membarane technic in ro
TRANSCRIPT
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Environmental Challenges: OverviewFacing Industry
Dr. Pedro Medellín Milán
Universidad Autónoma d
eSan Luis Potosí
Dr. Mahmoud M. El-Halwagi
e!as A"M Universit#
Monserrat $haire% Llamas
(Part III)
Pro&ess 'ntegration (or Environmental $ontrol in Engineering &urri&ula
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Let’s consider a typicalre ning industry with anaverage !""#""" $$l%day
capacity as the one presentedin gure ! on the ne&t slide'
In this process# the largestsource o pollutants such asphenol# ammonia and sul deresults rom the catalyticcrac ing unit' Considera$leamounts o thesecomponents and# high levelso *O+ and CO+ are oundedin the oily sour water coming
out o the ractionators in thedistillation units'
P+, LEMS A EME
PA+AME E+ /AS E 0UA ' 'ES A DL,ADS )l1s2da#*
,ater !- -./ -""
*O+ 0 !1 """
CO+ /. """
2uspended 2olids / .""
Phenols .""
2ul de 1 -""
34 / 53 ! 6""
Oil 0 /""
7he wastewater produced in thosesections o the process are loaded toa primary treatment unit (8PI
separator)# and the resulting streamshows the ollowing characteristicsgiven 7a$le/'!:
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A t m o s p
h e r i c
d i s t i l l a t i o n
Vacuumdistillation
Coking
CatalyticCracking
Hydrocracking
HydrogenProduction A
m i n e
Desulfurization
Treating
Desulfurization CatalyticReforming
AlkylationGas plant
Amineplant
B l e n
d i n g
Treating
Gasoline
Jet Fuel
Kerosene
Heating oil
Gas
Naphtha
Lubricating oil
Grease
Wax
Coke
Industrial Fuel
Asphalt
NaphthaGas
Fuel Gas
ButaneGasoline
Naphtha
L G ! Light
gases
NaphthaGas
NH "
H#$
H#
NH "
H#$
H#$
C% #
&iddle 'istillates
NH "
H#$
Gas %ilsNH "( H#$
NH "
H#$
C% #H#
H#
HCNH#$
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7he primary e9uent is then carried to secondary treatment#where the levels o *O+ 0# CO+# oil and suspended solids arediminished and can $e neglected or this open ended pro$lem'enerally# sul ur compounds are di;cult to remove# hence wewill not deal with sul de treatment and only consider thecomposition o secondary e9uent as shown in 7a$le /'1:
$om3ound 4low )l12hr* Mass4ra&tion
,ater -<0 !0" "'<<<.-.1
34 / 53 0.'// "'""""./<
Phenol //'// "'""""6=<
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7he re nery has to ul ll the e9uent limitation guidelinesdictated $y the Code o Federal >egulations (6" CF> 6!<'11)#stated $elow:
*O+ 0
722
CO+
Oil and grease
Phenolic compounds
8mmonia as 3
2ul de
7otal chromium
4e&avalent chromium
p4
1.'1 !<'0
1!"'"
.'6
"'1!
!.'.
"'!.
"'6/
"'"/0
(?1?)
!0'-
!1'-
!"<
6'0
"'!"
.'0"'".1
"'10
"'"!-
(?1?)
Ma!imum (or an# 5da#
Average o( dail#Ma!imum values (or67 &onse&utive da#s
shall not e!&eed
Pollutant or3ollutant 3ro3ert#
Metric units (kilograms per 1,000 m 3 offeedstock)
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In order to reach the CF> re@uirements# the secondary e9uentwill $e carried to the tertiary treatment and the consideredoptions or this are:
7o diminish the content o phenol and ammonia $y SteamStri33ing
7o remove phenol $y +everse ,smosis
For the last case we will suppose that there is no ammonia in thestream# so that the only pollutant to $e removed is phenol:
$om3ound 4low )l12hr* Mass 4ra&tion
,ater -<0 !0" "'<<<<01!
Phenol //'// "'""""6=<
7O78L -<0 !./'// !
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0UES ', S8 Is the level o separation achieved with each o these tertiary
treatment methods good enough to satis y the limits imposed in theCF>A
Could the target concentration $e reached $y modi ying someoperating conditionsA I so# how would these modi cations aBect thecostsA
8ccording to the nal separation and the cost analysis# which isthe most suita$le technologyA
,hich method would you recommend or secondary wastewatertreatment ta ing into account *O+ 0# CO+# suspended solids and oilamounts i secondary e9uent have to $e low enough to meet theCF> regulationsA
Is any o the two proposed tertiary methods convenient oradditional removal o *O+# CO+# suspended solids or oilA
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For the >everse Osmosis calculation the ollowing data is
re@uired:
Fi$er length# l: "'=0" mFi$er seal length# l s: "'"=0 mOuter radius o $er# r o: 61 & !" 5- mInner radius o $er# r i: 1! & !" 5- mem$rane area# 2 m : !." m 1
EO E7>IC8L +878
I3PD7 +878
a&imum ow rate per module: "'6-" g%s
inimum ow rate per module: "'1!" g%sa&imum eed pressure: 10'0. & !" 0
Pressure drop per module: "'6"0 & !" 0
Pure water permea$ility# 8: !'1" & !" 5!"
