact that regeneration of the anionic resins in column (C2) consists in introducing an alkaline solution and in discharging the exhausted solution, maintaining the liquid level just above the level of the resins. 14. Method according to claim 13, characterized by the fact that the alkaline solution contains sodium hydroxide at 4% w/w. 15. Method according to claim 6, characterized by the fact that after regeneration the resins are washed with deionized water and counter-washed with deionized water reaching an expansion of 100% of their initial volume. 16. Method according to claims 6 and 7, characterized by the fact that the transfer of the regenerated anionic resins from column (C2) to column (Cl) and the homogeneous reconstitution of the mixed bed are obtained by pumping water into column (C2) to push the bed of anionic resins through a conduit with valves and through the bottom of column (Cl) where the said bed of anionic resins riseε through the fluidized bed of cationic resinε mixing intimately with them. SUBSTITUTE SHEET 1SA/EP 17. Uεe of the device of claim 1 for the desalination/elimination of ionic impurities from aqueous solutions of neutral iodinated contrast agentε for radiography. 18. Uεe of the device of claim 1 for the desalination/elimination of ionic impuritieε from aqueouε εolutions of the following radiographic contrast agents: iopamidol, iomeprol, iohexol, ioversol, iopentol, iopromide, ioxilan, iotriside, iobitridol, iodixanol, iofratol, iotrolan, iodecimol, iopirol, iopiperidol. 19. Use of the device of claim 1 for the desalination/elimination of ionic impurities from aqueous solutions of neutral paramagnetic contrast agentε for MRI. 20. Use of the device of claim 1 for the desalination/elimination of ionic impurities from aqueouε solutions of gadoteridol.

Inventors: AUSONIO MARINA, PARENTI MAURO, VISCARDI CARLO FELICE, AUSONIO, MARINA, PARENTI, MAURO, VISCARDI, CARLO, FELICE
Applicants: AUSONIO MARINA, BRACCO SPA, DIBRA SPA, PARENTI MAURO, VISCARDI CARLO FELICE, AUSONIO, MARINA, BRACCO S.P.A., DIBRA S.P.A., PARENTI, MAURO, VISCARDI, CARLO, FELICE
Application year: 1997
Main classification: B01J49
IPC codes: B01J49