Biological Treatment Of petroleum Waste Water

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Biological Treatment Of petroleum Waste Wate

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Tayseir .M. Ahmed (1), Salma .E . Abdalkreem(2), Gurashi .A Gasmelseed(3) , Samah.S.Abdalkhalig(4)

1Red Sea University , Department of Chemical Engineering , Port Sudan, Sudan

2Red Sea University , Department of Chemical Engineering , Port Sudan, Sudan 3 University of Science and Technology ,P .o Box 30, Omdurman, Sudan

4Red Sea University , Department of Chemical Engineering , Port Sudan, Sudan ***

ABSTRACT:

Thewastewaterfrompetroleumindustriescontainshighorganicmattercontent,oilandgrease ,dissolvedsolids and turbidity.Thepetroleumwastewaternormallytreatedinaplantcomprisingofprimary,secondaryandtertiarytreatment .Thehighorganicloadingneedstobetreatedinbiologicaltreatmentstep.Biologicaltreatmentcanbesuspendedgrowth or attached growth type. The anaerobic treatment have advantages such as reduction in sludge content , many investigatorshaveinvestigatedbiologicaltreatmentofpetroleumrefinerywastewater.

Key Words : Biologicaltreatment,MaterialandEnergyBalance ,wastewater

1 Introduction :

Pollutionofwateroccurswhenoneormoresubstancesthatwillmodifythewaterinnegativefashionaredischargedin it.Thesesubstancescancauseproblemsforpeople,animalsandalsofortheenvironment(1) Wastewatercanbedefinedas theflowofusedwaterdischarged,fromhomes,businessesindustries,commercialactivitiesandinstitutions .Wastewater treatment is the process of purification of wastewater from impurities, suspended substances, pollutants and organic mattertobecomereusable(non human)ortobedisposedofinthewaterwayswithoutcausingcontamination(1)

2 Wastewater and petroleum wastewater :

The refineries were classified into either hydro skimming unit, which include a crude distillation unit, a desulphurising unitandareformingunit,oracomplexunit,whichincludeacatalyticcrackingunitwiththehydro skimmingrefinery.In addition, Petrochemical plants were sometimes incorporated within the refinery complex. In general, the pollutants in wastewatercanbedividedintoorganicmatter,inorganicmatterswhichincludenitrogen,phosphorus,ammoniaandiron chloridesaswellasheavymetals.

The organic compounds and ammonia nitrogen considered the principal chemical characteristics of environmental concern in wastewater. The chemical oxygen demand (COD) and 5 day biochemical oxygen demand (BOD5) are used as parameterstodescribeorganicmatterinwastewater(2)

3 Petroleum wastewater generation in refineries:

Transforming crude oil into useful products such as Gasoline and kerosene was achieved by the numerous refinery configurations. During these processes, the petroleum wastewater was generated in the units such as Hydro cracking, Hydro cracker flare, Hydro skimming, Hydro skimmer flare, sourwater, Condensate, Condensate flare and the desalter. Normal alkanes(C10 C21),aromatics,andpolycyclichydrocarbons(3)

4 Current petroleum wastewater treatment techniques :

The petroleum wastewater treatments are classified into three types; physical, chemical and biological. However, the treatment required a typical application of the integrated system due to the complexity of characteristics of petroleum wastewater. Thus, the conventional treatment methods need multistage process treatment. The first stage consisted of pre treatment, which includes mechanical and physicochemical treatments followed by the second stage which is the advanced treatment of the pretreated wastewater. the techniques and methods for petroleum wastewater treatment includedphysical,chemical,biologicaltreatmentprocessing(3) .

