1. Ion Exchange Design Calculation
2. Purolite Ion Exchange Design Calculation Program

• Jonathan Palmer
• 3 years ago
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Resources Here to. Evalutating the contribution of the column design to the ion exchange performance by calculation of. At puredesign@purolite.com, for the. Ion Exchange Design Hand calculation. Brian Windsor (Purolite International Ltd) Ion Exchange Design Hand calculation. Program Report No. 124 ION EXCHANGE.

1 Ion Exchange Design Hand calculation Brian Windsor (Purolite International Ltd)

2 Introduction Before design programmes were introduced, every engineer had to calculate the design by hand using resin manufacturers data. Each engineer had their own way to carry out in their calculation. Before starting the design ideally you need to know some basic information: 1. Maximum / Average / Minimum flow rate and roughly how many hours per day the maximum flow rate is required (m 3 /h). 2. Daily requirement (m 3 /day) over how many hours. 3. Design water analysis 4. Cation regenerant (sulphuric or hydrochloric acid)

3 Flow rate 1. If the maximum demand is for a short period, or if there is a wide range of operating flow rates, then you can design the plant on the average demand and include a larger treated water storage to cater for the maximum flow rate or variations in demand. 2. It is always to keep the plant in operation rather than operating on an on-off basis with lots of stopping and starting. 3. Resins can operate over a range of flow rates, but the design of ion exchange columns is often very basic and many cannot accommodate very low flow rates. Poor distribution / collection is often encountered at low flow rates leading to channelling and poor performance.

4 Cycle Time / No of Streams The cycle time for each cation anion pairing is determined by the water analysis, flow rate and number of streams. Where demineralised water is critical to the sites operation then normally the client will require a standby stream to cover for regeneration time of the other stream(s) and allow some basic maintenance. Most commonly encountered plants are therefore 2 x 100% or 3 x 50% duty, but where very high flow rates are encountered 4 x 33% duty and 5 x 25% duty streams have been supplied. A cation anion pair can be regenerated in under 2 hours if simultaneous regeneration is employed and with short cycle plant it is even quicker. Mixed beds are more complicated, but are regenerated less frequently and usually take 2 to 3 hours.

5 Cycle Time / No of Streams Ignoring short cycle plants, then classical designs are often base on 8 or 12 hours on line between regenerations depending on the water analysis used for the design. Longer cycle times are encountered when the raw water TDS is low. Such thin waters often see plants designed on 24 hours on line or even longer. We will now select the basis for our design calculations.

6 Design Analysis 1. Knowledge of the maximum and typical analysis is critical when choosing the cycle time. No point choosing short cycle time on the design analysis if the worst water has a much higher TDS. This will mean the time between regenerations is too short. 2. The analysis should balance i.e. The cations and anions expressed as mg/l CaCO 3 or in meq/l should be very similar (within 5%) 3. You have to design the plant to cope with the worst water, but if that water is very infrequently seen then all design operating costs and design decisions need to be based on the typical water analysis.

7 Maximum Water Analysis (Worst Water) If designed on the worst water analysis presented by the end user the water may not balance as the client may have cherry picked the highest recorded level for each ion. These highest level for all ions will not occur on the same day and hence it will not balance. Then you can round down the highest category to give the balanced analysis as naturally occurring waters must balance. In our calculation the end user has given us the analysis of his anticipated worst water.

8 Design Basis for this Calculation Flow Rate 60 m3/h (for 24 hours per day) Important application so standby stream required 2 x 100% duty. Hydrochloric acid for cation regeneration. Water temp 10 centigrade. Worst Water Analysis from client (all expressed in mg/l as CaCO 3.) Cations Anions Calcium (Ca) 110 Bicarbonate (HCO 3 ) 100 Magnesium (Mg) 55 Sulphate (SO 4 ) 50 Sodium (Na) 100 Chloride (Cl) 75 Potassium (K) 11 Nitrate (NO 3 ) 25 TOTAL CATIONS 276 TOTAL ANIONS 250 Greater than 10% difference!

