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.
Ion Exchange Process Design Joe Woolley Watercare International Ltd Aim of ion exchange process To reduce the Total Dissolved Solids (TDS) of the water to that specified for subsequent use. Water Composition
Trouble Shooting Ion Exchange Plant Problems Brian Windsor (Purolite International Ltd) Introduction This presentation is centred on 7 flow diagrams which can be used to track down the cause of Ion exchange
Ion Exchange RESIN SELECTION Marc Slagt Technical Support Specialist DOW Water & Process Solutions I WILL BRING YOU HAPPINESS!! Resin selection = HAPPINESS Why happiness... When it comes to resin selection
Resin Types and Production Brian Windsor (Purolite International Ltd) Properties of an Ion Exchanger Synthetic Ion Exchangers require certain properties to perform demineralisation. The three main properties
ION EXCHANGE RESINS C-1E Strong Acid Cation Exchange Resin (For use in water softening applications) Lenntech firstname.lastname@example.org www.lenntech.com Tel. +31-15-61.9. Fax. +31-15-61.6.89 Technical Data PRODUCT
Deionized Water (DI) DEIONIZATION IN A "NUT SHELL" City water is passed through dark amber colored, caviar sized plastic beads called cation ion exchange resin. The cation resin is in the hydrogen form
ION EXCHANGE FOR DUMMIES An introduction Water Water is a liquid. Water is made of water molecules (formula H 2 O). All natural waters contain some foreign substances, usually in small amounts. The water
Dow Water Solutions DOWEX HCR-W2 and HGR-W2 Ion Exchange Resins Engineering Information DOWEX HCR-W2 and HGR-W2 Strong Acid Cation Exchange Resin General Information DOWEX HCR-W2 and DOWEX HGR-W2 strong
Dow DOWEX Ion Exchange Resin DOWEX Engineering Information July 2003 DOWEX Weak Acid Cation Exchange Resin General Information DOWEX* resin is a high capacity, macroporous weak acid cation exchange resin
Lewatit MP 62 is a weakly basic, macroporous anion exchange resin with tertiary amine groups (monofunctional), hence of particularly low basicity, and of standard bead size distribution. Its high total
GUIDELINES FOR SELECTING RESIN ION EXCHANGE OR REVERSE OSMOSIS FOR FEED WATER DEMINERALISATION Prepared by: Purolite International Date: November 2003 Operating Puropack Plant 2 GUIDELINES FOR SELECTING
METHODS OF PURIFICATION (B) ION-EXCHANGE The process of Ion-Exchange In the context of water purification, ion-exchange is a rapid and reversible process in which impurity ions present in the water are
Dow Liquid Separations DOWEX MARATHON A Ion Exchange Resin ENGINEERING INFORMATION DOWEX MARATHON A Type 1 Strong Base Anion Exchange Resin General Information DOWEX* MARATHON* A resin is a high capacity,
Dow Liquid Separations DOWEX SBR-P Ion Exchange Resin ENGINEERING INFORMATION DOWEX SBR-P Type 1 Strong Base Anion Exchange Resin General Information DOWEX* SBR-P resin is a gel type 1 strong base anion
Lewatit DW 630 is a strongly basic macroporous anion exchange resin (type I) with beads of uniform size (monodisperse) based on polystyrene. The resin has been thouroughly washed with sulfuric acid and
ION EXANGE RESINS Ion exchange resins are polymers that are capable of exchanging particular ions within the polymer with ions in a solution that is passed through them. This ability is also seen in various
International Journal of Water Resources and Environmental Engineering Vol. 3(2), pp. 52-56, February 2011 Available online at http://www.academicjournals.org/ijwree ISSN 2141-6613 2011 Academic Journals
Dow DOWEX MARATHON MSA Ion Exchange Resin Engineering Information DOWEX MARATHON MSA Macroporous Type I Strong Base Anion Exchange Resin General Information DOWEX MARATHON MSA is a high capacity, macroporous,
CO2 applications for drinking water production, process water treatment and waste water treatment Dr. Dr. Hermans Hermans 03.2013 11.2009 Carbon dioxide in water is -a natural food additive, non poisonous
Application Notes Water Softening Basics Purolite Water Softening Resin Guide By: Chubb Michaud Water, passing through the atmosphere as snow or rain, picks up carbon dioxide (CO2) and other acid gases