2olute transport parameter: 1'6/ & !" 56
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Industrial ,astes 7he characteristics o industrial wastewaters# their composition# ow and volume diBer considera$lyamong industries depending on the speci c process carried on'
8s seen in section 1'/# wastewater rompetrochemical and petroleum re ning industrycontains ha ardous chemicals as hydrocar$ons#phenols# ammoniacal nitrogen# hydrogen sul de#sul uric acid# etc'
7hus# the environmental impact o thesewastewaters depend# $esides their collectivecharacteristics such as $iochemical o&ygen demand(*O+)# chemical o&ygen demand (CO+) andsuspended solids (22)# on their content o speci cinorganic and organic compounds' 7his su$stanceswill dictate the most suita$le treatment method'
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EP8Gs program to control wastes is$ased on the ollowing hierarchy:
8voidance>e5use
>e5cycling>ecovery o energy
7reatment
Containment+isposal 7he treating o wastewaters canta e place at diBerent points in theprocess'
Options for controlling industrial wastewaters
,astewater can $e:
H Pretreated or discharge tomunicipal treatment sources'
H 7reated completely at the plantand reused or discharged directlyinto receiving waters'
H 7reated at the point o generation'
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Classification of Wastewater Treatment Methods
iologi&al nitrogenremoval
ioaugmentation
A&tivated sludge
E!tended aerationAnaero1i& 3ro&esses
+otating 1iologi&al&onta&tors
Se9uen&ing 1at&hrea&tors and tri&:ling
;lters
$ar1on adsor3tion
Distillation
4iltration
Steam Stri33ing
,il and greases:imming
,il2water se3aration
Sedimentation
Mem1ranete&hnologies
$hemi&al ,!idation
$hemi&alPre&i3itation
$oagulation
Dissolved air <otation
Ele&tro&hemi&alo!idation
4lo&&ulation
H#drol#sis
eutrali%ation
Solvent E!tra&tion
'on E!&hange
C4E IC8L P4 2IC8L *IOLO IC8
L
!D"#TR A$ %A#T&%AT&R TR&AT'&!T '&TH(D#
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Classification of Wastewater Treatment Methods
iologi&al nitrogenremoval
ioaugmentation
A&tivated sludge
E!tended aerationAnaero1i& 3ro&esses
+otating 1iologi&al&onta&tors
Se9uen&ing 1at&hrea&tors and tri&:ling
;lters
$ar1on adsor3tion
Distillation
4iltration
Steam Stri33ing
,il and greases:imming
,il2water se3aration
Sedimentation
Mem1ranete&hnologies
$hemi&al ,!idation
$hemi&alPre&i3itation
$oagulation
Dissolved air <otation
Ele&tro&hemi&alo!idation
4lo&&ulation
H#drol#sis
eutrali%ation
Solvent E!tra&tion
'on E!&hange
C4E IC8L P4 2IC8L *IOLO IC8
L
!D"#TR A$ %A#T&%AT&R TR&AT'&!T '&TH(D#
Physical%Chemical processes i
chemical agentsas coagulating
agents areadded'
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Con)entional*reat+ent
High,-ualit.*reat+ent
Waste/atertreat+entprocess
It’s a com$inationo physical#
chemical# and$iologicalprocesses
P+EL'M' A+=+EA ME
P+'MA+=+EA ME
SE$, DA+=+EA ME
AD>A $ED+EA ME
4eedwastewater
stream
o dis&harge
orreuse2re&#&ling
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>emoval o grit# de$ris ande&cessive amounts o oils or
greases'
%aste)ater pretreatment plant*
Waste/atertreat+entprocess
It’s a com$inationo physical#
chemical# and$iologicalprocesses
P+EL'M' A+=+EA ME
P+'MA+=+EA ME
SE$, DA+=+EA ME
AD>A $ED+EA ME
4eedwastewater
stream
o dis&harge
orreuse2re&#&ling
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Waste/atertreat+entprocess
It’s a com$inationo physical#
chemical# and$iologicalprocesses
P+EL'M' A+=+EA ME
P+'MA+=+EA ME
SE$, DA+=+EA ME
AD>A $ED+EA ME
4eedwastewater
stream
o dis&harge
orreuse2re&#&ling
>emoves near to 0"5="J o22# 1050"J o *O+ 0 and -0J
o oil and grease'
$lari;er
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Waste/atertreat+entprocess
It’s a com$inationo physical#
chemical# and$iologicalprocesses
P+EL'M' A+=+EA ME
P+'MA+=+EA ME
SE$, DA+=+EA ME
AD>A $ED+EA ME
4eedwastewater
stream
o dis&harge
orreuse2re&#&ling
7he reached removal is up to.05<0J o *O+ and 22 and
-0J o CO+'
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Waste/atertreat+entprocess
It’s a com$inationo physical#
chemical# and$iologicalprocesses
P+EL'M' A+=+EA ME
P+'MA+=+EA ME
SE$, DA+=+EA ME
AD>A $ED+EA ME
4eedwastewater
stream
o dis&harge
orreuse2re&#&ling
>emoval o :H8dditional organic andsuspended solids'H3itrogenous O&ygen +emand(3O+)H3utrientsH 7o&ic materials
Mem1ranese3aration
8lso called? ertiar#reatment
@
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P+EL'M' A+=+EA ME
Objective: 7o separate su$stances which can causepro$lems to puri cation plant e@uipment' 4eavyinorganic solids such as sand# gravel# metal orglass are removed' 7he collected de$ris is usuallydisposed oB in a land ll'
Used processes: ainly sedimentation andltration'
Used e uipment : *ar screens# comminutors andgrit cham$ers' enerally the wastewater enters a$ar screen rst to remove large si e solids andthen passes to a grit cham$er'
Grit Chamber
P+'MA+= +EA ME
Objective: >emoval o organic and inorganic suspendedsolids# oils and greases' 8lso removed are some organicphosphorus# organic nitrogen# and heavy metals associatedwith solids' Colloidal and dissolved constituents are notaBected'
Used processes: 2edimentation# otation and oil%waterseparation'
Used e uipment : Clari ers and settling tan s or suspendedsolids removal and 8PI separators or oil%water and solid
Clarifier at the 'ain %aste)aterTreatment Plant in (akland
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2uspended lm systems: icroorganisms are suspended in wastewater and once theya$sor$ nutrients# reproduce and then are settled out as a sludge' 8 portion o the sludge ispumped $ac into the incoming wastewater as Kseed microorganisms while the other part issent to sludge treatment' E&les o such systems are e&tended aeration# activated sludge#se@uential $atch reactor systems and o&idation ditch'
Used processes: 7hree approaches are used to accomplishsecondary treatment Fi&ed lm systems: icroorganisms grow on su$strates (roc s#
plastic# sand) over which the wastewater is spread over' 7he lm omicroorganisms grows and thic ens while the nutrients area$sor$ed' 2ome e&les are rotating $iological contactors (>*C)#tric ling lters and sand lters'
SE$, DA+=
+EA MEObjective: +ecomposition o dissolved organic matter $y means o using $iologicallyactive sludge' Consist o the $iological treatment o the e9uent rom primary treatmentto remove the residual organics# suspended# colloidal and dissolved solids'
Lagoon systems: 8re shallow ponds designed to hold wastewater orseveral months while is treated through a com$ination o physical# $iologicaland chemical processes' 2ome aeration devices can $e added to rise thesystem e;ciency' 7he most common types o lagoons are:
8naero$ic lagoons 3aturally aero$ic lagoons 8erated lagoons
Treatment process )ith a RBChttp+,,)))*oleau*fr,
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!e"nition: 8ny process applied a ter secondary treatment designed to produce ane9uent o higher @uality to protect the receiving waters or to provide reusa$le wateror its urther domestic and%or industrial recycling (cooling water supplies)' 7histechnology encompasses all unit operations not commonly ound in the typicalwastewater treatment'
#lassi"cation of advanced $aste$ater treatment process:
AD>A $ED /AS E/A E+ +EA ME
%&'% '* %'& M&+%
#OM +&!O-O. # -/ *2 # -/# &M # -
%'& %M&+%
*2 #O# &M # - %'& %M&+%
By the type ofprocess flo)
scheme utilized
K7reatment processin which unit
operations areadded to theconventional
secondarytreatment'
K7reatment processin which $iological
and physical5chemical processes
are intermi&ed toachieve the desired
e9uent'
Com$ination o$iological and
physicochemicaltreatments'
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H0$IC%CH1&ICAL2%C1$$
BI%L%GICAL2%C1$$
not er $a4 to classif4 advanced $aste$ater treatment is to di5erentiate according tot e desired treatment goals6 2ome e7amples are presented ne7t6
AD>A $ED /AS E/A E+ +EA ME
'
+,
E
+EM,>AL
Al:aline air stri33ing
'on e!&hange : ,astewateris passed through a porous$ed o organic resin wherecationic and anionic ione&changers react with cationsand anions# respectively# orremoval or recovery'
rea:3oint &hlorination
Consist o two phases:3itri cation or rst phase: Occurs in an aero$icenvironment and a than similar to that or the activesludge is used to o&idi e the ammonia to nitrate'2econd phase: Occurs in an ano&ic (without K ree o&ygen#i'e'# O 1) environment where the nitrates are denitri ed tomolecular nitrogen $y means o diBerent genus o $acteriausing the nitrates as o&idi ing compound in place oo&ygen'
///3+ech,che+3co+4 about4/.+an3ht+l
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CH1&ICAL2%C1$$
BI%L%GICAL2%C1$$
AD>A $ED /AS E/A E+ +EA ME
PH,SPH,+US
+E
M,>AL
# &hemi&al 3re&i3itationusing multivalent metalions as iron salts oraluminum &om3ounds su&has (erri& &hloride or alum)aluminum sul(ate*
Phos3horus removal is done 1# en&ouraging PA,Bs)3hos3horus a&&umulating organisms* to grow and&onsume 3hos3horus 1# using an anaero1i& tan:3la&ed ahead o( an a&tivated sludge aeration tan:.
