A520

Typical Physical & Chemical Characteristics Polymer Matrix Structure Macroporous Styrene-Divinylbenzene Physical Form and Appearance Opaque Cream Spherical Beads Whole Bead Count 95% min. Functional Groups Quaternary Ammonium Ionic Form, as shipped Cl - Shipping Weight (approx.) 680 g/l (42.5 lb/ft 3) Screen Size Range: - U.S. Standard Screen 16 - 50 mesh, wet Particle Size Range +1200 mm <5%, -300 mm <1% Moisture Retention, Cl -form 50 - 56% Reversible Swelling Cl -?SO 4/NO 3negligible Total Exchange Capacity, Cl -form, wet, volumetric 0.9 meq/ml min. dry, weight 2.8 meq/g min. Operating Temperature, Cl -Form 100?C (212?F) max. pH Range, Stability 0 - 14 pH Range, operating 4.5 - 8.5 Technical Data PRODUCT DESCRIPTION Purolite A-520Eis a macroporous strong base anion resin which is specially designed for the removal of nitrates from water for potable processes. The macroporous matrix and special ion exchange group functionality imparts ideal nitrate selectivity to Purolite A-520Emaking this resin par- ticularly suitable for nitrate removal even when moderate to high concentrations of sulphate are present. Hence this resin gives superior performance in nitrate removal applications when compared with standard exchange resins.A requirement of the nitrate removal process is to pro- duce potable water meeting the quality standard defined by the European Economic Community in the Directive No. 80/778 of July 1980. This directive limits the nitrates to a maximum admissable concentration (M.A.C.) of 50 mg NO 3/l. The U.S.A. drinking water regulations limit nitrates to 45 mg NO 3/l. ION EXCHANGE RESINS ? A-520E Macroporous Strong Base Anion Exchange Resin (For the selective removal of nitrate) Page 1 of 8 Sodium chloride is generally preferred for regeneration for reasons of cost and efficiency. When available sea water can be used quite effectively. The use of softened water for make up of regenerant and rinse is often rec- ommended to avoid the precipitation of calcium carbon-ate in and around the Purolite A-520E(or any other resin used in this application). Although the precipitation is not particularly detrimental in the short term, the long term effects may include increased resin attrition and leakage of nitrates. REGENERATION Purolite A-520Eis processed to insure that it meets the requirements for use in the treatment of potable water.On installation it is recommended that the resin be regenerated with two bed volumes of 6% NaCl followed by a rinse of four bed volumes of potable water, prior to use. PRECONDITIONING PROCEDURE The pressure drop or headloss across a properly classified bed of ion exchange resin depends on the particle size dis- tribution, bed depth, and void volume of the exchange material as well as on the viscosity (and hence on the tem- perature) of the influent solution. Factors affecting any of these parameters, for example the presence of particulate matter filtered out by the bed, abnormal compressability ofthe resin, or the incomplete classification of the bed will have an adverse effect and result in an increased headloss. Depending on the quality of the influent water, the application and the design of the plant, service flow rates may vary from 10 - 40 bed volumes/hour (1 - 5 gpm/ft 3). Typical pressure drop data is given in Fig. 1. HYDRAULIC CHARACTERISTICS Page 2 of 8 Standard Operating Conditions Nitrate Removal Operation Rate Solution Minutes Amount Service 8 - 32 BV/h Influent water per design per design 1 - 4 gpm/ft 3 to be treated