training session on water treatment
TRANSCRIPT
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COMMONLY USED TERMS IN WATER TREATMENT
1. OBR: OUTPUT BETWEEN TWO SUCCESSIVE REGENERATIONS.
2. TDS: TOTAL DISSOLVED SOLIDS
3. TSS: TOTAL SUSPENDED SOLIDS
4. HARDNESS: TOTAL OF CALCIUM & MAGNESIUM
5. FLOW RATE: VOLUME IN M3/HR REQUIRED TO BE TREATED.
6. CATIONS: POSITIVELY CHARGED IONS IN WATER.
7. ANIONS: NEGATIVELY CHARGED IONS IN WATER.
8. DM PLANT: DEIONISATION / DEMINERALIZATION PLANT.
9. EXCHANGE CAPACITY: THE CAPACITY OF RESIN TO REMOVE THE
DISSOLVED IMPURITIES.
10. REGENERATION: THE RECHARGING OF ION EXCHANGE RESIN BY
USE OF ACID OR CAUSTIC.
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COMMONLY USED TERMS IN W TER TRE TMENT
1. RO PLANT: REVERSE OSMOSIS PLANT.
2. GFD: GALLONS OF WATER FROM RO PLANT PER DAY PER FT
SQUARE AREA OF RO MEMBRANE.
3. FOULANTS: THE ELEMENTS IN WATER THAT IS LIKELY TO CAUSE
DAMAGE TO THE TREATMENT EQUIPMENT (RESIN/MEMBRANE).
4. CONDUCTIVITY: THE ELECTRONIC MEASUREMENT OF DISSOLVED
IONS.
5. CLEANING: THE CHEMICAL CLEANING OF RO MEMBRANE TO
RESTORE THE OPERATING CONDITION.
6. M3: 1000 LITRES.
7. GALLONS: US GALLONS 3.785 LITRES.
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RAW WATER APPRAISAL
SOURCES LIKE BORE WELL,SHALLOWWELL,RIVER,LAKE,SEA,MUNICIPAL.
DIFFERENT SOURCES HAVE DIFFERENTCHARACTERISTICS.
IONIC IMPURITIES VARY FROM SOURCETO SOURCE. TWO WELLS IN SAMEPREMISES SHALL BE DIFFERENT.
IMPURITIES: SOLUBLE,NON-SOLUBLE,ORGANIC ORIGIN.
IMPORTANT TO UNDERSTAND RAWWATER.
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RAW WATER SOURCES & THEIR PECULIARITIES
SOURCE DISSOLVEDIMPURITIES
SUSPENDEDIMPURITIES
ORGANICIMPURITIES
DEEP WELLWATER
HIGH LOW LOW
SHALLOW WELL
WATER
MODERATE LOW MODERATE
RIVER LOW HIGH -SEASONAL
MODERATE
LAKE MODERATE MODERATE HIGH
SEA V. HIGH MODERATE MODERATE
MUNICIPAL LOW LOW LOW
EFFLUENT HIGH HIGH HIGH
NOTE: THIS IS TO GIVE THE GENERAL IDEA. THERE CAN BE EXCEPTIONS.
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CLASSIFICATION OF RAW WATER ANALYSIS INVARIOUS CATEGORIES
NONDISSOLVEDIMPURITY
TSS, TURBIDITY, COLLOIDALSILICA, COLOR, SMELL
DISSOLVEDIMPURITY
TDS, CALCIUM, MAGNESIUM,SODIUM, SILICA, CHLORIDES,
SULPHATES, NITRATES,ALKALINITY, TOTAL HARDNESS
ORGANICIMPURITY
COD, BOD, COLOR, SMELL
TOTALHARDNESS
CALCIUM, MAGNESIUM
EACH OF THESE REQUIRES DIFFERENTTREATMENT FOR REMOVAL.
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WATER TREATMENT METHODS AVAILABLE & WHICH IMPURITYIT CAN REMOVE.