Alum treatment at #-ui.. $ake/ $a)rence0ille/ !1 http544///3alliedbiological3co+4treat+ent63ht+l
Anaero.icreactor
Aero.icreactor
Clarifier
#econdaryeffluent
P cleaneffluent
,aste activatedsludge with Prich $acteria
8s these methods convertdissolved phosphorus into
particulate orm it is common touse sand lters as nal stage'
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AD>A $ED /AS E/A E+ +EA ME
,
HE+
+E
ME
ME
H,DS
Adsor3tion with a&tivated &ar1on. It is appliedas advanced treatment or the removal o non5$iodegrada$le dissolved organics or as a secondarytreatment replacing conventional $iological treatment'2ome molecules as methanol# ormic acid# and sugars
are not remova$le $y t his method'
Polishing 3onds. Dsed to o$tainadditional suspendedsolids removal'
7reatment can $eaero$ic or acultative(a com$ination oaero$ic and anaero$ic$iological activity)'
Mi&rostraining ' ethod used or removalo additional suspended solids andassociated $iochemical o&ygen demand' 7heprocess involves the passing o an e9uentthrough a hori ontal rotating drum with altering a$ric &ed $y a porous screen'
Post-aeration ' ethod used tomaintain certain dissolved o&ygenlevel' 7his is accomplished $y
mechanical aeration# diBusedaeration or cascade aeration'
4iltration. Dsed or additional elimination o suspended solids and $iochemical o&ygendemand' 7hese processes include sand ltration# constructed wetlands and mem$raneltration'
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7he most common e&les used in wastewater treatments are presented in the
ne&t ta$le:
http544nett#63gec37p4CC*8'A*A4WA*124IN*2%'9C*I%N4ht+l4Water,::63ht+l
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asinAeration
1asin$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
*his e;;luent is thentreated in a central
;acilit. called <end,o;pipe< treat+ent as it isnor+all. i+ple+entedas the last stage o; theprocess be;ore the
It is co++on in +ost re;ineriesto collect all process
/aste/aters and to co+binethe+ into a single /aste/ater3
strea+ is disposedo; or deli)ered3 *he
end,o;,pipe
treat+enttechnolog.
includes biologicaland che+ical
s.ste+s3
8dapted rom K8n IntegratedE&pert 2ystem orOperating a Petroleum>e nery
8ctivated 2ludge Process,ei$o uan# ichael M'
2tenstrom # 3aci 4' O gur#
+avid O rent
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asinAeration
1asin$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
The American Petroleum nstitute 2AP 3 separator is a long rectangular tank that
operates on the principle o; strokes la/ /hichde;ines the rise )elocit. o; an oil particle based
on its densit. and si=e3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asinAeration
1asin$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
2elati)el. ine;;icient
2e-uires largea+ount o; space
Accept a /ide)ariet. and proportions
o; oil and solidsincluding )iscous( stick.
or /ax. oil3http544///3+onroeen)iron+ental3co+4api8clari;iers3ht+
AP #eparator
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
E9uali%atio
n 1asinAeration
1asin$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
*he Dissol0ed Air4lotation 2DA43 unitconsist o; t/o sections
First( in the > flocculatorcha+ber? the in;luent is
+ixed /ith coagulantde+ulsi;iers that cause the
agglo+eration o; oildroplets and solids3
*hen the oil./aste ;lo/s into
the flotationsection ( in /hichrising air bubblesadhere to these
particles causingthe+ to rise3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
Finall.( in thesur;ace the scu+is re+o)ed b. aski++er and the
settled sludge;ro+ the botto+ is
displaced b.gra)it. orpu+ping3
http544///3h.dro;lotech3co+4site8+ap3ht+
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
&-ualization Basin *hese are tanks or lined ponds3 According to the
'epart+ent o; 1n)iron+ent ! Natural 2esourceso; $outh 'akota( e-uali=ation basins ha)e t/oob7ecti)es5
///3ba.cod/s3org48about4process3ht+l
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
>*he secondar. ob7ecti)e isto da+pen the strength o;
/aste/ater constituents b.blending the /aste/ater in
the e-uali=ation basin to+aintain a degree o;
reliabilit. and operationalcontrol?3
Genesee County ARTP&-ualization Basin
*he pri+ar. ob7ecti)e is toda+pen the )ariationscaused b. in;lo/4in;iltration and the diurnal ;lo/)ariation( to achie)e anearl. constant ;lo/ ratethrough the do/nstrea+treat+ent processes3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
*he Acti0ated #ludge Process is one o; the +ost
co++on secondar. treat+ent processes3 *his processuses $aproph.tic bacteria to re+o)e suspended solidsand dissol)ed B%'3
According to Acti)ated $ludge( &anual o; ractice @Water 1n)iron+ent Association( 6 DE( the acti)ated,
sludge process contains ;i)e essential interrelatede-uip+ent co+ponents3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
63 An aeration tank in /hich air or ox.gen is
introduced into the s.ste+ to create an aerobicen)iron+ent3 At least se)en +odi;ications in theshape and nu+ber o; tanks exist to produce)ariations in the pattern o; ;lo/3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
#3 An aeration source that can be pro)ided b.
pure ox.gen( co+pressed air or +echanicalaeration3
Pi&ture o( adi user usedto su33l# theair needed (orthemi&roorganisms.
