Cold Lime Softening

COLD LIME SOFTENING

Cold lime softening, also known as Clark’s process, is used to reduce raw water hardness, alkalinity, silica, and other constituents. This helps prepare water for direct use as cooling tower makeup or as a first-stage treatment followed by ion exchange for boiler makeup or RO Reject recycle. The water is treated with lime or a combination of lime and soda ash (carbonate ion). These chemicals react with the hardness and natural alkalinity in the water to form insoluble compounds. The compounds precipitate and are removed from the water by sedimentation/clarification. Waters with moderate to high hardness and alkalinity concentrations (150-500 ppm as CaCO3) are often treated in this fashion.

Chemistry of Precipitation Softening

In almost every raw water supply, hardness is present as calcium and magnesium bicarbonate, often referred to as carbonate hardness or temporary hardness. These compounds result from the action of acidic, carbon dioxide laden rain water on naturally occurring minerals in the earth, such as limestone. For example:

CO2 + H2O = H2CO3

H2CO3 + CaCO3 ¯ = Ca(HCO3)2 Cold Lime Softening Lime softening accomplished at ambient temperatures is referred to as cold lime softening. When hydrated lime, Ca(OH)2, is added to the water being treated, the following reactions occur:

CO2 + Ca(OH)2 = CaCO3 ¯ + H2O

Ca(HCO3)2 + Ca(OH)2 = 2CaCO3 ¯ + 2H2O

Mg(HCO3)2 + 2Ca(OH)2 = Mg(OH)2 ¯ + 2CaCO3 ¯ + 2H2O If the proper chemical control is maintained on lime feed, the calcium hardness may be reduced to 35-50 ppm. Permanent calcium hardness is not affected by treatment with lime alone. If non carbonate magnesium hardness is present in an amount greater than 70 ppm and an excess hydroxyl alkalinity of about 5 ppm is maintained, the magnesium will be reduced to about 70 ppm, but the calcium will increase in proportion to the magnesium reduction. For example, in cold lime treatment of a water containing 110 ppm of calcium, 95 ppm of magnesium, and at least 110 ppm of alkalinity (all expressed as calcium carbonate), calcium could theoretically be reduced to 35 ppm and the magnesium to about 70 ppm. However, an additional 25 ppm of calcium would be expected in the treated water due to the following reactions:

MgSO4 + Ca(OH)2 = Mg(OH)2 ¯ + CaSO4

MgCl2 + Ca(OH)2 = Mg(OH)2 ¯ + CaCl2 To improve magnesium reduction, which also improves silica reduction in cold process softening, sodium aluminate may be used. The sodium aluminate provides hydroxyl ion (OH-) needed for improved magnesium reduction, without increasing calcium hardness in the treated water. In addition, the hydrolysis of sodium aluminate results in the formation of aluminium hydroxide, which aids in floc formation, sludge blanket conditioning, and silica reduction. The reactions are as follows:

Na2Al2O4 + 4H2O = 2Al(OH)3 ¯ + 2NaOH

Mg [ SO4 ] + 2NaOH = Mg(OH)2¯ + [ Na2SO4 ] Cl2 2NaCl Soda ash (Na2CO3) is also used to improve hardness reduction. It reacts with non-carbonate calcium hardness according to the following:

CaSO4 + Na2CO3 = CaCO3 ¯ + Na2SO4

CaCl2 + Na2CO3 = CaCO3 ¯ + 2NaCl However, permanent magnesium hardness reduction in cold process softening requires added lime. The reactions are as follows:

MgSO4 + Ca(OH)2 + Na2CO3 = Mg(OH)2 ¯ + CaCO3 ¯ + Na2SO4

MgCl2 + Ca(OH)2 + Na2CO3 = Mg(OH)2¯ + CaCO3 ¯ + 2NaCl In these reactions, dissolved solids (TDS) are not reduced because a solution reaction product (sodium sulfate or sodium chloride) is formed.

Reduction of Other Contaminants

Lime softening processes, with the usual filters, will reduce oxidized iron and manganese to about 0.05 and 0.01 ppm, respectively. Raw water organics (colour-contributing colloids) are also reduced. Turbidity, present in most surface supplies, is reduced to about 1.0 NTU with filtration following chemical treatment. Raw water turbidity in excess of 100 NTU may be tolerated in these systems; however, it may be necessary to coagulate raw water solids with polyelectrolyte. Oil may also be removed by adsorption on the precipitates formed during treatment. However, oil in concentrations above about 30 ppm should be reduced before lime treatment because higher concentrations of oil may exert a dispersing influence and cause floc carryover.

Equipment Employed

Continuous sludge-contact softeners are used to provide a constant flow with effluent quality superior to that obtained through batch treatment. Treating chemicals are added as a function of flow rate and water quality to the rapid mix zone of the unit. Sludge, recirculated either internally or externally to the unit, may be returned to this rapid mix zone for improved softening, softened water clarity, and silica reduction. The water then flows to the slow mix zone of the unit. Here, the precipitation reactions continue and the precipitates formed become large enough to begin settling. In the sludge-contact unit, the water flows through a bed of sludge for additional contact. The sludge level is maintained by the proper combination of sludge bed conditioning chemicals, mechanical agitation, hydraulic suspension, and sludge blowdown. A discernible line of separation between clarified water and slurry pool should exist in a properly operated unit. Effluent turbidity is usually less than 10 NTU. Flow rate is usually limited to less than 1.5 gpm/ft2 of settling area. A retention time of 1- 1.5 hrs is required to allow the softening reactions to come as close to completion as possible. Because the reactions in cold process softening are not complete, the water contaminant levels leaving the unit are unstable. With additional time and/or increased temperature, further precipitation will occur downstream of the unit. Frequently, acid or carbon dioxide is added to stabilize the water. The pH is reduced from about 10.2 to between 8.0 and 9.0, which converts the carbonate to the more soluble bicarbonate.

Limitations

Given proper consideration of raw water quality and ultimate end use of the treated water, the application of precipitation processes has few limitations. However, operational difficulties may be encountered unless the following factors are controlled: Temperature. Cold and warm units are subject to carryover if the temperature varies more than 4°F/hr (2°C/hr). Hot process units are less sensitive to slight temperature variations. Hydraulics. In any system, steady-state operation within design limits optimizes the performance of the equipment. Rapid flow variations can cause severe system upsets. Suitable treated water storage capacity should be incorporated into the total system design to minimize load swings on the softener. Chemical Control. This should be as precise as possible to prevent poor water quality. Because of the comparatively constant quality of most well waters, changes in chemical feed rates are largely a function of flow only. However, surface water quality may vary hourly. Therefore, for proper control, it is imperative that users perform frequent testing of the raw water as well as the treated effluent, and adjust chemical feed accordingly.