TREATMENTMETHOD
IMPURITIES REMOVED
TUBE SETTLER &CLARIFIERS
TSS, TURBIDITY, COLLOIDAL SILICA
FILTERS TSS, TURBIDITY
SOFTENER TOTAL HARDNESS
DM PLANTS TOTAL HARDNESS, TOTAL DISSOLVEDSOLIDS, CALCIUM, MAGNESIUM, SILICA,ALKALINITY, CHLORIDES, SULPHATES
RO PLANTS TOTAL HARDNESS, TOTAL DISSOLVEDSOLIDS, CALCIUM, MAGNESIUM, SILICA,ALKALINITY, CHLORIDES, SULPHATES
CHLORINATION BOD & COD
ACTIVATEDCARBON FILTER
FREE CHLORINE, COD, BOD, COLOR, SMELL
DEGASSER TOWER ALKALINITY
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WHICH METHOD OF TREATMENT
TO CHOOSE ? RAW WATER ( INLET ) PARAMETERS
TREATED WATER QUALITY REQUIRED
APPLICATION OF TREATED WATER
ECONOMIC OPERATIONAL COST
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FILTERS: Diameter (Mtrs.)=
(FLOW RATE M 3 /HR / VELOCITY M/HR)0.785
HEIGHT OF FILTERS IS USUALLY FIXED AT 1500 MM OR2000 MM.
SOFTENER: REQUIRES SOME CALCULATIONS ASFOLLOWS:FLOW RATE IN M3/HR = FDURATION BETWEEN REGENERATION HRS = THENCE OUTPUT BETWEEN REGENERATION= F X T
REFER TO SOFTENER RESIN GRAPHS TO GETREGENERATION LEVEL = SAY 150 G/LEXCHANGE CAPACITY = SAY @ 50
HENCE QUANTITY OF RESIN REQUIRED IN SOFTENER (
LITRES):
= OUTPUT BETWEEN REGENERATION NET EXCHANGE CAPACITY
SELECT THE SOFTENER WITH THE NEAREST RESINQUANTITY FROM SOFTNER CHART.
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SIZING
RO PLANTS: REQUIRES DETAILED CALCULATIONS.
STEPS AS FOLLOWS:
DATA COLLECTION:FLOW RATE IN M3/HRDETAILED CATION & ANIONIC ANALYSISHOURS OF OPERATIONSQUALITY OF WATER REQUIRED
DESIGN STEPS:RO PROJECTION FROM SOFTWAREDECIDE ON THE OVERALL SCHEMEEQUIPMENT SIZINGCHEMICAL CONSUMPTION SIZING
CALCULATIONS
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COMMONLY OCCURING PROBLEMS IN A WATERTREATMENT SYSTEM
1. REDUCTION IN FLOW RATES
2. REDUCTION IN THE OUTPUT BETWEEN REGENERATION
3.
QUALITY DETERIORATION
4. LEAKAGES & OTHER MECHANICAL PROBLEMS
5. PROBLEMS RELATING TO INSTRUMENTS & CONTROL
6. CHOCKING OF FILTERS & MEDIA LEADING TO FREQUENTBACKWASH.
7. HIGH PRESSURE DROP
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IT IS ESSENTIAL TOUNDERSTAND THE
CONSTRUCTIONAL DETAILS &OPERATING STEPS IN ORDERTO SOLVE THE PROBLEM
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EQUIPMENT DESCRIPTION
FOR FILTERS PRESSURE VESSEL INLET DISTRIBUTION SYSTEM
BOTTM COLLECTION SYSTEM SUPPORT MEDIA FILTRATION MEDIA FRONTAL PIPEWORK
SERVICE OPERATION BACKWASH OPERATION
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EQUIPMENT DESCRIPTION
FOR SOFTENER PRESSURE VESSEL INLET DISTRIBUTION SYSTEM BOTTM COLLECTION SYSTEM STRAINERS SOFTENING RESIN REGERATION SOLUTION TANK FRONTAL PIPEWORK
SERVICE OPERATION BACKWASH OPERATION REGENERATION OPERATION
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EQUIPMENT DESCRIPTIONFOR DM PLANTS
PRESSURE VESSEL INLET DISTRIBUTION SYSTEM BOTTM COLLECTION SYSTEM STRAINERS CATION & ANION RESIN REGERATION SOLUTION TANK FRONTAL PIPEWORK
SERVICE OPERATION BACKWASH OPERATION REGENERATION OPERATION
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DM REGENERATION SEQUENCE
1 TO REMOVE ACCUMULATED FOREIGN
MATERIALS AND RESIN DUST.