9 Design Basis Corrected Analysis Corrected Worst Water Analysis to balance (all expressed in mg/l as CaCO 3) ) Cations Anions Calcium (Ca) 100 Bicarbonate (HCO 3 ) 100 Magnesium (Mg) 50 Sulphate (SO 4 ) 50 Sodium (Na) 90 Chloride (Cl) 75 Potassium (K) 10 Nitrate (NO 3 ) 25 TOTAL CATIONS 250 TOTAL ANIONS 250 Design analysis to go forward In addition we will assume a Reactive Silica of 5 mg/l as CaCO 3. It is a ground water and contains negligible dissolved organics.

10 Degassing tower The inclusion of a degassing tower to remove the bicarbonate after the cation, when it is converted to carbonic acid, has to be decided before the design is commenced. If the bicarbonate level is above 40 mg/l as CaCO 3 then it is normally cost effective to include a degasser, this is particularly the case on engineered design where a neutral effluent is often required from the waste water produced and plant costs are greater. However, on small, low flow rate, standard plants many companies do not supply a degasser as the capital cost associated with the tower, degassed water pumps (stainless steel) makes the pay back period less attractive and here all the bicarbonate load is often removed by the anion stage. On this design with 150 mg/l bicarbonate we will have a degasser tower.

11 Design Approach In all cases however you have to design from the back of the plant. If you have a cation anion mixed bed system then you start with mixed bed calculation, then anion and then the cation. This way you can calculate or estimate the waste water required which must pass through the preceding unit during the design. For this example I will assume a simple co-flow regenerated system of cation anion followed by a polishing mixed bed. Counter flow regeneration is a little more complicated as you have to estimate the additional treated water required for regenerant injection and slow rinses on the cation and anion beds.

12 Polishing Mixed Bed - Design basis After SAC / SBA resins the loading on to polishing mixed beds is very low and so these units are sized on flow rate which makes it very simple. The basis I use is: Vessel sizing based on specific velocity of 60 m 3 /m 2 /h. 600 mm minimum bed depth for cation / anion components. Anion regeneration level 65 g/l with cation regen level designed to give substantially self neutralising effluent. Depending on cation load, approx. 62 g/l for HCl and 80 g/l for sulphuric acid gives a neutral effluent. If not worried about neutral effluent then regen levels as low as 60 g/l NaOH and 48 g/l HCl or H 2 SO 4 have been used.

13 Polishing Mixed Bed - Sizing Applying these parameters to 60 m 3 /h flow rate then: 60 m 3 /h divided by 60 m/h = Minimum area 1 m 2 required. Hence based on UK vessel sizing = 1219 mm diameter (1.16 m 2 ) Resin volume per unit = 0.6 m x 1.16 m 2 = m3 (696 litres) Rounded up to the nearest 25 litres = 700 litres of each component. Caustic applied at 65g/l regen level = 65g/l x 700 / 1000 = 45.5 Kg (as 100% NaOH). HCl applied at 63 g/l regen level = 63 g/l x 700 / 1000 = 44.1 Kg (as 100% HCl). (Metric Sizing 1200 mm diameter with 675 litres of each resin)

14 Polishing Mixed Bed - Operation Mixed beds should never be run near to exhaustion due to the long run length this has little effect on plant operating costs. Historically I tend to use the following guide capacities to determine run length of a polishing mixed bed based on the cation / anion leakage. Anion reactive silica loading should not exceed 9 g/l (6 g/l used by some) Cation sodium loading should not exceed 15 g/l. These are highly conservative. Hence good quality obtained at all times!

15 Anion Design Anion analysis after Degasser Tower After the degassing tower the bicarbonate anion loading will be reduced typically to < 5 mg/l CO 2 as CaCO 3 Therefore the anion load based on the original raw water will now be: Anions Sulphate (SO 4 ) 50 Chloride (Cl) 75 Nitrate (NO 3 ) 25 Reactive Silica 5 Carbon Dioxide 5 Anion Load = 160 mg/l as CaCO 3

16 Anion Design Gross water production per cycle Early we chose 8 hour on line for the worst water. Therefore volume of water treated per cycle would be: (8 hours x 60 m) + MB regen water (Note MB normally uses between 12 and 20 BV of water per regen.) We will use 15 BV for the calculation, so with 1400 litres of resin per mixed bed it needs 15 x 1400 = litres (21 m 3 ) Therefore anion volume of treated water = (8 x 60) + 21 m 3 = 501 m 3