International Research Journal of Engineering and Technology (IRJET) e ISSN:2395 0056

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Material Balance :

AmassbalancealsocalledaMaterial Balanceisanapplicationofconservationofmasstotheanalysisofphysical systems(5). By accounting for a material entering and leaving a system, mass flows can be identified which might havebeenunknown,ordifficulttomeasurewithoutthistechnique.Theexactconservationlawusedintheanalysis of the system depends upon the context of the problem but all revolve around the mass conservation, i.e. that mattercannotdisappearorbecreatedspontaneous

Quantityofmaterialsentering=amountofmaterialsoutsideofmaterialsentering=amountofmaterialsoutside

International Research Journal of Engineering and Technology (IRJET) e ISSN:2395 0056 Volume: 09 Issue: 06 | June 2022 www.irjet.net p ISSN:2395 0072

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Overallmaterialbalance: F1=F2+F3 30000=F2+67.065 F2=29932.935kg/hr Error=0 6 3 Material balance bio reactors: Determinetheamountofreflux(5): RAS=0.75*F2+0.25*Bacteria*(1 XA) =0.75*29932.93+0.25*2.61*(1 0.9)

RAS=22449.7 8COHNS+4O2+1/3N+bacteria 3CO2+1/3NH3+C5H7NO2+otherendproduct Table (4) stoichiometric calculations follows Component Mole Change(90%) Remaining COHNS 0.0349 0.03141 0.00349 O2 0.12 0.12 0 C02 0 0.094 0.094 H2O 1662.79 0 1662.79 NH3 0 0.01 0.01 C5H7NO2 0 0.03141 0.03141 Bacteria 0.0349 0.0394 0 N 0.01 0.01 0 otherendproducts 0 0.0349 0.0349

Table (5) Overall and Component input Material Balance on Multi component bio reactors Component Stream F2 IN Mole Kg/hr W% OIL 0.0088 0.66 0.0012 TSS 0.0035 0.2625 0.0005

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BOD 0.004 0.3 0.00057 COD 0.009 0.675 0.0012 PHENOL 0.0096 0.72 0.0013 N 0.01 0.14 0.00026 O2 0.12 3.84 0.0073 Bacteria 0.0349 2.61 0.0049 H2O 1662.79 29930.31 57.13 RAS 22449.7 42.85 TOTAL 52389.49 100

Table (6) Overall and Component output 1 Material Balance on Multi component bio reactors:

Component Stream F4 out1 Mole Kg/hr W%

OIL 0.0088 0.594 0.0011 TSS 0.0035 0.236 0.00045 BOD 0.004 0.27 0.00051 COD 0.009 0.607 0.00115 PHENOL 0.0096 0.648 0.00123 H2O 1662.79 29930.31 57.136 RAS 22449.7 42.85 otherendproducts 0.0349 0.89 0.0016 TOTAL 52383.25 100

Table (7) Overall and Component output 1 Material Balance on Multi component bio reactors:

Component Stream F4 out2 Mole Kg/hr W% Co2 0.94 3.88 95.80 Nh3 0.01 0.17 4.19 TOTAL 4.05 100

F2=52389.49kg/hr RAS=22449.7Kg/hr F4=52383.52Kg/hr F5=4.05Kg/hr Erorr=0.003

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Table ( 8) The organic materials were removed in the proportions shown in the table below {5} Component Percentage in removal % OIL 94 TSS 97.6 BOD 94.4 COD 93.4 PHENOL 65 Table ( 9) : Overall and Component Material Balance on Multi component secondary clarifiers Unit Stream F4 in Stream F7 out Stream F6 out Component W% Kg/hr W% Kg/hr W% Kg/hr OIL 0.0011 0.594 0.0024 0.5583 0.00011 0.0366 TSS 0.00045 0.236 0.001 0.230 0.000018 0.0056 BOD 0.00051 0.27 0.00113 0.2548 0.000050 0.0151 COD 0.00115 0.607 0.00252 0.566 0.000133 0.04 PHENOL 0.00123 0.648 0.0018 0.42 0.00075 0.226 H2O 57.136 29930.31 99.99 29930.31 RAS 42.85 22449.7 99.9 22449.7 otherend products 0.0016 0.89 0.0039 0.89 TOTAL 100 52383.25 100 22452.61 29930.632 F4=52383.25Kg/hr F6=29930.632Kg/hr F7=22452.61Kg/hr Error=0.00001