2 TO INJECT ACID OR ALKALI TO CONVERT RESIN
IN TO ACTIVATED FORM.
3 TO REMOVE EXCESS ACID / ALKALI FROM RESIN .
OBJECTIVES OF REGENERATION
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STEPS OF REGENERATION
1 BACKWASH.
2 REGENERATION INJECTION.
3 SLOW RINSE.
4 FAST RINSE
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BACKWASH
- RESIN IS FLUIDISED TO 40 TO 50 %BED EXPANSION.
- ACCUMULATED DIRT, RESIN FINESREMOVAL.
- RESIN BED IS HYDRAULICALLY
CLASSIFIED.
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REGENERATION INJECTION .
- ACID OR ALKALI IS USED SAC : HCL OR H 2 SO4
WBA : NaOH
SBA : NaOH- CONCENTRATION
WEAK RESINS : 0.5 % - 2.5%
STRONG RESINS : 3.0 % - 5%- TIME TO BE SUFFICIENT FOR
ADEQUATE CONTACT .
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REGENERATION LEVEL
- KGS OF 100% REGENERANTINJECTED FOR EVERY M 3 OF RESINS.
- IMPORTANT FOR ONLY STRONG
RESINS ( SAC & SBA)
- R/L RANGE IS 30-160 KG/M 3
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REGENERATION QUANTITY
- FOR STRONG RESINS.RESIN VOL. (M 3 ) X REGENERATION
LEVEL (KG/M 3 ).
- FOR WEAK RESINS.
WORK DONE BY RESIN.=
IONIC LOAD ( As CaCO 3) X OBR M3
1000 X 1.25 OR 1.37 ( TO CONCERT FROM CaCO3 TO EQUIVALENT)
X 115
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TYPES OF REGENERATION
SEQUENCES .
- CO-FLOW- COUNTER FLOW- DOWN FLOW, PACKED- UPFLOW , CONVENTIONAL
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FAST RINSE
- PURPOSE IS TO REMOVE EXCESS
REGENERANT FROM RESIN BED.
SERVICE INLET WATER IS USED.FAST RINSE IS CONTINUED
TILL DISIRED OUTLET QUALITY IS
OBTAINED
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CO FLOW REGENERATION.
REGENERANTINLET
SERVICEINLET
REGENERANTOUTLET.
SERVICEOUTLET
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COUTER REGENERATIONDOWN FLOW
REGENERANTINLET
SERVICEOUTLET
REGENERANTOUTLET.
SERVICEINLET
COFLOW REGENERATION
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COFLOW REGENERATION
- LEAKAGE OF IONS IS HIGH
- TREATED WATER QUALITY IS NOT CONSISTENT.
THROUGH OUT CYCLE.
- REQUIRES VERY LARGE QUANTITY OF REGENERANT
FOR QUALITY IMPROVEMENTS.
- REGENERATION EFFICIENCY IS LOWER ( 30-45%)
COUNTER REGENERATION
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COUNTER REGENERATION
( DOWNFLOW)- HAS ALL ADVANTAGES OF UPFLOW COUNTER
CURRENT REGENERATION.
- UP FLOW COUNTER CURRENT REGENERATION.
- BACKWASH IS NOT POSSIBLE BECAUSE OF LACK
OF FREE BOARD.
- FEED WATER TURBIDIY SHOULD BE LOW ( < 1 NTU )
COUNTER REGENERATION
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COUNTER REGENERATION
- LEAKAGE OF IONS IS LOW.
- TREATED WATER QUALITY IS CONSISTENT
THROUGHT THE RUN.
- REDUCED REGENERANT QUANTITY ALSO
PRODUCES IMPROVED QUALITY.