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
"3 Clari;iers3 Acti)ated sludge,solidsare separated ;ro+ thesurrounding /aste/ater b.;locculation and gra)it.sedi+entation3 *hen a thickenedsludge ;locs and ter+ed returnacti)ated sludge or 2A$E is;ounded in the botto+s /hile inthe upper portion o; the clari;ierthe /aste/ater /ith lo/ le)el o;acti)ated,sludge solids insuspension is ;or+ed3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
ECuen
t
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
Activated SludgeProcess
3 *he return acti)ated sludge 2A$E;ro+ the secondar. clari;iers ispu+ped back to the aeration tank toensure the replenishing o; the+icroorganis+s3
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#3i&al Petroleum
+e;ner# ECuentreatment Plant
AP'
Se3arator
4eed
an:s
DissolvedAir
4lotation
E9uali%atio
n 1asin
Activated SludgeProcess
Aeration
1asin
$lari;e
r
+aw
4eed
Sludge+e&#&le
Sludge/astag
e
3 Finall.( acti)ated sludge containing an
o)erabundance o; +icroorganis+s +ust bere+o)ed( or /asted /aste acti)ated sludge(or WA$E( ;ro+ the s.ste+3
ECuen
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Membrane Separation Techniques em$rane separation ( 2) techni@ues
have e&perienced high growth in recentyears and are widely $eing applied in theindustry today as they are intended to
ul ll the ollowing necessities:'e+and ;or higher -ualit. productsIncreased regulator. pressures*he rising interest in preser)ing naturalresources1n)iron+ental and econo+ic sustainabilit.3
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Among its many strengths, some of the reasons for the increased applicabilityof membrane separation processes are:
Appreciable energ. sa)ings5 Lo/ energ. consu+ption becausethese s.ste+s operate near roo+ te+perature3Clean technolog. /ith operational ease3Co+pact and +odular design using less space than cu+berso+etraditional +ethodsE3roduce high,-ualit. products due to the high selecti)it. o; the+e+branes3
Allo/ the reco)er. o; salable b.,products ;ro+ /aste strea+s(/hich increases their pro;itabilit.3Greater ;lexibilit. in designing s.ste+s31as. incorporation to presentl. existing industrial plants3
ncreasing applicability
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Membrane separation techniquesH 7he $asic o$Nective o mem$rane separation processes is the selective permeation o one or
more species through a mem$rane# there$y achieving separation'
H 8ccording to IDP8C# a mem1rane is a Kstructure# having lateral dimensions much greaterthan its thic ness# through which mass trans er may occur under a variety o driving orces '
H 2ince mem$ranes avoid the ow o li@uid# the transport through the mem$rane is $y:2orption: It re ers either to adsorption or a$sorption o the particles in the mem$rane'+iBusion: 7he movement o particles rom areas o high concentration to areas o lowconcentration' For diBusion to occur# the mem$rane must $e permea$le to molecules
H 7he 3ermea1ilit# descri$es the rate o transport o particles through mem$ranes'
$che+atic representation o; a +e+brane separation unit3
4eed
u+p
Retentate
'em.rane
Permeate
A&M
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by-product
Final Product
residueFeed stream 1
Feed stream 2
"p5stream processsection
n5course processsection
Do)n5stream processsection
PR(C&##
Fluid preparation Fluid regeneration( production uri;ication( production reco)er.(e;;luent re)alori=ation
B y-product for sale
K em$rane separation techni@ues can$e applied in diBerent sections o theprocess '
! Membrane Separation "rocesses can differ from one another in the type and configuration ofthe membrane, the mechanism of trans#membrane transport for $arious water solutioncomponents and, the nature of the process dri$ing force%
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(* Mem1rane 3a&:ing densit#8 It de nes the eBective mem$ranearea installed per volume o a module and is the main indicator orthe degree o pretreatment necessary or the diBerent modules inorder to achieve a sa e and trou$le5 ree long term operation'
,here C is the molar concentration o the solute# > is theuniversal gas constant and 7 is the a$solute temperature'
CRT =π
In the case o dilute solutions#
osmotic pressure can $e predictedwith
an’t 4oB’s e@uation:
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em$ranes*he +axi+u+ separation reached in +e+brane processes depends on theper+eabilit. o; the +e+brane ;or the ;eed solution co+ponents3
A permea.le mem.rane allo/s the passage o; all dissol)ed substances and thesol)ent3
A semipermea.le mem.rane is capable o; transporting di;;erent +olecular speciesat di;;erent rates under identical conditions3 *he ideal se+iper+eable +e+brane in+e+brane processes is per+eable to the sol)ent onl. but i+per+eable to allsolutes3&e+brane separation processes depend strongl. on the che+ical nature o; the+e+brane +aterials and the ph.sical structure o; the +e+branes3
*he ;ollo/ing are so+e desirable characteristics o;+e+branes5
Good per+eabilit.High selecti)it.&echanical stabilit.*e+perature stabilit.
Abilit. to /ithstand large pressure di;;erences across+e+brane thickness
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MEM +A E$LASS'4'$A ',
%2IGIN
&A*12IAL
&%2 H%L%G04$*29C*921
MEM +A E
$.nthetic *iological
$olidLi-uid
%rganic Inorganic
Non,porous orous
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MEM +A E$LASS'4'$A ',
%2IGIN
&A*12IAL
&%2 H%L%G04$*29C*921
MEM +A E
$.nthetic *iological
$olidLi-uid
%rganic Inorganic
Non,porous orous
!iscriminationaccording to
c emical a8nities
bet$een componentsand membranematerials6
!iscriminationaccording to si9e of
particles or molecules6% e mec anism on$ ic separation isbased is sieving or
"ltrating6 gradient in
4draulic pressure actsas t e driving force6
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MEM +A E$LASS'4'$A ',
%2IGIN
&A*12IAL
&%2 H%L%G04$*29C*921
MEM +A E
$.nthetic *iological
$olidLi-uid
%rganic Inorganic
Non,porous orous
Mass transport t roug t ese membranes isdescribed b4 t e solution/di5usion model; asfollo$s:
•2orption of a component out of t e feedmi7ture and solution in t e membrane material6
•%ransport t roug t e membrane along a potential gradient6
•!esorption on t e second side of t emembrane6
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MEM +A E$LASS'4'$A ',
S=MME +'$)H,M, E ,US
*
#onstructed b4 a single material and becauseof t is reason, t e membrane is uniform indensit4 and pore structure t roug out t e
cross/section6
AS=MME +'$
May be either homogeneous orheterogeneous and are characterized by adensity change givenby the membrane material across the cross
sectional area.