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ISSN:2395 0072

OIL 0.0024 0.5583 19.1 0.5583

TSS 0.001 0.230 7.9 0.230 BOD 0.00113 0.2548 8.75 0.2548 COD 0.00252 0.566 19.4 0.566 PHENOL 0.0018 0.42 14.43 0.42 100 RAS 99.9 22449.7 22449.7 otherend products 0.0039 0.89 30.59 0.89 TOTAL 22452.61 100 2.91 100 22449.7 F7=22452.61Kg/hr RASOUT=22449.7Kg/hr F8=2.91Kg/hr Error=0 6 6 Material balance at digester : F8+F3=2.91+67.065=69.975kg/hr 1kg 0.2kgbiogas

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69.975 x X=13.99kg/hr(biogas) Sludge=69.975 13.99 =55.98kg/hr F10=13.99Kg/hr F11=55.98Kg/hr Error=0.0007

6 7 Material balance at Activated Carbon:

Filterpercentage65%

Table (11) : Overall and input Component Material Balance on Multi component Activated Carbon Component Stream F6IN Kg/hr W%

OIL 0.0366 0.0001 TSS 0.0056 0.0000187 BOD 0.0151 0.000050 COD 0.04 0.000133 PHENOL 0.226 0.00075 H2O 29930.31 99.99 Total 29930.632 100

Table (12) : Overall and output Component Material Balance on Multi component Component Stream F9 Out Kg/hr W%

OIL 0.0023 0.0000076 TSS 0.0036 0.00012 BOD 0.0098 0.000032 COD 0.026 0.000086 PHENOL 0.146 0.000487 H2O 29930.31 99.99 Total 29930.497 100

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F6=29930.632Kg/hr F9=29930.497Kg/hr

7 Energy Balance:

Energycanbeconsideredtobeseparatelyconservedinallbutnuclearprocesses.Theconservationofenergy,however, differsfromthatofmassinthatenergycanbegenerated(orconsumed)inachemicalprocess.Materialcanchangeform, newmolecularspeciescanbeformedbychemicalreaction,butthetotalmassflowintoaprocessunitmustbeequaltothe flowoutatthesteadystate(5)

7-1 Energy Balance at primary clarifiers:-

Generally: Q=MCPT Where: Q=quantityofheat(kj/hr). M=massflowrate(kg/hr). CP=specificheat(kj/kg.c)

Table( 13 ) Input energy balance at primary clarifiers :

Stream F1input Cpi*mi Cpi Mass in kg/hr Component 13.794 2.09 6.6 OIL 14.7 2.8 5.25 TSS 5.496 0.916 6 BOD 12.366 0.916 13.5 COD 6.864 1.43 4.8 PHENOL 125248.83 4.18 29963.85 H2O 125303.05 30000 TOTAL

Qin=(∑icpi*mi)*T =125302.05*30=3759061.5kj/hr

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Table( 14 ) output energy balance at primary clarifiers : Stream F2 output 1

Cpi*mi Cpi Mass in kg/hr Component 1.3794 2.09 0.66 OIL 0.735 2.8 0.2625 TSS 0.2748 0.916 0.3 BOD 0.6183 0.916 0.675 COD 1.0296 1.43 0.72 PHENOL 125108.72 4.18 29930.318 H2O 125112.76 29932.935 TOTAL

Table( 15 ) output energy balance at primary clarifiers:Stream F3 output 2

Cpi*mi Cpi Mass in kg/hr component 12.14 2.09 5.94 OIL 13.965 2.8 4.9875 TSS 5.2212 0.916 5.7 BOD 11.747 0.916 12.825 COD 5.83 1.43 4.08 PHENOL 140.16 4.18 33.532 H2O 189.33 67.065 TOTAL Qout=(∑icpi*mi)*T Q(F2)=125112.76*30 =3753382.8Kj/hr Q(F3)=189.33*30 =5679.9Kj/hr Qout=Q(F2)+Q(F3)=3753382.8+5679.9 Qout=3759062.7kj/hr Load=Qout Qin=3759062.7 3759061.5 Load=1.2kj/hr