- REGENERATION EFFICIENCY IS HIGHER (80-90%)
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DV NT GES OF REVERSE OSMOSIS SYSTEM OVER
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DM
We would like to propose an RO based treatment scheme inplace of DM based system. We would like to highlight that theR.O. based treatment system shall be more beneficial in
terms of following parameters :
1. Very less operating cost. (Enclosed an annexure ontypical operating cost calculations for DM & RO)
2. Less chemical handling and storage.
3. Very less operational needs thus the manual Reverse
Osmosis Plant shall suffice in place of an automatic DMPlant.
4. Less civil work.
5. Less area requirements.
6. Reverse Osmosis system can take the marginalvariations in feed water quality without affecting thetreated water parameters.
7. No need for any neutralisation pit. The RO reject & MBregeneration effluents can be directly taken to guardpond.
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REVERSE OSMOSIS RO )
TOPICS :
- PRINCIPLES OF RO.
- PRETREATMENT FOR RO.
- OPERATION & MAINTAINANCE.
- TROUBLE SHOOTING.
- CASE STUDIES & DISCUSSIONS.
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PRINCIPLES OF RO
- RO BASICS.
- TYPICAL RO ARANGEMENT - OPERATING ARANGEMENT.
- DESIGN PARAMETERS. - SELECTION OF RO MODEL.
Reverse Osmosis
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Reverse Osmosis
P >
Reversing osmotic flow by applying a pressurein excess of the osmotic pressure
P
DILUTESOLUTION
CONCENTRATEDSOLUTION
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TYPICAL RO ARRANGEMENT.
PRETREATMENT RO POST TREAT
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Block Diagram of RO
(PERMEATE )
PRODUCTWATER
REJECTWATER
(CONCENTRATE)
HIGH
PRESSURHEPUMP
SALTWATER
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OPERATING PARAMETERS
FEED
PERMEATE7.5 M3/HR50 PPM
CONCENTRATE2.5 M3/HR
3850 PPM
RECOVERY = PERMEATE FLOW = 0.75 OR 75 %
FEED FLOW
10 M3/HR
1000 PPM
SALT PASSAGE = PERMEATE TDSFEED TDS
= 0.05 OR 5 %SALT REJECTION = 100 - SALT PASSAGE
= 95 %.
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OPERATING PARAMETERS
FEED PERMEATE 7.5m3/hr.OF 50 PPM AT 5 PSI
CONCENTRATE 2.5 M3/HROF 3850 PPM AT 215 PSI
RECOVERY = PERMEATE FLOW = 0.75 OR 75 %
FEED FLOW10 M3/HR
1000 PPM230 PSI
SALT PASSAGE = PERMEATE TDSFEED TDS
= 0.05 OR 5 %SALT REJECTION = 100 - SALT PASSAGE
= 95 %.
P = FEED PR - CONC. PR= 230 - 215 = 15 PSI
DESIGN PARAMETERS
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FLUX - GFD
- L/M 2H
GFD = 0.59 * L / M 2 H
GFD = 8-10 FOR WASTE WATER &
SEAWATER.
< 14 FOR SURFACE
< 18 FOR WELL WATER
< 25 FOR PERMEATE
DESIGN PARAMETERS
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BETA FACTOR = MAXIMUM
1.16 FOR LAST ELEMENT ATCONCENTRATE SIDE
T i l A li ti
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Typical ApplicationsOf
Reverse Osmosis
Industrial process water Production of potable water Food processing Waste treatment
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Membrane manufactures Dow Filmtec.,U.S.A. Fluid systems U.S.A.