$,MP,S' E)HE E+, E ,U
S*
#onstituted b4 di5erent ( eterogeneous)materials, t e membranes ave a t in, densela4er t at serves as t e "ltration barrier6 ut,unlike skinned membranes,
is made of di5erent material t an t e poroussubstructure onto $ ic it is cast6
Skinned type: consist o a dense
s inned layer used as primary ltration$arrier and# a thic and more porousunderstructure that serves as supportstructure'
Graded density type : the porousstructure gradually decreases in
density rom the eed to the ltrateside o the mem$rane'
According tothe PhysicalStructure
(“trans-wallsymmetry”)
7his @ualitydescri$es the level
o uni ormitythroughout the
cross5section o themem$rane'
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MEM +A E PE+4,+MA $E A D
MA' E A $E 7he per ormance o a mem$rane depends on:
7he characteristics o the mem$rane
7he eed solution $eing treated
7he operating conditions
7he ollowing are some parameters used to measure mem$raneper ormance:
+e&over#4a&tor
&''co$(e = Feed
permeate
Q
Qery
< ere = permeate and = >eed are t e permeate ?o$ rate and t e feed ?o$ rate
respectivel46
easures how mucho the eed is
recovered aspermeate'
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+e e&tion or+etention
&'')* −
= Feed
Permeate Feed
C C C
R
< ere # >eed is t e concentration of a particular species in t e feed and # permeate is t e concentration of t e same specie in t e puri"ed stream6
ransmission Percentage o solutethat is not retained $y
the mem$rane'
easure o the ractiono solute that isretained or the
mem$rane'
&''= Feed
permeate
C
C T RT −=&''or
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$on&entration4a&tor
Feed
tentate
C
C CF (e=
ig #>@s are desirable but, t e4 are limited because it results in a igosmotic
pressure ('O, +>) or cake buildup (M>, U>), $ ic leads to t e cost raise6
De&ontamination 4a&tor
Permeate
Feed
C C
DF =
Dse ul to evaluate theper ormance o wastetreatment processes'
easure o the degree oincreasing the
concentration o acomponent'
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em$rane Per ormance can $e aBected or the ollowing phenomena:
Membrane compaction: Is the decrease in mem$rane permea$ilitycaused or the compression o the mem$rane structure under thetransmem$rane pressure'Concentration polarization: is characteri ed or the accumulation oretained species at the mem$rane sur ace' 8s conse@uence# themem$rane sur ace is su$Nected to a eed concentration that is higherthan the concentration o the $ul eed stream which leads to thedevelopment o high osmotic pressures in reverse osmosis andnano ltration' 7he thic ness o this $oundary layer can $e controlledpartially $y the velocity and tur$ulence o the li@uid pumped over themem$rane during the mentioned cross5 ow operation'
8lthough this phenomenon isreversi$le# the ouling it
causes may not $e'
s detrimentalbecause:
It decreases u& and retention and increases the potential
or ouling through $acterial growth or chemical reactionssuch as precipitation'
It causes stagnant and irreversi$ly $ound ca e ormation inmicro ltration'
In ultra ltration# it causes arising osmotic pressure $uild upand possi$le gel ormation'
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ouling: Is the deposition o su$5micrometre particles (smaller than !m) on the mem$rane sur ace and%or its pores' It occurs whenreNected solids are not transported rom the sur ace o the mem$rane$ac to the $ul stream'
In general# there are our maNor types o ouling:
$om3arison o( 4ouled and $lean Mem1rane
.enerall4, t edi5erent t4pes of
fouling occursimultaneousl46
!issolved solids
2uspended solids
+on/biological organics
iological organisms
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+ri$ing orces for TransportH In general# our diBerent driving orces are possi$le in mem$rane transport:
H Each o the driving orces have a counter in uence on the other u&es in addition to their primary eBect' Fore&le# the pressure gradient can cause a u& o current called the streaming current# $esides the u& o solvent'
D+'>' 4,+$E P+'MA+= E44E$
Pressure Flu& o solvent
Concentration Flu& o solute
Electrical Potential Flu& o electrical current
7emperature Flu& o thermal energy
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According to the Driving Forces for transport ( +e+brane processes
can be classi;ied as ;ollo/s5Pressure Gradient 2P3+
2e)erse os+osis
9ltra;iltration
&icro;iltration
Nano;iltration
apor per+eationGas per+eation
er)aporation
&lectrical potential Gradient 2&3+
1lectrodial.sis
&e+brane electrol.sis
1lectrosorption
1lectro;iltration
1lectroche+ical ion exchange
Concentration gradient 2C3+
'ial.sis
&e+brane extraction$upported li-uid +e+brane $L&E
1+ulsion li-uid +e+brane 1L&E
Non,dispersi)e sol)ent extraction /ithhollo/ ;iber contactors3
Temperature gradient 2T3+
&e+brane distillation
*her+o,os+osis
Pro&esses with &om1ined driving(or&es81lectro,os+o;iltration 1E
1lectro,os+otic concentration 1 CE
Gas separation CE
ie=odial.sis CE
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E&les o applications and separation processes which
compete with the respective mem$rane separation process'Pro&ess A33li&ations Alternative
Pro&esses
icro ltration 2eparation o $acteria and cells romsolutions
2edimentation#Centri ugation
Dltra ltration 2eparation o proteins and virus#concentration o oil5in5water emulsions Centri ugation
3ano ltration 2eparation o dye and sugar#water so tening
+istillation#Evaporation
>everse Osmosis +esalination o sea and $rac ish water#process water puri cation
+istillation#Evaporation#
+ialysis
+ialysis Puri cation o $lood (arti cial idney) >everseosmosis
Electrodialysis 2eparation o electrolytes romnonelectrolytes Crystalli ation#Precipitation
Pervaporation +ehydration o ethanol and organicsolvents +istillation
as Permeation4ydrogen recovery rom process gas
streams#dehydration and separation o air
8$sorption#8dsorption#
Condensation
em$rane+istillation ,ater puri cation and desalination +istillationPerryGs Chemical EngineersG 4and$oo # =th edition# pages 115/= to 115-<'
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Pressure +riven em$rane
ProcessesPressure driven processes are mature technologies with alarge num$er o success ul applications in industrial water andwastewater treatment'
7heir e&i$ility in process con gurations can optimi e
per ormance' 7hey are suita$le or system integration with conventionaltreatment steps'
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P+,$ESS P,+E S'FE 4LUG)L2m h*
P+ESSU+E)3si*
F "'! to 1 mm !"" Q !"""!0 5 -"DF "'""0 to "'!
mm/" Q /"" !" Q !""