SODIUM CATION EXCHANGE (ZEOLITE) WATER SOFTENING PROCESS A. History The name zeolite comes from the two Greek words zein and lithos which mean boiling stone. It was first applied by Granstedt, a Swedish
Dow Liquid Separations DOWEX MARATHON A2 Ion Exchange Resin ENGINEERING INFORMATION DOWEX MARATHON A2 Type 2 Strong Base Anion Exchange Resin General Information DOWEX* MARATHON* A2 resin is a high capacity,
Water and Wastewater Engineering Dr. Ligy Philip Department of Civil Engineering Indian Institute of Technology, Madras Lecture 12 Softening Last class we were discussing about coagulation and flocculation
CARBONATE CHEMISTRY AFFECTING PRODUCTION OF BEVERAGE STILL WATER Prepared by: Htec Systems, Inc. 561 Congress Park Drive Dayton, Ohio 45459 937 438-3010 December 2005 TABLE OF CONTENTS 1.0 SUMMARY... 1
FE REVIEW: ENVIRONMENTAL ENGINEERING Y. T. Wang Chemical Equilibrium and Stoichiometry 1. The chloride (C1 - ) concentration in a lake is found to be 10-2 M. The HgC1 2 (aq) concentration is found to be
Application Data Sheet ADS 4900-87/rev.B January 2009 Power Industry Inferred ph in Steam Plant Water Chemistry Monitoring INTRODUCTION Inferred ph means ph calculated from straight and cation conductivity.
1.85 WATER AND WASTEWATER TREATMENT ENGINEERING HOMEWORK 5 Question 1 (4 points) The water defined by the analysis given below is to be softened by excess-lime (and soda ash) treatment. a. Sketch an meq/l
APPLICATION GUIDE Choosing an ion exchange system for nitrate removal Nitrate levels are coming under stricter control due to health and environmental concerns. Ion exchange technology not only effectively
TOPIC 10. CHEMICAL CALCULATIONS IV - solution stoichiometry. Calculations involving solutions. Frequently reactions occur between species which are present in solution. One type of chemical analysis called
ISR IRON REMOVAL MEDIA Description INDION ISR is a special media designed to provide excellent catalytic properties to remove dissolved iron from ground water. INDION ISR is an insoluble media which oxidizes
Experiment 9 - Double Displacement Reactions A double displacement reaction involves two ionic compounds that are dissolved in water. In a double displacement reaction, it appears as though the ions are
APPLICATION NOTE STEAM GENERATION IN POWER PLANTS Application description Water quality within power plants is of critical importance in maintaining efficient operation and in limiting downtimes due to
Guidance Leaflet Reducing water use softeners and reverse osmosis Most water supplies contain dissolved solids (e.g. salts and other minerals, particularly calcium and magnesium). The type and level of
Chapter 3 ATOMS AND MOLECULES Multiple Choice Questions 1. Which of the following correctly represents 360 g of water? (i) 2 moles of H 2 0 (ii) 20 moles of water (iii) 6.022 10 23 molecules of water (iv)
Water Softening (Precipitation Softening) (3 rd DC 178; 4 th DC 235) 1. Introduction Hardness - Multivalent metal ions which will form precipitates with soaps. e.g. Ca 2+ + (soap) Ca(soap) 2 (s) Complexation
Ion Exchange Softening Ion-exchange is used extensively in small water systems and individual homes. Ion-exchange resin, (zeolite) exchanges one ion from the water being treated for another ion that is
_ENNTEC WATER TREATMENT SOlUTioNS Industrial Water Supply Water is widely used in industry, whether it is encountered as raw water, process water or waste water. Very often make-up water must be treated
GCSE Chemistry Making Salts Instructions and answers for teachers The Activity: Learning Outcomes: To be able to recall the names and chemical formulae for commonly used acids To understand how salts can
6. A Six-Bottle Study of Ionic Compounds What you will accomplish in this experiment In last week s experiment, you observed a chemical change: a chemical reaction that resulted in a change in the composition,
The Relationship between ph and Deionized Water The basics of ph The topic of ph and water has been well documented over the years; however, there is still much confusion about its significance in high
40 Engineering Chemistry and Environmental Studies 2 SOLUTIONS 2. DEFINITION OF SOLUTION, SOLVENT AND SOLUTE When a small amount of sugar (solute) is mixed with water, sugar uniformally dissolves in water