Hydranautics U.S.A. Osmonics inc U.S.A. Trisep USA. Saehan KOREA
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CROSS SECTION OF THIN FILM
COMPOSITE MEMBRANE
SEMIPERMEABLEMEMBRANE
POROUSSUPPORT
BACKINGMATERIAL
THIN-FILM COMPOSITE MEMBRANES
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40 micrometer
120 micrometer
0.2 micrometerPolyamide
Polysulfone
UltrathinBarrier Layer
MicroporousPolysulfone
ReinforcingFabric
THIN FILM COMPOSITE MEMBRANES
Membrane Assembly
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Membrane Assembly
End cap
In board connec tor
Outer bord
connector
Feed tube
o rings
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Reverse OsmosisMembranes - Types
Cellulose Acetate
Thin Film Composite Polysulfones
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THIN FILM COMPOSITE
MEMBRANE CHARACTERISTICS Lower Operating Pressure
High Salt Rejection Available for Sea Water Stable to pH 11 Sensitive to Oxidants
Benefits of R O
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Benefits of R.O.High recovery rates.Predictable water quality--regardless ofTDS content.Simple operation and control.Limited chemical problems.No daily regeneration hassels.Can be skid mounted,hence less space.Very few components for maintenance.Less operator attention
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Source of Water
Surface water Lake or Pond
River Well Water
Shallow well
Deep Well Treated Effluent
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Silt Density Index - SDI
How to measure SDI Quanitifies particles of range 0.45 to 5
microns Dual media removes upto 50 microns. Multimedia with garnet removes down to
25 microns.
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Feed Water Analysis
Need to know the trend in the increase. Onsite pH. Appearance of water as drawn Organics. Biological activity of water.
RO System Design
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Temperature (Max, Min & Average) Chlorine Residual Turbidity Suspended solids Color. Silt Density Index pH colliform Count (bacteria) Total Plate Count Calcium Magnesium Pottashium Iron
y g
ManganeseBariumStrontiumChloriteSulfateNitrateAmmoniaPhosphateFluorideSilicaTotal Dissolved SolidsHydrogen SulfateCarbon Di Oxide
Parameters required for designing :
Note : Variation in these parameters should be noted and odours, traces of industrial pollutant,clay, sand, rust, or other unusual characteristics should be described.
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Reverse Osmosis
System Design
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MEMBRANE SELECTION
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MEMBRANE SELECTIONBASIS
Application or end use Quality Desired Water Temperature
4-2-1 Array
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y
Feed
2000mg/L173 gpm
89 mg/L98 gpm
239 mg/L42 gpm
638 mg/L16 gpm
Concentrate18,211
mg/L17 gpm
8231 HR, 90%
Recovery
Permeate187 mg/L156 gpm
1st Bank
2nd Bank 3rd Bank
RO S
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RO System components
The basic expanded design of a single systemincludes the following:
Raw water feed pump to supply water to the pretreatment
Pre treatment system for Turbidity,TSS,Colloidalparticles & Organic matter.
Cartridge filter to remove micron size particle tocontrol the SDI( Silt density index) of feed water
Anti scalant dosing system. High pressure pump&feed control valve to pressurize
the feed water. Membranes housed in Pressure tubes. -----continued.,
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A reject control valve to control the recovery of the ROsystem.Askid to mount to all mechanical equipment .Flow indicators to measure permeate and rejectflowrates.Pressure gauges for monitoring the differentialpressures across the RO feed, reject and intermediatestages.Conductivity & pH meter for measuring the quality ofthe permeate water.And other necessary instruments for monitoring easyoperation and critical parameters.A cleaning system consisting of Tank,CF,Pump andnecessary instruments.
PRETREATMENT FOR
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PRETREATMENT FORRO PLANT
CHLORINATION.
USE OF SODIUM HIPO CHLORITE.
- TO GET MAXIMUM FRC 0.5 PPM AT THE POINT OF
BISULPHITE DOSING.- EFFECTIVE REACTION TIME 20 - 30 MIN.
PRETREATMENT FOR
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PRETREATMENT FORRO PLANT
DE - CHLORINATION
- TOLERANCE < 1 PPM MAX
- ACITIVATED CARBON FILTER.
- BISULPHITE DOSING WITH ORP METER.
- 1 PPM OF F.R.C REQUIRES 1.46 PPM OF NaHSO3
.
PRETREATMENT FOR
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PRETREATMENT FORRO PLANT
pH
- ACID DOSING / ANTISCALENT CHEMICALS.
