MEMBRANE
PROCESSES
Common membrane processes include ultrafiltration
(UF), reverse osmosis (RO ), electrodialysis (ED), and electrodialysis rever
sal (EDR). These processes (with the exceptio n of UF) reduce most ions; RO and
UF system s also provide efficient reduction of nonionizzed organics and
particulates. Because UF mem brane porosity is too large for ion rejection, t
he UF process is used to reduce contaminants, such as oil and grease, and
suspended solids.
Reverse
Osmosis
Osmosis is the flow of solvent through a
semi-permeable membrane, from a di lute solution to a concentrated solution.
This flow results from the driving force created by the difference in pressure
between the two soluti ons. Osmotic pressure is the pressure that must be added
to the concentrated solution side in o rder to stop the solvent flow through
the membrane. Reverse osmosis is the process of rev ersing the flow, forcing
water through a membrane from a concentrated solution to a dilute solution to
produce filtered water.
Reverse osmosis is
created when sufficient pressure is applied to the concen trated solution to
overcome the osmotic pressure. This pressure is provided by feedwater pumps.
Concentrated contaminants (brine) are reduced from the high-pressure side of
the RO membrane, and filtered water (permeate) is reduced from the low-pressure
side. Figure 9-2 is a simpli fied schematic of an RO process. Membrane mod ules
may be staged in various design configur ations, producing the highest-quality
permeate wi th the least amount of waste.
Typically, 95% of dissolved salts are reduced from
the brine. All particulates are removed. However, due to their molecular
porosity, RO membranes do not remove dissolved gases, such as Cl2,
CO2, and O2.
RO Membranes. The two most common RO membranes used
in industrial water treatment are cellulose acetate (CA) and polyamide (PA)
composite. Currently, most membranes are spiral wound; however, hollow fiber
configurations are available. In the spiral wound configuration, a flat sheet
membrane and spacers are wound around the permeate collection tube to produce
flow channels for permeate and feed water. This design maximizes flow while
minimizing the membrane module size.
Hollow fiber systems are bundles of tiny, hair-like
membrane tubes. Ions are rejected when the feedwater permeates the walls of
these tubes, and permeate is collected through the hollow center of the fibers.
Concentrated brine is produced on the outside of the fibers contained by the
module housing.
Electrodialysis
Electrodialysis (ED) processes transfer ions of
dissolved salts across membranes, leaving purified water behind. Ion movement
is induced by direct current electrical fields. A negative elec-trode (cathode)
attracts cations, and a positive electrode (anode) attracts anions. Systems are
compartmentalized in stacks by alternating cation and anion transfer membranes.
Alternating compartments carry concentrated brine and filtered permeate.
Typically, 40-60% of dissolved ions are removed or rejected. Further
improvement in water quality is obtained by staging (operation of stacks in
series). ED processes do not remove particulate contaminants or weakly ionized
contaminants, such as silica. Figure 9-6 is a simplified schematic of an ED
process.
Electrodialysis
Reversal
Electrodialysis reversal (EDR) processes operate on
the same principles as ED; however, EDR operation reverses system polarity
(typically 3-4 times per hour). This reversal stops the buildup of concentrated
solutions on the membrane and thereby reduces the accumulation of inorganic and
organic deposition on the membrane surface. EDR systems are similar to ED
systems, designed with adequate chamber area to collect both product water and
brine. EDR produces water of the same quality as ED.
Ultrafiltration
In many process and
wastewater applications, reduction of dissolved ions is not required but
efficient reduction of colloidal inorganic or organic molecules is.
Ultrafiltration (UF) membrane configurations and system designs are similar to
those used in the single-stage RO process. Because the large molecules removed
by UF exhibit negligible osmotic pressure, operating pressures are usually much
lower than in RO systems. Figure 9-7 illustrates the performance of
ultrafiltration membranes. Typical applications include reduction of oil and
grease and recovery of valuable contaminants in process waste streams.
PRETREATMENT
Processes that rely on microporous membranes must be
protected from fouling. Membrane foul- ing causes a loss of water production
(flux), reduced permeate quality, and increased trans-membrane pressure drop.
Membrane fouling is typically caused by
precipitation of inorganic salts, particulates of metal oxides, colloidal silt,
and the accumulation or growth of microbiological organisms on the membrane
surface. These fouling problems can lead to serious damage and necessitate more
frequent replacement of membranes.
SOLIDS
REDUCTION
Membrane feedwater should be relatively free from
colloidal particulates. The most common particulates encountered in industrial
membrane systems are silt, iron oxides, and manganese oxides.
Silt Density Index (SDI) testing should be used to
confirm sufficient water quality for the specific membrane system employed. SDI
evaluates the potential of feedwater to foul a 0.45 µm filter. Unacceptable SDI
measurements can be produced even when water quality is relatively high by most
industrial water treatment standards. Where pretreatment is inadequate or
ineffective, chemical dispersants may be used to permit operation at
higher-than-recommended SDI values. RO systems are highly susceptible to
particulate fouling, ED and EDR systems are more forgiving, and UF systems are
designed to handle dirty waters.
SCALE
CONTROL
Membrane processes produce a concentration gradient
of dissolved salts approaching the membrane surfaces. The concentration at the
membrane may exceed the solubility limits of certain species. Calcium carbonate
(CaCO3) and calcium sulfate (CaSO4) are typical
precipitates formed. Silica, barium, and strontium salts are also frequently
identified in membrane deposits. Because of their low solubility, very low
levels of feedwater barium or strontium can cause membrane fouling.
Various saturation indexes, such as the Stiff-Davis
and Langelier, should be maintained below precipitating values in the brine
(through pH control or deposit control agents) to prevent calcium carbonate
fouling. Other precipitates may be controlled by the proper application of
deposit control agents.
MICROBIOLOGICAL
FOULING
Cellulose acetate membranes can be degraded by
microbiological activity. Proper maintenance of chlorine residuals can prevent
microbiological attack of these membranes.
Polyacrylamide
membranes are resistant to microbiological degradation; however, they are
susceptible to chemical oxidation. Therefore, chlorination is not an acceptable
treatment. If inoculation occurs, microbiological fouling can become a problem.
Nonoxidizing antimicrobials and biodispersants should be used if serious
microbiological fouling potential exists.
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