3F "'"""0 to"'""0mm
1" Q !0" 6" Q 1"" psig(<"
typically)
>O R "'0 nm !" 5 /0 1"" Q /""
% e follo$ing table s o$s t e most used ressure !riven ( !)Membrane processes and t eir t4pical operating values:
P+mem$raneprocessesprimarily$ased on
species si e
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"ressure +ri$en Membrane "rocesses
Features o; ressure,'ri)en &e+brane $.ste+s ;or 1n)iron+ental Applications3 21F
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Pressure driven mem$rane processes are specially use ul where a wide range o possi$lecontaminants have to $e removed over the entire removal spectrum i'e' macro particles toionic species' Mem1rane
Pore Si%e) µm*
Pressure)1ar*
2e)erse %s+osis 2%E
9ltra;iltration9FE
Nano;iltrationNFE
&icro;iltration&FE
":, :
#:, :
6,6:
6
6: , ,6: ,"
6: ," ,6: ,#
6: ,# ,6: ,6
6: ,6 ,6: 6
#uspended solids
Bacteria
Viruses
'ulti0alent ions
'ono0alent ions
%ater
Retentate2concentrate3
Permeate2filtrate3
4&&D
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4+ 4+
4+
4+
SP
S P
P
P P
4
M M
M
M
M
7here are several types o ows used in mem$rane5$asedseparations' 7he ollowing are some o them:
)a* &o-&urrent <ow
)d* $ross<ow
)e* Dead-end<ow
)1* $om3letel#-mi!ed <ow
)a* &ounter-&urrent <ow
S em$raneF S FeedP S Permeate> S >etentate2 S 2weep
stream
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n pressure driven processes separation is ac ieved eit er b4 dead/endor cross ?o$ mode:
Dead-end flow mode 8 7he eed ow is perpendicular tothe mem$rane and the only outlet or upstream uid isthrough the mem$rane' In this con guration the ow$om$ards the mem$rane sur ace' It is not a veryrecommended mode $ecause the particles accumulatedon the mem$rane sur ace could cause signi cantpressure drop as it $ecomes plugged or ouled'
Cross flow mode : In this mode the eed streammoves parallel to the mem$rane and the uid on thedownstream side o the mem$rane moves away romthe mem$rane in the direction normal to the mem$ranesur ace' 7his con guration reduces material $uildup onthe mem$ranes $y sweeping the material away rom thesur ace'
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Types of OsmosisThere are two types of Osmosis processes
as shown in ig &%&! Direct Osmosis (DO): +O uses low
pressure% The sol$ent passes through themembrane dri$en by the difference insolute concentrations on the two sides%-quilibrium is reached when sufficientwater has mo$ed to equali.e the soluteconcentration on both sides of themembrane%
! Reverse osmosis (RO): (O uses a high# pressure which is larger than O" on thehigh concentration side% So, the carrier is
preferentially permeated, while the
retentate contains the re/ected solute*contaminant)% Thus, the membranedi$ides the water from the contaminants%The main aim is to purify water and notdilute the contaminants%
!"#$%$&'$#M
π
,smoti&Pressure
7he solvent u& isstopped '
Puresolven
t Solution
Mem1rane
(SM(S$S2olvent passes
the mem$rane tothe solution side'
rom lowsolute
concentrationto high
concentration.
∆ P π
'!)!'S!(SM(S$S
7he u& isreversed when aP greater than π is
applied'
rom highsolute
concentrati on to low
concentrati on
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Permeate
eed
'e*ect
In >everse Osmosis a pump is used to raise the pressure and the eed isdistri$uted among a num$er# n # o modules' 7he reNect is collected and ta enor urther treatment# disposal or sale' 7he permeate is recovered andconstitute the clean stream'
>everse Osmosis can$e used in a legion oapplications' 2ome othem are: seawaterdesalting# treatmento cheese whey#metal nishingsolutions# $leach anddye plant e9uent andwaste water romsewage treatment
wor s'
+everse ,smosisPer(orman&e
ultra;ltration
eva3oration
+everseosmosis
eva3oration
lea&h3lant
eCuent
Sugars IJ)w2v* /ater
(orreuseSugars 7J)w2v*
Sugars K7J)w2v*
Lignosul(onates 67J )w2v*
Lignosul(onates K7J )w2v*
+everse ,smosis (or 3ul3ed 3a3er industr# waste
treatment.
+E>E+SE
,SM,S'S
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+E>E+SE ,SM,S'S
MEM +A E A DM,DULES
H,LL,/ 4' E+
4LA SHEE
U ULA+
According toGeometric
Shape ,membranes
can beclassified in
ollo$ >ibermodule
2piral$oundmodule
late and
>ramemodule
%ubularmodule
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)))*mtrinc*com, Pages,4A6,fa-s*html
S3iral-/ound Module8 Consist o twosemipermea$le mem$ranes placed $acto $ac and separated $y a woven a$ricthat unctions as a permeate carrier#designed to prevent the mem$rane rompenetrating into it and to minimi epermeate pressure drop' 7he threeedges o the mem$rane are sealed withadhesive# while the ourth one isattached to a per orated central tu$e',hen the pac age is rolled up# themem$rane layers are separated $y amesh that not only promotes tur$ulence#improving mass trans er $ut alsoreduces concentration polari ation' 7hespirally wound element is inserted into apressure vessel or module housing'
7hus# the pressuri ed eed water owsa&ially into only one ace o the cylinder'
7he permeate passes through themem$rane and down the permeatecarrier and into the per orated centraltu$e# where it is collected and removed'
7he reNect ows out o the other end othe spiral module'
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Plate and 4rame Module8 Consists o circularmem$ranes sealed to $othsides o a rigid plate(constructed o plastic#porous $erglass orrein orced porous paper)#which acts as mechanicalsupport and as permeatecarrier' 7hese units areplaced in a pressuri edvessel or use' Each platein the vessel is at lowpressure# so that permeatepasses through themem$rane and is collectedin the porous media'
u1ular Module8 Each mem$rane is heldin a porous tu$e' In practise# the eedstream is circulated through tu$es inseries or parallel' Permeate solutionpasses through the mem$rane# throughthe tu$e and drops oB into a receptacleor urther permeate removal'
Tubular Module
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Hollow 4i1er Module )H4+,*8 Consist o a shell which houses avery large num$er o hollowmem$rane $ers' 7hemem$rane $ers are grouped ina $undle# evenly spaced a$out a