- HCL / MAXTREAT CHEMICALS. - AS PER PROJECTION.
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PRETREATMENT FOR RO PLANT
OIL & GREASE & COD / BOD
REQUIREMENT - NIL
- IF IT IS PRESENT- REF : MATTER TO H.O. PEG.
IRON & Mn - LESS THAN 0.1
PRETREATMENT FOR
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PRETREATMENT FORRO PLANT
REMOVAL METHODS FOR Fe (Iron)
1. BY MnO 2 FILTER UP TO 1 PPM.
2. OXIDATION BY AIR, FOLLOWED BY FILTERATION -MORE THAN 3 PPM
3. OXIDATION BY CHLORINATION - UP TO 2 PPM.
Reverse osmosis systemCleaning tank
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Pretreatment
RO hydrablock
Cleaningsystem
Clarification
Coagulation
Filteration
De-chlorination
Dosing system
Cartridge filter
Membrances
Pressure tubes
HP pumps
Control pannel
Cleaning tank
Pump (SS)
Cartridge filter
DM plant
pH adjustment
Degassification
Posttreanment
Schematic diagram of RO unit for brackish water
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Lime or lime - sodacoagulant aids
coagulation andsedimentation
Sandfilter
Activatedcarbon filter
Mn greensandfilter
S.H.M.P. Acid
High pressurepump
DESALATION SECTIONMembrane modulesProduct
water
Wastebrine
Polishingfilter
Operating Parameters
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p g
.Feed PressureConcentrationpHTemperature
Permeate ConcentrationFlowPressure
Concentrate FlowPressureConcentration
S P fil
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System Profile The System Profile is a measurement of the
permeate concentration from each individualvessel.
Identifies which vessels in an array have highsalt passage. A System Profile should be taken at startup,
as a baseline record. Record complete system data whenever a
System Profile is performed.
PROBING
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Probing is done while the system isoperating at normal conditions.
Insertion is normally done from the endopposite the permeate collectionmanifold.
PROBING
PROBING
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Conc.
Feed
Permeate
CONDUCTIVITY
PROBING
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CHANGE IN PRESSURE
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CHANGE IN PRESSUREDROP
HIGHER
BIOFOULING SCALING INORGANIC FOULING HIGHER FLOWRATES LOWER FEED TEMPERATURES
LOWER
LOWER FLOWRATES
HIGHER FEED TEMPERATURES
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CHANGE IN FEED PRESSURE
HIGHER SCALING PLUGGAGE FOULING HIGHER FEED TDS LOWER FEED
TEMPERATURE IMPROVER VALVING
LOWER HIGHER FEED
TEMPERATURE LOWER FEED TDS MEMBRANE
DAMAGE
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CHANGE IN FEED CHEMISTRY
pH TOO HIGH = MEMBRANE DAMAGE
Ph TOO LOW = MEMBRANE DAMAGE
CHLORINE ABOVE = MEMBRANEVENDORS SPEC DAMAGE
SCALING IONS ABOVE SPEC = SCALING
INCREASED SDI OR TURNIDITY = FOULING
TROUBLESHOOTING OF RO
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Too high system recovery : Concentration Polarization
Localized Salt Concentration
Causes :Operator errorFlow meter out of calibrationUnnoticed change in Feed water composition
SYSTEM
Troubleshooting of RO System
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Common causes for high pH Buildup of bacteria
g y
RO element manufacturing problem Elements moved from their original
marked position .
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Troubleshooting of RO System
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Severe membrane deterioration ormultiple problems:
Troubleshooting of RO System
TIMELY CORRECTIVE ACTION
Instrumentation
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pH
Conductivity Rota meter. Pressure gauges. ORP
Thermometer Level switches Flow switches Pressure switches Electrical control
Instruments used in an RO system
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130
R. O. PLANT LOGSHEET FORMAT (TYPICAL)DATE-
O/P R. W. AREA SMBS D. P. ANTI.D. P.