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7 2 Energy Balance at Bioreactor: Table(16 ) Input energy balance on bioreactor :Stream F2 input1 Cpi*mi Cpi Mass in kg/hr Component 1.379 2.09 0.66 OIL 0.735 2.8 0.2625 TSS 0.2748 0.916 0.3 BOD 0.6183 0.916 0.675 COD 1.0296 1.43 0.72 PHENOL 125108.69 4.18 29930.31 H2O 0.145 1.0395 0.14 N 3.517 0.916 3.84 O2 3.393 1.3 2.61 Bactera 125119.77 2993.51 TOTAL StreamRASinput2 28059.88 1.24 22449.7 RAS Qin=(∑icpi*mi)*T =125119.77*30=3753593.1kj/hr Qin(RAS)=28059.88*30=841796.4Kj/hr Qin=Q(F2)+Q(RAS) =3753593.1+841796.4 =4595389.5Kj/h

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Table(17 ) output energy balance at bioreactor : Stream F4 output1 Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 1.02 1.73 0.594 OIL 0.613 2.6 0.236 TSS 0.243 0.9 0.27 BOD 0.546 0.9 0.607 COD 0.77 1.2 0.648 PHENOL 103858.17 3.47 29930.31 H2O 27837.62 1.24 22449.7 RAS 0.0061 0.00695 0.89 OTHEREND 131698.96 52383.25 TOTAL STREAM F4

Stream F5 output2 3.298 0.85 3.88 Co2 0.714 4.2 0.17 NH3 4.012 4.05 TOTAL Qout=(∑icpi*mi)*T Q(F4)=131702.39*35=4609463.88 kj/hr Q(F5)=4.012*35=140.42Kj/hr Qout=Q(F4)+Q(F5)=4609463.88+140.42 =4609604.30kj/hr Load= Qout Qin =4609604.30 4595389.5 Loadofreaction=14214.8kj/hr 7 3 Energy Balance at secondary clarifiers:

Table (18 ) input energy balance at secondary clarifiers:

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Stream F4 input

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 1.02 1.73 0.594 OIL 0.613 2.6 0.236 TSS 0.243 0.9 0.27 BOD 0.546 0.9 0.607 COD 0.77 1.2 0.648 PHENOL 103858.17 3.47 29930.31 H2O 27837.62 1.24 22449.7 RAS 0.0061 0.00695 0.89 OTHEREND 131698.96 52383.25 TOTAL STREAM F4

Qin=(∑icpi*mi)*T Qin=131698.96*35=4609463.88kj/hr

Table(19 ) output energy balance at secondary clarifiers:-

Stream F6 output 1

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 0.0615 1.73 0.0356 OIL 0.014 2.6 0.0056 TSS 0.0135 0.9 0.0151 BOD 0.036 0.9 0.04 COD 0.271 1.2 0.226 PHENOL 103858.17 3.47 29930.31 H2O 103858.56 29930.632 TOTAL Stream F7 output 2 0.965 1.73 0.5583 OIL 0.598 2.6 0.230 TSS 0.229 0.9 0.2548 BOD 0.509 0.9 0.566 COD 0.504 1.2 0.42 PHENOL 27837.62 1.24 22449.7 RAS 0.0061 0.00695 0.89 OTHEREND 27840.43 22452.61 TOTAL

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Qout=(∑icpi*mi)*T

Q(F6)=103858.56*35=3635049.6kj/hr

Q(F7)=27840.43*35=974415.05kj/hr

Qout=Q(F6)+Q(F7)=4609464.6kj/hr

Load=Qout Qin=o.77kj/hr

7 4 Energy Balance at splitter:

Table(20 ) input energy balance at splitter

Stream F7 input

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 0.965 1.73 0.5583 OIL 0.598 2.6 0.230 TSS 0.229 0.9 0.2548 BOD 0.509 0.9 0.566 COD 0.504 1.2 0.42 PHENOL 27837.62 1.24 22449.7 RAS 0.0061 0.00695 0.89 OTHEREND 27840.43 22452.61 TOTAL