Backwash Refer to Fig. 2 Influent water 5 - 20 1.5 - 4 BV 10 - 20?C 10 - 25 gal/ft 3 (50 - 68?F) Regeneration 2 - 5 BV/h 3 - 10% NaCl 20 - 60 90 - 250 g/l 0.25 - 0.6 gpm/ft 3 7.8 - 15.6 lb/ft 3 Rinse, (slow) 2 - 5 BV/h Influent water 20 - 60 2 - 5 BV 0.25 - 0.6 gpm/ft 3 15 - 40 gal/ft 3 Rinse, (fast) 8 - 32 BV/h Influent water - - 1 - 4 gpm/ft 3 Backwash Expansion 50% to 75% Design Rising Space 100% "Gallons" refer to U.S. Gallon = 3.785 litres During upflow backwash, the resin bed should be expanded in volume by between 50 and 70%. This oper- ation will free it from any particulate matter, clear the bed of bubbles and voids, and reclassify the resin parti-cles, ensuring minimum resistance to flow. Bed expan- sion increases with flow rate and decreases with temper- ature, as shown in Fig. 2. Care should be taken to avoid over expansion of the bed. The high selectivity of Purolite A-520Efor nitrate over sulphate ensures that any necessary reduction in nitrate levels can be achieved even in the presence of high influ- ent sulphate concentration. Hence it so offers the advan- tage over standard strong base resins that its exchange capacity for nitrates is less affected by a high influentconcentration of sulphate. For this reason, although Purolite A-520Ehas a lower total exchange capacity than standard strong base anion resin, its use can pro- duce advantageously higher throughputs for the follow- ing reasons. OPERATING PERFORMANCE Page 3 of 8 1.10 0.8 0.6 0.4 0.24 3 2 1 0102030404 8 12 16 30 °C (85 °F) 5°C (41°F) 10°C (50°F) 20°C (68°F) 100 80 60 40 20 0 02468100.8 1.6 2.4 3.2 4.0 50 °C (120 °F) 35°C (95°F) 20 °C (68 °F) 5°C (41 °F) 10°C (50°F) Fig. 1 PRESSURE DROP CHARACTERISTICS SERVICE FLOW RATE, U.S. gpm/ft 2 PRESSURE DROP, kg/cm 2/m of bed depth PRESSURE DROP, psi/ft of bed depth BED EXPANSION, Percent Fig. 2 BACKWASH EXPANSION FLOW RATE, U.S. gpm/ft 2 Conversion of Units 1 m/h (cubic meters per square meter per hour) = 0.341 gpm/ft 2 = 0.409 U.S. gpm/ft 2 1 kg/cm 2/m (kilograms per square cm = 4.33 psi/ft per meter of bed) = 1.03 atmos/m = 10 ft H 2O/ft SERVICE FLOW RATE, m/h BACKWASH FLOW RATE, m/h Page 4 of 8 1.0 0.8 0.6 0.4 0.20 0 0.2 0.4 0.6 0.8 1.0 20 15 10 5 250 g NaCl/l (15 lb/ft 3) 125 g NaCl/l (8 lb/ft 3) VS. RATIO NO 3- NO 3- + SO 4= RATIO NO 3- NO 3- + SO 4= 50 40 30 20 10 0 0 0.2 0.4 0.6 0.8 1.0 250 g NaCl/l (15 lb/ft 3) 125 g NaCl/l (8 lb/ft 3) VS. RATIO NO 3- NO 3- + SO 4= RATIO NO 3- NO 3- + SO 4= Fig. 3 OPERATING CAPACITY BASE OPERATING CAPACITY, NO 3 -eq/l OPERATING CAPACITY, NO 3 -Kgr/ft 3 NITRATE LEAKAGE, % OF INFLUENT Fig. 4 NITRATE LEAKAGE PUROLITE A-520E, CO-FLOW REGENER ATION Both standard gel type or macroporous strong base resins are quite capable of effective nitrate removal where sulphate to total anion ratios are low. However, on account of the high selectivity for sulphate in dilute solu- tions which follows the order, HCO3 -< Cl -< NO 3 -< SO4 = selective displacement of nitrate by sulphate results in the effective nitrate removal capacity being reduced by sulphate loading. Apart from the obvious disadvantage of the reduction of treated water obtained on cycling, the exchange of both nitrate and sulphate by chloride will result in a less palatable and sometimes less acceptable water than the influent supply, in that the treated water may be more corrosive and the limits for chloride con- centration may be exceeded. Fig. 3 and Fig. 4 give the operating capacity and nitrate leakage respectively which may be obtained using co- current