17 Anion Design Anion load per cycle Therefore anion volume of treated water = (8 x 60) + 21 m 3 = 501 m 3 The anion ionic load per cycle is therefore 501 m 3 x 160 mg/l / 1000 = Kg as CaCO 3 Now we have the load per cycle to calculate the resin volume we need to now calculate from the resin manufacturers data the working capacity of the resin. For the basis of this calculation, with a low organics content I am basing on a gel, polystyrenic, anion resin with a high capacity. This type of product is available from all the leading suppliers.

18 Anion Design Capacity Correction Factors For a type 2, gel, polystyrenic, anion resin the working capacity is determined by a base capacity dependent on regen level (amount of caustic applied. This capacity then has various correction factors applied and each manufacturers graphs presented differently. The percentage sulphate in the anion load. The percentage CO2 in the anion load. The silica endpoint for regeneration. The bed depth (if shallow below 0.7 m). We can ignore this with our design as with the size of plant our bed depth will be between 1 and 1.5 m. The percentage silica in the anion load and regenerant temperature. Co-flow plant regen levels tend to be between 55 and 80 g/l. However, regen levels are sometimes encountered outside this range.

19 Anion Design Base Resin Capacity For this co-flow regenerated design I have chosen a regeneration level of 60 g/l NaOH. From the resin engineering bulletin this gives a base working capacity of 0.75 eq/l. This is 37.5 g/l as CaCO 3 (0.75 x 50)

20 Anion Design Anion Capacity Adjustment Sulphate percentage in anion load 50 mg/l / 160 mg/l x 100 = 31.25%. From graph correction factor = 0.95 Carbon Dioxide percentage in anion load 5 mg/l / 160 mg/l x 100 = 3.125%. From graph correction factor = 1.00 (no effect)

21 Anion Design Anion Capacity Adjustment We can operate to a 200 ppb endpoint. From graph correction factor = 1.00 (No effect) We will have a bed depth above 0.7 m. From graph correction factor = 1.00 (No effect)

22 Anion Design Capacity (Theoretical) Silica percentage equates to 3.1% of Anion load. If we assume regenerant temperature of 10 C then from graph correction factor = If we now apply all these correction factors to the base capacity we will obtain the theoretical working capacity (Ignoring those which are 1.0 as they have no effect). Theoretical Working capacity = 37.5 g/l x 0.95 x = g/l as CaCO 3

23 Anion Design Rinse Correction Now I need to correct the capacity for the loading on to the bed caused when the resin is rinsed after regeneration with decationised water. For a co-flow regenerated anion resin I would use 6 BV final rinse (when new). Therefore the rinse correction in g/l as CaCO 3 is: 6 (bed volumes) x 160 (mg/l anion load) / 1000 = 0.96 g/l Therefore revised working capacity is now = g/l Depending on the design / actual knowledge of the water, and the engineering system being used, a smart engineer will now apply a design margin to ensure the resin manufacturers performance can be guaranteed for an operating plant for the warranty period.

24 Anion Design Design Margin / Working Capacity The selection of and the amount of design margin is critical to a well designed reliable plant. When I am doing these calculations I favour taking a larger design margin on the anion resin over the cation resin. This is because I want the plant to be cation limiting making conductivity control of the plant on exhaustion easier and also because anion resin performance usually falls off at a quicker rate than cation performance. I therefore tend to take a 10 to 15% design margin on the anion capacity and correspondingly lower 5 to 10% on the cation resin. Many engineers just take 10% design margin on both to make the plant more competitively priced etc. On this example I will apply 10% to both. Therefore anion working capacity = x 0.9 = g/l.

25 Anion Design Resin Volume If you recall we calculated back on slide 17 we calculated the anion load as Kg as CaCO 3 The resin volume required (in litres) is therefore the ionic load / the working capacity of the resin x 1000: ( / 30.07) / 1000 = 2665 litres We normally round up to nearest 25 litre bag quantity hence: 2675 litres required Anion regen level was 60 g/l. Therefore caustic applied per regen is 60 x 2675 / 1000 = Kg as 100% NaOH.