central eed distri$utor tu$e'One end o the $er is sealedand the other is open to theatmosphere' 7his $undle isinserted into a pressurecontainer or use'
+uring operation# pressuri edeed water is introduced throughthe distri$utor tu$e which owsaround the outer side o the$ers toward the shell perimeter'
7he permeate penetratesthrough the $er wall into the$are side and is removed at the
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AD>A A ES A D D'SAD>A A ES ,4 MEM +A EM,DULES
2PI>8L5,OD3+
4OLLO, FI*E>
7D*DL8>
PL87E 83+F>8 E
H Low manu acturing costH >elatively easy to clean $y $oth
chemical and hydraulic methods'H 4as a very $road range o
applicationsH 4igh pac ing density
H >elatively low manu acturingcost'
H CompactH 4igh pac ing densityH odes energy re@uirement
H Can $e operated on e&tremelytur$id eed waters'
H >elatively easy to clean eithermechanically or hydraulically'
H Can process high suspended solideed with minimal pretreatment'
H oderate mem$rane sur ace'H ,ell5developed e@uipment'
H It can not $e used on highly tur$ideed waters without e&tensivepretreatment'
H 2uscepti$le to plugging $yparticulates
HE&tremely suscepti$le to oulingdue to very small spacing $etween$ers'
H +i;cult to clean'H >e@uires e&tensive pretreatment'H Limited range o applications'H 4igh capital cost'H >elative high volume re@uired per
unit mem$rane area'
H E&pensive to operate or largescale'
H 2uscepti$le to plugging $yparticulates at ow stagnation
points'H Potentially di;cult to clean'
AD>A A ES D'SAD>A A ES
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+, $al&ulationsH In modeling an >O unit we should consider the ollowing aspects: T em$rane 7ransport: +escri$es the phenomena
ta ing place at the mem$rane sur ace ( waterpermeation# etc')
T 4ydrodynamic model: +escri$es the macroscopictransport# the momentum and energy o the species'H 7he 7wo5+ model# as e&plained $y +r' El54alwagi is used or >O
calculations in this section' 7he method captures the radial anda&ial ows in 4F>O model'
H >O calculations demand that we calculate the ollowing:
a) ,ater u&# 3 water$) 2olute u&# 3 solute
c) Permeate owrate# andd) Permeate Concentration'
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Schematic for 0 (O module
! Adopted from 1"ollution "re$ention Through "rocess ntegration Systematic +esign Tools,2 by +r%-l#0alwagi, fig&&%3, page 455%
2ealing >ing
Feeder
4eed
Permeate
L
1> 2
L2
1>
+e e&t
1r i
1r oA #3i&al
Hollow 4i1er
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Water6"henol Mi7tureH 8s seen earlier or a li@uid5 li@uid mi&ture >O is a good
choice' 7he common eed pressure range is !"5=" atmwith a porous to non5porous mem$rane'
H 7he e@uations used or calculations are as ollows:
+, (verall Material &alance 8
where @ F #@> #@P are volumetric owrates per module oeed# permeate and retentate respectively'
1) 7he volumetric -owrate per module is given $y:
nQ
q F F =
R P F qqq +=
,here UV F’ is the total eed volumetric owrate and U nM is the num$er
o modules'
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/) #omponent Material &alance on solute :
where# C F# CP and C > are the concentrations o solute in theeed# permeate and reNect respectively'
6) ater lu/ :
where#
∆P S Pressure diBerence , π S OP o eed# CF S solute concentration in the eed C 2 S average solute concentration in the shell side# and
8 S solvent permea$ility
γ π
−∆= S
F
F water C
C P A N
( ( "",, CqCqCq +=
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6a) 8nd γ is given $y:
89&''&33%&&5&
i
S o
r x LLr A η µ
η γ +=
θ θ
η tanh
=ii
o
r L
r x
r A 4
&
49&''&33%&
&5
= µ
θ
P R F P
P P P −
+=∆
4
4 R F
S C C
C +
=
,here#
6$) 8lso# the pressure di0erence across the mem$rane is :
where P F #P> #PP are pressures o eed# reNect and permeate'
and
or
6c) 7he concentration o solute in the shell is calculated asollows:
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0) Solute lu/ : 3 solute S solute transport parameter T C 2
-) Permeate lowrate :
where# 2 m is the hollow $er sur ace area per module'
=) Permeate Concentration :
S M
solute C K D
N
=
δ 4
water m P N S q =
water
solute P N
N C =
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H Com$ining these e@uations with e@uation 6) we get the ollowing:
R P F F F C qqC q )* −≈
H Considering most o the solute is retained in the reNect#
e@uation /) can $e simpli ed to:
4ence#
7he last e@uation is a @uadratic e@uation that can $e solved or C > 'Once this is done we can calculate e@uations 6) through =) too$taining the end permeate concentration' I this concentration doesnot satis y the target concentration# new values or parameters suchas n # PF or diBerent system con gurations has to $e proposed'
R F
R F m F F F C C
C P AS qC q
+−∆−= γ π
&4
'44
4 =−
−∆−+ F F R
F m F R
F
F m C qC P AS qC
C AS γ
π γ
π
alid or highly reNectingmem$ranes# when
F F P P C qC q <<
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$,S A AL=S'SA$ Annuali%ed ;!ed &ost o( modules Annuali%ed ;!ed &ost o(
3um3
nnuali9ed "7ed cost of pumps (AB4r)C
0601DEF?o$ rate t roug pump (kgBs)G pressure di5erence across pump
(+Bm H )I 06EJ
nnuali9ed "7ed cost of 'O modules (including annuali9ed installed cost,membrane replacements, labor and maintenance)C
yr ulemod:
!#!6"
Cost o electric powerS "'"- W% , hr
7he mechanical e;ciency o pumps and tur$ines was considered as -0J
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+ESULS ,4 H4+, $AL$ULA ',
VFS1<'1 g%sCFS6='< ppmn ma&S -/ >
P
>
P
>
P
VPS6'"/ g%sCPS/0'<< ppm
VFS10'!= g%sC>S00'-1 ppm8limentaciXn
VFS1<'1 g%sCFS6='< ppm
VFS1<'1 g%sCFS6='< ppm
n ma&S -/
VFS1<'1 g%sCFS6='< ppm
n ma&S -/
*y doing 4>FO calculations many diBerent solutions can $e o$tainded or this pro$lemdepending on the modules con guration and the cost analysis' 7he ollowing gure is onesolution# where the target composition is not achieved'
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>
P
VFS1<'1 g%s
CFS6='< ppmn ma&S -/VFS10'!= g%sC>S00'-1 ppm
>
P
>
P
>
VFS!1'". g%sC>S/0'<< ppm
VFS!'= g%sC>S1='"0 ppm
V>S!"'/. g%sC>S6!'.. ppm
8limentaciXnVFS.='0< g%sCFS6='<0ppm P