regeneration at the given regeneration levels. Values obtained from Fig. 3 are expressed in terms of nitrate throughput, corrected for nitrate leakage, and hence may not be used directly to determine the through- put of water. All ion concentration values are either on a ppm or a meq/l basis for ratio determination. Calculation for throughtput of treated water where V = resin volume (liters) OC = operating capacity (eq/l) L = nitrate load (meq/l) l n = nitrate leakage (meq/l) or cyclic output (U.S. gal) = where V f= resin volume (ft 3) OC k= operating capacity (kgr/ft3) L p = nitrate load (ppm as CaCO 3) np = nitrate leakage (ppm as CaCO 3) cyclic output (liters) = x 10 3 V fx OC kx 10 3 0.058 (L p- l np ) Vx OC L- l n Page 5 of 8 OPERATING CAPACITY, NO3 -Kgr/ft 3 1.0 0.8 0.6 0.4 0.2 0 0 0.2 0.4 0.6 0.8 1.0 20 15 10 5 180 g NaCl/l (11.5 lb/ft 3) 125 g NaCl/l (8 lb/ft 3) VS. RATIO NO 3- NO 3- + SO 4= RATIO NO 3- NO 3- + SO 4= 50 40 30 20 10 0 0 0.2 0.4 0.6 0.8 1.0 180 g NaCl/l (11.5 lb/ft 3) 125 g NaCl/l (8 lb/ft 3) VS. RATIO NO 3- NO 3- + SO 4= RATIO NO 3- NO 3- + SO 4= Fig. 5 OPERATING CAPACITY BASE OPERATING CAPACITY, NO 3 -eq/l NITRATE LEAKAGE, % OF INFLUENT Fig. 6 NITRATE LEAKAGE PUROLITE A-520E, COUNTER-FLOW REGENER ATION Similarly Fig. 5 and Fig. 6 give the values for counter- current regeneration. It should be noted that in this case the nitrate leakage is lower for a given regeneration level. Hence the possibility to blend treated with untreated water on a 50% basis is a useful option which can make counter-current regeneration attractive. On the other hand the choice of co-current regeneration can result in the production of higher volumes of treated water of satisfactory quality for direct use. The higher leakage (l n, l np , in the equations above) so reduces the load on the ion exchange bed that for a given operating capacity greater throughputs per cycle are obtained. This latter effect can influence the throughput more than dif- ferences in basic operating capacity. It therefore follows that both capacity and leakage for alternative modes of regeneration should be evaluated before recommending specific design conditions. Presupposing that the objective of the nitrate removal treatment is to obtain potable water of a quality which meets the World Health Organization (WHO) limit, where the nitrate/(nitrate + sulphate) ratio is higher than 0.6, a nitrate selective resin is not necessary. A standard strong base resin can give higher throughputs as a result of its higher total capacity. It will be seen that up to the ratio of 0.6 the curves in Figs. 3 - 6 are continuous to show where Purolite A-520E is the recommended resin. The discontinuous curves are given so that comparisons may be made with alternative resins. Where lower leak- ages than the WHO limit are required, for example in the processing of certain foods, Purolite A-520Ewill often give a superior performance to the standard resins even where nitrate/(nitrate + sulphate) ratios are higher than 0.6. One particular advantage here is that there is no slug of highly concentrated nitrate at breakthrough as is found with standard resins, hence the possibility to excessively contaminate the food product by overrun- ning the bed is avoided. (L) (L p) Page 6 of 8 Depending upon the throughput requirement the resin volume is chosen so as to operate within the flow rate stipulations given in the standard operating conditions above. A design factor of 0.9 is also recommended as is customary. Hence throughput/liter