World Bank & Government of The Netherlands funded Training module # WQ - 28 Major Ions in Water New Delhi, September 1999 CSMRS Building, 4th Floor, Olof Palme Marg, Hauz Khas, New Delhi 11 00 16 India
Water Softening for Removal 1 in Water High concentration of calcium (Ca2+) and magnesium (Mg2+) ions in water cause hardness Generally, water containing more than 100 mg/l of hardness expressed as calcium
Drinking Water Chemistry CTB3365x Introduction to water treatment Dr. ir. Doris van Halem Assistant Professor in Drinking Water This lecture Ion balance ph Carbonic acid equilibrium Saturation index (SI)
Department of Civil Engineering-I.I.T. Delhi CEL 212: Environmental Engineering Second Semester 2011-2012 Home Work 7 Solution Q1. For a single-stage softening, following water (see characteristics below)
Ion Exchange Resins for Metal Plating and Surface Finishing ION EXCHANGE RESINS Contents Introduction 5 Plating Bath Rejuvenation 6 Rinse Water Recycling 8 Waste Effluent Treatment 12 Copper Recovery 16
Wastewater Reuse Most metal finishing industries have in-house wastewater treatment to economically dispose of the acids, alkali, oils, and dissolved metals in the rinse water and occasional tank solution
T-27 Tutorial 4 SOLUTION STOICHIOMETRY Solution stoichiometry calculations involve chemical reactions taking place in solution. Of the various methods of expressing solution concentration the most convenient
WRITING CHEMICAL FORMULA For ionic compounds, the chemical formula must be worked out. You will no longer have the list of ions in the exam (like at GCSE). Instead you must learn some and work out others.
Accepted 2005 Process liquors from bleach plants Dissolved and precipitated oxalate Using Ion Chromatography 0 Introduction In bleach plants of pulp mills with a high degree of system closure, there is
: General Chemistry Lecture 9 Acids and Bases I. Introduction A. In chemistry, and particularly biochemistry, water is the most common solvent 1. In studying acids and bases we are going to see that water
TYPES OF CHEMICAL REACTIONS Most reactions can be classified into one of five categories by examining the types of reactants and products involved in the reaction. Knowing the types of reactions can help
Experiment 8 - Double Displacement Reactions A double displacement reaction involves two ionic compounds that are dissolved in water. In a double displacement reaction, it appears as though the ions are
CHEMISTRY Ionic Bonding 1 Ionic Bonding Ionic Bonds: Give and take! Ions and Ionic Bonds Atoms with five, six, or seven valence electrons usually become more stable when this number increases to eight.
More on ions (Chapters 2.1 and 3.5 3.7) Ion: an atom or molecule that has a net electrical charge. Examples: Na + (sodium ion), Cl - (chloride), NH 4 + (ammonium). Anion: a negative ion, formed when electrons
Technical Paper Technology Selection Tools for Boiler Feedwater Applications (US Units) Authors: Robert Gerard and Roch Laflamme, GE Water & Process Technologies Introduction During the last decade, the
Technical Paper Industrial Water Reuse and Wastewater Minimization Author: James P. McIntyre, P.E. Abstract Many industrial users of fresh water are under increasing pressure to reuse water within their
Case History MAR Systems Inc. Removing Thallium from Industrial FGD Scrubber Water with Sorbster Adsorbent Media Trace thallium levels in process and wastewater streams pose a human toxicity threat. Tidwell
CORROSION CONTROL OF ELECTROLYZER, ANOLYTE TANK AND DECHLORINATION TOWER TANK OF A CHLOR-ALKALI PLANT BY AN INNOVATIVE METHOD Sazal Kumar Kundu* Global Heavy Chemicals Limited (GHCL), Dhaka, Bangladesh
REMOVAL OF DISSOLVED OXYGEN FROM WATER USING THE SULPHITE FORM ANION EXCHANGE RESIN A. Tamazashvili and M.Gomelya National Technical University of Ukraine Kyiv Polytechnic Institute, Chemical Engineering
Solubility Rules and Net Ionic Equations Why? Solubility of a salt depends upon the type of ions in the salt. Some salts are soluble in water and others are not. When two soluble salts are mixed together