VPS6'"/ g%sCPS/0'<< ppm
+ESULS ,4 H4+, $AL$ULA ', 7he ollowing diagram shows another solution to our pro$lem# in this solution the targetcomposition is lower $ut as in the last case# the target composition is not achieved'
any con gurations were tried and no one o them gave satis actory results $ecause thecomposition o the permeate was not the desired'
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, SE+>A ', S A D
+E$,MME DA ', S 4,+ '( $AL$ULA ', S
7he permeate stream should meet two re@uirements:
!) 7he permeate owrate should $e no less than a given owrate:
1) 7he concentration o the undesira$le components in the permeateshould not e&ceed a certain limit generally settled $y an
environmental regulation'
min P P QQ ≥
ma7 P P C C ≤
7he owrate per module is typically $ounded $y manu acturer’sconstraints:
ma7min
F F F qqq ≤≤
7he oregoing e@uations assume that mem$rane per ormance is timeindependent# this means the eBects o reduction in permea$ility are notconsidered'
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PP is typically atmospheric'It is advisa$le to maintain moderate to low eed pressure to avoid theincrease o the costs'
8lso in order to reduce the 78C# the num$er o modules should $e minimumand to get that# the owrate per module must $e ma&imum'
In some cases it is use ul to recover energy rom the retentate (Nust when thevalue o recovered energy is higher that the cost o recovering it)# to do it isnecessary to eed this stream to a tur$ine' In those cases the annuali ed&ed cost o tur$ines must $e added to the 78C:
nnuali9ed "7ed cost of turbines (AB4r)C
06K1LHF?o$ rate t roug turbine (kgBs)G pressure di5erence across turbine(+Bm H )I 06KE
>eed 'eject
ermeate
= >
# >
>
= '
# '
'
=# '
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8mmonia and phenol contents are
high and cyanides which areanions o 8mmonia ma e some othe $iological treatments involvingnitri cation%denitri cationwaste ul 1 '
1 >' arr and ' Moucar# >ecovery o ammonia rom industrial wastewater' nt6 # em6 &ng6 66 /(!<</)# p' 6!-
S EAM S +'PP'
N/h# Steam Stri33ingO
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y
2team 2trippingH 8 wastewater stream is contacted with steam in
a pac ed or trayed tower' 7he com$ined eBectso the steam and heat causes pollutants (phenolsand ammonia) to trans er rom the li@uid to thevapor phase' 7he pollutants are carried out withthe vapour' 7he contacting continues down thetower# ma ing the wastewater leaner in theorganic material while the vapor phase richer inpollutants as it travels up the tower'
7he wastewater is ed at the top o the tower' 7he inNectedsteam at the $ottom o the tower provides the re@uired heatand vapor ow' Clean water leaves as $ottoms while thepollutants leave the top heavily laden with organic material'
7his steam%organic com$ination is condensed and processedlater' 7he principal eature o steam stripping is that acontaminated wastewater and steam are inNected into thetower which results in clean water as the end product'
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8spen >8+F>8C*he stea+ stripping processcul+inates to gi)e a clean /aterstrea+ /ith trace a+ounts o;a++onia and phenol strea+#E3 $trea+ contents high
le)els o; phenol and a++oniathat co+e along /ith around# o; the /ater a+ount instrea+ 63 In strea+ " there areno products since thecondenser has a distillation;raction o; =ero3
*he 2A'F2AC ;eature o; Aspenused ;or the si+ulation o;separation process is sho/n inthe ;igure to the right3
B6
6
#
"
F
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2team 2tripping with 8spen
#etup and operating specifications
for steam stripping using AspenRAD4RAC
um1er o( stages 67
$ondenser Par&ial->-L
+e1oiler ettle
Valid Phases >-L
em3erature 77 Q4
Pressure 5R. 3sia
Distillate to feed ratio(mole) 0.25
H 8spen simulation was usedor the steam strippingprocess' 7he con gurationor the setup are given inta$le !'!'
H Further# the temperature
used is 1""oF
near $oilingpoint o water and apressure o !6'= psia# closeto atmospheric pressure'
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>E2DL72H Dsing the setup shown in
gure!'! and running the 8spensimulations# resulted in the datarecorded in the ta$le to theright'
H 2tream !:7otal Feed S -<016!'-=l$%hr
H 2tream 1: ,ater S 01!6!/'-1 l$%hr(7race ammonia and Phenol)'H 2tream /: Condenser set to ero# no
condensation'H 2tream 6: ,ater S !=/.1.'! l$%hr
H 2tream 1 has mostly water andphenol concentration o "'!!=ppm complying with CF>regulations# while water5phenol5ammonia separation in stream6 can $e urthered using othersuita$le separation processes'
#TR&A' 7 8 9 :
*e+perature F #:: # #3 #D D ## 3" "
ressure psi 6 3D # 3# 6
apor Frac : : :
&ole Flo/ lb+ol4hr " :3 # #3 6 : D3 6D
&ass Flo/ lb4hr # 63 D #6 6"3 6 : 6D" # 36
olu+e Flo/ cu;t4hr 6#: 63# D # 3" : ": 3"
1nthalp. &&Btu4hr , 3: #D ," 3 "# ,66 3""
&ass Flo/ lb4hr
A&&%N,:6 3""""""" 3 1," : 3"""""
WA*12 6 : #6 6"3 : 6D"D" 3
H1N%,:6 ""3""""""" :3: 666 " : ""3#D##6
&ass Fraction A&&%N,:6 3" 1,: 63# 1," :3:::""
WA*12 :3 6 :3 :3 D"
H1N%,:6 3D 1,: 636D1,:D :3:::6 6
:366D pp+
+esults o( simulation (or water-3henol-ammonia 1# streamstri33ing
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Conclusions! The most suitable separation technique in according to the separation
achie$ed and the cost analysis was steam stripping% "henol is poorlyre/ected by (O membranes so the cost of applying this technique isnot /ustified%
! ;otwithstanding the foregoing, membrane techniques are a good
option since can reach high purity le$els which can be cheaper in longterm%! Some membrane techniques can be combined with con$entional
methods for the treatment of effluents *hybrid processes)%! Con$entional treatment methods as distillation and adsorption and
membrane techniques not studied in this tier as per$aporation or
membrane<based sol$ent e7traction can be used for the remo$al of phenol and ammonia% =u/aws>i and co#wor>ers studied se$eralseparation techniques with this purpose *(emo$al of phenol fromwastwater by different separation techniques)