of resin for design pur- poses will be 313 x 0.9 = 281.7 liters (2124 U.S. gal/ft 3). In this example the leakage is 17.3 ppm as CaCO 3(21.4 ppm as NO 3), hence the useful option to blend treated water with raw water on a 50% basis could be applied. Itwould be of no advantage to move to counter-current regeneration in this case. Reference to Fig. 5 will show that the basic capacity curve is very similar. However the throughput will be lower, because the reduced leakage increases the ion exchange load for a given throughput. When on the other hand nitrate concentrations or ratios are higher, it may be advantageous to operate counter-current rather than increase the regeneration level while operating co-current. In this way a suitable blend may be obtained with lower regenerant costs (and costs of disposal). WATER ANALYSIS Anions ppm meq/l ppm as CaCO 3Cations ppm meq/l Nitrate 93 1.5 76 Calcium 90 4.5 Sulphate 98 2.0 100 Magnesium 18 1.5 Chloride 71 2.0 100 Sodium 30 1.3 [HCO 3* 122 2.0 100 ] Potassium 8 0.2 Total Anions 7.5 Total Cations 7.5 Equivalent Mineral Acidity (EMA) 5.5 *Note: Unless concentration of bicarbonates is well above average it does not affect the performance to a significant extent. A regeneration level of 125 g NaCl/l has first been chosen, using co-current regeneration. To calculate the cyclic throughput from the equations given above; From Fig. 3, Base Capacity at 0.43 for = 0.36 eq/l From Fig. 4, Leakage at = 23% Hence for each litre of resin, throughput = (0.36/1.15) x 10 3liters = 313 liters And for each cubic foot of resin, = [7.9/(0.058 x 57.7)] x 10 3 = 2360 U.S. gal. Nitrate NO 3 - 76 Nitrate + Sulphate NO 3 -+ SO 4 = 76 + 100 = = = 0.43 NO 3 - NO 3 -+ SO 4 = 0.43 NO 3 - NO 3 -+ SO 4 = How to use Figs. 3 through 6. It is assumed that it is required to treat a well water of the following analysis to produce a nitrate concentration of less than 50 mg/l. EXAMPLE OF CALCULATION Page 7 of 8 NOTES ION EXCHANGE RESINS ? WORLDWIDE OFFICES USA: www.puroliteUSA.com International: www.purolite.com All suggestions and recommendations given above concerning the use of Purolite products are based on tests and data believed to be reliable. However, as Purolite cannot control the use of its products by others, no guarantee is either expressed or implied by any such suggestion or recommendation by Purolite nor is any information contained in this leaflet to be construed as a recommendation to infringe any patent currently valid. A-520E/1299/SOP U.S.A.The Purolite Company 150 Monument Road Bala Cynwyd, PA 19004 Phone: (1) 610-668-9090 Toll Free: 800-343-1500 Telefax: (1) 610-668-8139 Email: sales@puroliteUSA.com TEXASThe Purolite Company 1700 West Loop South Suite 740 Houston, TX 77027 Toll Free: 800-562-6488 Telefax: (1) 713-627-7890 CANADAThe Purolite Company 625 Wabanaki Drive Unit #2 Kitchener, Ontario N2C 2G3 Toll Free: 800-461 -1500 or (1) 519-896-6674 Telefax: (1) 519-896-6679 UNITED KINGDOMPurolite International Limited Kershaw House Great West Road Junction with Lampton Road Hounslow, TW5 OBU Sales Phone: (44) 181 -570-4454 Telefax: (44) 181-572-7726 European Marketing Phone: (44) 181-577-1222 Telefax (44) 181-577-1136 GERMANYPurolite Deutschland GmbH Harkort Strasse 25 40880 Ratingen Phone: (49) 2102-46033 Telefax: (49) 2102-443663 FRANCEPurolite International SARL 34 Avenue Matignon 75008 Paris Phone: (33) 1-4256-4563 Telex: 648856 Telefax: (33) 1-4563-3826 SPAINPurolite Iberica S.A. 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