Product Information DOWEX Resins as Organic Solvent Desiccants DOWEX* ion exchange resins can be used as desiccants for organic solvents, after having been dried to a low moisture level, in a manner similar
Improving Silica Removal By EDI and GTM January 16, 2014 August 27, 2014 McIlvaine Michael J. Snow, Ph.D. President SnowPure Water Technologies (USA) San Clemente, California Headquarters Electropure EDI
Water Softeners Industrial Water Purification (800) CAL-WATER By Dave Peairs, Cal Water, Technical Director Rev: 06/08/2004 Before any discussion of water softeners, we must first define what hard water
IFS INTERNATIONAL FERTILISER SOCIETY TECHNICAL CONFERENCE 2015 London 22-23 June 2015 40 YEARS EXPERIENCE USING ION-EXCHANGE TO TREAT AND RECOVER CONTAMINATED PROCESS CONDENSATE FROM AMMONIUM NITRATE PLANTS
Chapter 17 Acids and Bases How are acids different from bases? Acid Physical properties Base Physical properties Tastes sour Tastes bitter Feels slippery or slimy Chemical properties Chemical properties
TECHNICAL PAPER 161 A New Ion Exchange Process For Softening High TDS Produced Water SPE/Petroleum Society of CIM/CHOA Paper Number 78941 Calgary, Alberta - November, 2002 Craig J. Brown, P.Eng., Michael
1 Index 1. Inspection and monitoring... 3 1.1 Handling of new elements... 3 1.1.1 Storage of original packaged RO elements... 3 1.1.2 Packing... 3 1.2 Initial start- up checks of a plant... 3 1.2.1 Preparation
Chapter 6: Neutralizing the Threat of Acid Rain Is normal rain acidic? Is acid rain worse in some parts of the country? Is there a way to neutralize acid rain? Acid Rain The problem Regional atmospheric
Name Date Class Atoms and Bonding Section Summary Ionic Bonds Guide for Reading What are ions, and how do they form bonds? How are the formulas and names of ionic compounds written? What are the properties
Question Bank Electrolysis 1. (a) What do you understand by the terms (i) electrolytes (ii) non-electrolytes? (b) Arrange electrolytes and non-electrolytes from the following substances (i) sugar solution
UPCORE System Suspended Solids Removal for Countercurrent Ion Exchange Systems Daniel B. Rice - The Dow Chemical Company, Midland, Michigan Andre Medete - Dow Deutschland Inc., Rheinmuenster, Germany Published
Application Note Power Monitoring Steam Purity in Power Plants Part 1: Using Conductivity Utility operators have long known that contaminated steam can cause severe damage to the turbine, leading to lengthy
6 Reactions in Aqueous Solutions Water is by far the most common medium in which chemical reactions occur naturally. It is not hard to see this: 70% of our body mass is water and about 70% of the surface
1 Chemical Reactions Unit 8: Chemical Reactions and Equations What are chemical reactions and how do they occur? How are chemical reactions classified? How are products of chemical reactions predicted?
Topic 4 National Chemistry Summary Notes Formulae, Equations, Balancing Equations and The Mole LI 1 The chemical formula of a covalent molecular compound tells us the number of atoms of each element present
CHEMICAL PRECIPITATION: WATER SOFTENING Submitted to: Dr. Hashsham Research Complex Engineering Department of Civil and Environmental Engineering Michigan State University East Lansing, MI 4884 Authors
Dynamic Soil Systems Part A Soil ph and Soil Testing Objectives: To measure soil ph and observe conditions which change ph To distinguish between active acidity (soil solution ph) and exchangeable acidity
DETERMINING THE ENTHALPY OF FORMATION OF CaCO 3 Standard Enthalpy Change Standard Enthalpy Change for a reaction, symbolized as H 0 298, is defined as The enthalpy change when the molar quantities of reactants
Application Data Sheet ADS 43-018/rev.D January 2010 Theory THEORY AND APPLICATION OF CONDUCTIVITY BACKGROUND Conductivity is a measure of how well a solution conducts electricity. To carry a a solution
All of the chemical changes you observed in the last Investigation were the result of chemical reactions. A chemical reaction involves a rearrangement of atoms in one or more reactants to form one or more
Module 9 : Experiments in Chemistry Lecture 38 : Titrations : Acid-Base, Redox and Complexometric Objectives In this lecture you will learn the techniques to do following Determination of the amount of