26 Cation Design Design Analysis and Water Production The cation load based on the original raw water will now be: Cations Calcium (Ca) 100 Magnesium (Mg) 50 Sodium (Na) 90 Potassium (K) 10 Cation Load = 250 mg/l as CaCO 3 The volume of water treated per cycle would be: (8 hours x 60 m) + Anion regen water + MB regen water (21 m 3 ) (Note: a co-flow anion normally uses between 10 and 12 BV of water per regen.) We will use 12 BV for the calculation, so with 2675 litres of resin per anion unit, it needs 12 x 2700 litres = litres (32.1 m 3 )

27 Cation Design - Cationic Load Therefore cation volume of treated water = (8 x 60) + 32 m m 3 = 533 m 3 The cation load per cycle is therefore 533 m 3 x 250 mg/l / 1000 = Kg as CaCO 3 Now we have the load per cycle to calculate the resin volume we need to now calculate from the resin manufacturers data the working capacity of the resin. For the basis of this calculation, I am basing on an 8% DVB cross linked, gel, polystyrenic, standard grade strong acid cation resin with a high capacity. Similar product available from all the leading suppliers.

28 Cation Design - Capacity Correction Factors For this type of resin the working capacity is determined from a base capacity dependent on regen level (amount of acid applied). This capacity then has various correction factors applied dependent on the following: The percentage bicarbonate present in influent water. The temperature of the water treated. The percentage sodium in the cation load. The kinetic loading. This will not apply as this is mainly linked to high TDS waters or high BV/h flow rates.

29 Cation Design Base Resin Capacity For this co-flow regenerated design I have chosen a regeneration level of 66 g/l HCl. This corresponds from the cation engineering bulletin to a base working capacity of 1.14 eq/l. This is 57 g/l as CaCO 3 (1.14 x 50)

30 Cation Design Cation Capacity Adjustment Bicarbonate percentage in Cation load 100 mg/l / 250 mg/l x 100 = 40%. From graph correction factor = 0.97 Design water temperature 10 C (minimum water temp) From graph correction factor = 0.96

31 Cation Design- Cation Capacity Adjustment Sodium percentage in cation load 100 mg/l / 250 mg/l x 100 = 40%. From graph correction factor = This graph applies to high TDS or high BV/h flow rates. In this design it does not apply as we are to the LHS of the graph where the factor is 1.0 (No effect).

32 Cation Design Working Capacity If we now apply all these correction factors to the base capacity we will obtain the theoretical working capacity (Ignoring those which are 1.0 as they have no effect). Theoretical Working capacity = 57 g/l x 0.97 x 0.96 x = If we now apply rinse correction for co-flow cation. I tend to use 5 BV for this calculation for a co-flow regenerated cation. = 5 BV x 250 mg/l cation load / 1000 = 1.25 g/l as CaCO 3 This gives a theoretical capacity of = g/l as CaCO 3 If we then apply 10% design margin we have a working capacity of: x 0.9 = g/l as CaCO 3

33 Cation Design Resin Volume If you recall we calculated back on slide 27 we calculated the cation load as Kg as CaCO 3 The resin volume required (in litres) is therefore the ionic load / the working capacity of the resin x 1000: ( / 47.83) / 1000 = 2785 litres We normally round up to nearest 25 litre bag quantity hence: 2800 litres required Cation regen level was 66 g/l. Therefore acid applied per regen is 66 x 2800 / 1000 = Kg as 100% HCl.

34 Checking for Neutral Effluent (Taken from earlier slides) Cation load = Kg as CaCO 3 Anion load = Kg as CaCO 3 Cation acid applied = Kg as 100% HCl Caustic applied = Kg as 100% NaOH If we convert the chemicals applied to as CaCO 3 we can establish the excess acid and caustic generated from a regeneration (Conversion factor for HCl is x 1.37 and for NaOH it is x 1.25). Acid applied = x 1.37 = Kg. Therefore excess acid is the = Kg as CaCO 3 Caustic applied = x 1.25 = Kg. Therefore excess acid is the = Kg as CaCO 3 The two excesses are similar therefore neutral effluent!