Qin=(∑icpi*mi)*T

Qin=27840.43*35=974415.05kj/hr

Table( 21 ) output energy balance at plitter

Stream F8 output1

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component

0.965 1.73 0.5583 OIL 0.598 2.6 0.230 TSS 0.229 0.9 0.2548 BOD

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0.509 0.9 0.566 COD 0.504 1.2 0.42 PHENOL 0.0061 0.00695 0.89 OTHEREND 2.811 2.91 TOTAL

Stream output2 Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 27837.62 1.24 22449.7 RAS 27837.62 22449.7 TOTAL Qout=(∑icpi*mi)*T Q(F8)=2.811*35=98.385Kj/hr Q(RAS)=27837.62*35=974316.7Kj/hr Qout=Q(F8)+Q(RAS)=98.385+974316.7Kj/hr =974415.085kj/hr Load=Qout Qin=0.035Kj/hr

7 5 Energy Balance at Digester: Table(22 ) input energy balance at digester StreamF3input1 Cpi*mi Cpi Massinkg/hr Component 12.14 2.09 5.94 OIL 13.965 2.8 4.9875 TSS 5.2212 0.916 5.7 BOD 11.747 0.916 12.825 COD 5.83 1.43 4.08 PHENOL 140.16 4.18 33.532 H2O 189.32 67.065 TOTAL

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Stream F8 input2

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 0.965 1.73 0.5583 OIL 0.598 2.6 0.230 TSS 0.229 0.9 0.2548 BOD 0.509 0.9 0.566 COD 0.504 1.2 0.42 PHENOL 0.0061 0.00695 0.89 OTHEREND 2.811 2.91 TOTAL

Qin=(∑icpi*mi)*T

Q(F3)=189.32*30=5679.6Kj/hr Q(F8)=2.811*35=98.385Kj/hr Qin=Q(F3)+Q(F8)=5777.9kj/hr

Table(23 ) output energy balance at digester

Stream F10 output1

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 30.778 2.2 13.99 BIOGAS Stream F11 output2 233.99 4.18 55.98 SLUDGE

Qout=(∑icpi*mi)*T Qout(F10)=30.778*35=1077.23Kj/hr Qout(F11)=233.99*35=8189.65Kj/h Qout=Q(F10)+Q(F11)=9266.88Kj/hr

Load=Qout Qin=3488.9kj/hr

7 6 Energy Balance at Actived Carbon:

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Table (24)input energy balance at Actived carbon

StreamF6input

Cpi kj/kg.c Massinkg/hr Component 0.0615 1.73 0.0356 OIL 0.014 2.6 0.0056 TSS 0.0135 0.9 0.0151 BOD 0.036 0.9 0.04 COD 0.271 1.2 0.226 PHENOL 103858.17 3.47 29930.31 H2O 103858.56 29930.632 TOTAL Qin=(∑icpi*mi)*T Qin=103858.56*35=3635049.6kj/hr

Cpi*mi

Table(25 )output energy balance at Actived carbon Stream F9 output

Cpi*mi Cpi kj/kg.c Mass in kg/hr Component 0.0039 1.73 0.0023 OIL 0.0093 2.6 0.0036 TSS 0.0088 0.9 0.0098 BOD 0.0234 0.9 0.026 COD 0.1752 1.2 0.146 PHENOL 103858.17 3.47 29930.31 H2O 103858.39 29930.497 TOTAL Qout=(∑icpi*mi)*T 103858.39*35=3635043.65kj/hr = Load=Qout Qin=3635043.65 3635049.6= 5.95kj/hr

8 Conclusions

The waterdrainagewithactivatedsludgeusinga reactor in the phaseof biological processingcarried outby bacteria in thepresenceofoxygen,whichproducescleanwaterandlessharmfulproductsplusenergyandsowecanbenefitfromthe treatedwaterinhygieneandforthepurposesofagricultureandirrigationoflandandothers.

ACKNOWLEDGENT

TheauthorswouldliketoacknowledgesupportofCollegeofGraduateandportSudanRefineryparticularly.

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