HRS.NaOCl D. P. I/L FLOW I/L PR. O/L PR. O/L FRC ON/OFF ON/OFF O/L PR. O/L SDI O/L FRC ORP READING FEED PR. REJ. PR. PERMEATE FLOW REJ. FLOW PERMEATEON/OFF (LPM) (KG/CM2) (KG/CM2) (PPM) (KG/CM2) (PPM) (KG/CM2) (KG/CM2) (LPM) (LPM) (Microsieme
SIGN. OF OPERATOR SIGN. SUPERVISOR
G.F./D.M.F. C. F. R. O. BLOCK AREA
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D. M PLANT LOGSHEET FORMAT (TYPICAL)DATE -
O/PHRS. ALUM D.P. NaOCL D.PI/L FLOW I/L PR. O/L PR. I/L PR. O/L PR. O/L FRC I/L PR. O/L PR. I/L PR. O/L PR. O/LCOND. O/L Ph
ON/OFF ON/OFF (M3/HR) (KG/CM 2) (KG/CM2) (KG/CM 2) (KG/CM 2) (PPM) (KG/CM2) (KG/CM 2) (KG/CM 2) (KG/CM 2)(m/cm2)
SIGN. OPERATOR SIGN. OF SUPERVISOR
SBAR.W. AREA DMF ACF SAC
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AL KAL I BOI L OUT PROCEDURE
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4. Determine the quantity of water added to the boiler and add a sufficient quantity ofMelrose Chemicals, Ltd A-420 or F-685 for the treatment in progress. Refer to theTechnical Bulletin of the product used to know its solubility. When the necessaryquantity of A-420 or F-685 is added, alkalinity "M" will be 3000 to 4000 ppm.5. A concentrated solution of the cleaner can be added proportionally to the feed waterwhile filling of the boiler. If there is an economiser in the system, the concentratedsolution must be added to there directly. In the case of small boilers or when the
conditions allow it, the concentrated solution can be added through a manhole or anyother opening located at the top of the boiler. Do not add solids to a boiler. The use of A-420 liquid for an alkaline boil-out eliminates any problem from deposits incurred bythe use of solid chemicals.6. Read and follow closely the instructions of the manufacturer of the boiler concerningthe firing stages and the evacuation of the vapours during an alkaline boil-out.7. In the case of new boilers, the drying of refractory materials can be combined withthe alkaline boil-out. Light a fire with wood to dry the boiler lining. Leave the chimneyopen until vapour appears - then close. If wood cannot be used, use oil. In installationswhere the oil is pulverized, it is often necessary to use a more easily controllable fuel.
The temperature of the furnace during the preliminarystages of boil-out must be low -
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in order to obtain uniform drying - then can be graduallyincreased by varying the rate offuel addition or firing period to maintain the minimumpressure necessary during theboil-out. The suggested maximum pressure isapproximately 50% of the limit of
pressure for the valve operating with the lowestpressure. This pressure will createsufficient circulation in boilers having a waterwall and anetwork of complicated internal
piping.
8. It is difficult to precisely determine the optimal duration of analkaline boiling.Experience shows that 1 to 3 days are generally necessary for the
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internal cleaning of aboiler. One prolonged period is better if drying of refractorymaterials is also carried out.The state and the appearance of the blowdown water of the boilerare the bestindication in knowing if the treatment should be continued or
stopped.9. For the duration of the boiling, all the safety measures must beobserved with regardto the superheaters, the economisers, etc. in order to avoid any
damage with theequipment. The superheaters and the economisers should beoperated in the sameway as when the system is operating. Detailed attention should begiven to the
at least every 8 hours. The total quantity of water removed from allthese points shouldbe roughly a quarter of the level indicated on the gauge, this
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quantity being also dividedbetween the various drains and the continuous blowdown. Firstdrain the continuousblowdown, then progressing toward the drains on lower level ofthe boiler. Following thisoperation, the water level in the boiler should be restored by using
water containing thealkaline cleaner, so that the concentration of the cleaner in theboiler is not reduced bythese regular purges.
11 At the end of the boiling, cool the boiler gradually, then drainand flush the system byi d hi h Ch k h l li f h