35 Checking for Neutral Effluent I CHEATED I did the calculation first before preparing the slides and this is why I selected a cation regen level of 66 g/l. I knew it gave me a neutral effluent for the calculation/presentation Otherwise this part of the hand calculation takes some time to resolve. You have to draw a graph on which you plot regeneration level against excess regenerant generated and regeneration level against resin volume. Based on this graph it is then possible to interpret the results to reach a neutral effluent but it takes some time! Probably the subject of a another presentation. THIS IS WHERE DESIGN PROGRAMMES HELP SO MUCH

36 Vessel Sizing Design Parameters Fortunately in this example co-flow cation and anion have very similar resin volumes so the sizing will be almost identical (2.675 m 3 in the anion and m 3 in the cation. For insitu regenerated co-flow regenerated plant I use the following parameters for my vessel sizing: Maximum service velocity. 50m 3 /m 2 /h (m/h) Minimum service velocity. 12m 3 /m 2 /h (m/h) Guide to maximum pressure drop at minimum temperature for a fully classified bed to allow for some compaction/fouling. 100 to 122 Kpa. Maximise bed depth within pressure drop guide but rarely would the bed depth exceed 1.75 m and preferably more than 1.0 m and never below 0.6 m. 50 to 60% freeboard above resin for co-flow backwash.

37 Vessel Sizing Using these parameters and the pressure drop curves for each resin the vessel size I would have selected the same vessel size for both columns: Metric 1600 mm diameter x 2250 mm i/s. This corresponds to 1.40 m cation and 1.34 m anion bed depth (installed) and a service velocity of 30 m 3 /m 2 /h (m/h) UK 5 feet diameter x 8.25 feet i/s This corresponds to 1.54 m cation and 1.47 m anion bed depth (installed) and a service velocity of 33 m 3 /m 2 /h (m/h)

38 Pressure Drop Across Resin Beds We know the bed depths 1.4 m (cation) and 1.34 m (anion) and because the vessels are the same diameter the velocity of the water through each bed is the same (30 m 3 /m 2 /h (m/h)). If we assume the minimum water temperature is 10 C in the winter, we can now calculate the pressure drop from a single graph for each resin which is based on the. Velocity Water Temperature Bed Depth

39 Pressure Drop Across Resin Beds Anion Resin Example Different graph for cation resin At a velocity of 30 m/h and temperature of 10 C (green line) we can read of the pressure drop. In this case the answer is 46 kpa/m. Our bed depth is 1.34 m so pressure drop across a clean, fully classified, not compacted bed is 46 x 1.34 = Kpa. For my pump calculations I add a safety margin between 10 and 20% depending on how free of solids the water is, cycle length (compaction), resin ageing etc. Therefore pressure loss for pump is around 70 Kpa within limit.

40 Leakage from Resin Beds Cation Resin Example From the cation regen level selected, and the raw water analysis we can calculate the sodium leakage from the cation resin which allows us to establish the conductivity exit the anion. Reactive silica leakage from anion makes no contribution to the anion outlet conductivity. Similar to the capacity calculation the leakage starts with the base leakage based on the regeneration level. Then we apply factors. In this case the factors are: 1. The EMA present in the feed in meq/l. (EMA = Sulphate + Nitrate + Chloride) 2. The % Sodium in the feed as CaCO3.

41 Leakage from Resin Beds Cation Resin Example Regen level selected 66g/l. From slide 9: Sodium % in feed 90/250 = 36% EMA level in meq/l 150 mg/l / 50 = 3.0 Sodium Leakage 7 mg/l x 0.35 x 0.75 = 1.83 mg/l Therefore average leakage 2 mg/l as Na

42 Leakage from Resin Beds Anion Resin From the anion regen level selected, and the raw water analysis we can calculate the reactive silica leakage from the anion resin. Similar to the cation calculation the leakage starts with the base leakage based on the regeneration level. Then we apply factors. In this case there are five factors which are: 1. The % Reactive Silica to Total Anions. 2. Feed Water Temperature (Highest temp gives highest leakage correction). 3. Regenerant Temperature (Highest temp gives lowest leakage correction). 4. Sodium leakage from cation in mg/l Na. 5. Silica end point.

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