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MODUL 6PENGOLAHAN BIOLOGIS ANAEROBIK DAN ANOKSIK SISTEM TERSUSPENSI DAN TERLEKAT
Joni HermanaJurusan Teknik Lingkungan FTSP – ITSKampus Sukolilo, Surabaya – 60111Email: [email protected]
PERENCANAAN PENGOLAHANAIR LIMBAH DOMESTIK (RE091322)Semester Ganjil 2010-2011
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PENDAHULUAN
“OLD” SMALL SCALE ANAEROBIC TREATMENT ( ON SITE ) =
SEPTIC TANK
IPAL KOMUNAL PERKOTAAN = IMHOFF TANK DAN UASB
IMHOFF TANK = LOW RATE SYSTEM KURANG DIMINATI
HIGH RATE SYSTEM = PREFERABLE !
ANOXIC SYSTEM DENITRIFIKASI : ( NO3) N2
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Gambar Upflow Anaerobic Sludge Blanket(a) Skema , (b) Reaktor
(a) (b)
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DESKRIPSI PROSES
PROSES ANAEROBIK
1. TAHAP PEMBENTUKAN ASAM
susbtrat organik kompleks ( karbohidrat, protein, lemak) asam lemak
CONTOH : PENGURAIAN GLUKOSA
TAHAP PEMBENTUKAN ASAM
TAHAP PEMBENTUKAN GAS METHAN
HIDROLISIS
DIURAIKAN O/ BAKTERI FAKULTATIFH2, , CO2 dan CH3COOH
C6H12O6 + 4H2O 2CH3COO- + 2HCO3- + 4H+ + 4H ………………………. (1)
asetat
C6H12O6 + H2O CH3COO- + CH3CH2COO- + HCO3- + 2H+ + H2………. (2)
propionat
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CONTOH : PENGURAIAN GLUKOSA ( LANJUTAN )
C6H12O6 + H2O CH3CH2COO- + 2HCO3- + 3H+ + 2H2……………………….(3)
butirat
CH3CH2COO- + 2H+ + H2O CH3COO- + HCO3- + 2H+ + 3H2…………………...(4)
propionat asetat
CH3CH2CH2COO- + H+ + 2H2O 2CH3COO- + 2H+ + 2H2……………………………..(5)butirat asetat
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FATTY ACIDS, ALCOHOLSAMINO ACIDS, SUGARS
METHANE CARBON DIOXIDE
HYDROGEN CORBON DIOXIDE
ACETATE
INTERMEDIATE PRODUCTS (Propionate, Butyrate, etc)
PROTEIN LIPIDSCARBOHYDRATES
COMPLEX POLYMERS
1 1
11
2
3
5 4
1HYDROLYSIS
HOMOACETOGENESISACETOLASTICMETHANOGENESIS
ANAEROBICOXIDATION
Skema proses anaerobic (Pavlostathis dan Giraldo-Gomez, 1991)
KETERANGAN :]
1. Bakteri fermentatif2. Bakteri Asetogenik
Penghasil Hidrogen3. Bakteri Asetogenik
Pemakan Hidrogen4. Methanogenesis
Reduktif5. Asetoklastik
Methanogenesis
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2. TAHAP PEMBENTUKAN GAS METHAN
BAKTERI METHANOGENESISHYDROGENOTROPHIC
( H2 ; CO2 Methan )
ACETOCLASTIC
( Dekarbolaksilasi Asam Asetat
Methan )
CH3COOH CH4 + CO2……………………….……………………………………………(6)methane
H2 + CO2 CH4 + 2H2…………………………………………………………………….(7)
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Tabel 1. Proses Tahapan Degradasi Senyawa Organik Secara Anaerobik
Tahap Jenis Senyawa Asal
Bakteri Pengurai
Jenis Senyawa Produk
Keterangan
Tahap I : AcidogenesisHidrolysis Protein
KarbohidratLipid
Hydrolysing and fermentation bacteria
Asam amino,GulaAsam LemakAlkohol
Fermentasi Asam amino,GulaAsam LemakAlkohol
-Fermentationbacteria-Hydrogen-producingacetogenicbacteria-Hydrogen-consumingacetogenicbacteria
Produk Perantara (Volatile Fatty Acids, VFA), Asam Asetat, Hidrogen dan CO2
ProsesAcetogenesis
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Tabel 1. Proses Tahapan Degradasi Senyawa Organik Secara Anaerobik( Lanjutan )
Tahap II :MethanogenesisTAHAP JENIS
SENYAWAASAL
BAKTERI PENGURAI
SENYAWAPRODUK
KETERANGAN
AceticlasticMethanogenesis
Asetat Aceticlastic methanogens
Methane danCO2
ReductiveMethanogenesis
Hidrogen CO2 CO2-Reducingmethanogenes(Hydrogenotrophicmethanogens)
Methane danCO2
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PROSES DENITRIFIKASI ( ANOKSIK )
NO3- NO3
- NO N2O N2……………………………………(8)
JIKA KESELURUHAN N BERADA DALAM BENTUK NITRAT, MAKA :
NO3- + 1.08 CH3OH + H+ 0.065 C5H7O2N + 0.47N2 + 0.76COY + 2.44 H2O (9)
JIKA N BERADA DALAM BENTUK NITRIT & MENGANDUNG SEDIKIT OKSIGEN
MAKA :
Cm = 2.47 N0 + 1.53 N1 +0.87 D0
Dimana:Cm = konsentrasi methanol yang diperlukan, mg/lN0 = konsentrasi nitrat awal, mg/lN1 = konsentrasi nitrit awal, mg/lD0 = konsentrasi oksigen awal, mg/l
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PRINSIP RANCANG BANGUN
Jenis Nama Unit Pengolah PenggunaanProses Anoksik:Suspended growthAttached growth
Suspended growth DenitrificationFixed-Film Denitrification
Removal N (Denitrification)Removal N (Denitrification)
Proses Anaerobik:Suspended growthAttached growth
Anaerobik DigestionAnaerobik Cantact Process, ACPUpflow Anaerobic Sludge Bed, UASBAnaerobic Baffled Reactor, ABRAnaerobic Filter Process, AFExpanded Bed, EBR
Stabilisasi (lumpur)Removal BODRemoval BODRemoval BODRemoval BODRemoval BOD
Tabel 2. Jenis proses biologis anaerobik dan anoksik yang umum digunakan
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Proses Influen COD
HRT(jam)
Beban Organik(kgCOD/m3.hari)
Removal COD(%)
ACPUASB
AFEBR
1500 – 50005000 –15000
10000 –20000
5000 - 10000
2 – 104 – 1224 – 485 – 10
0.03 – 0.150.25 – 0.750.06 – 0.300.30 – 0.60
75 – 9075 – 8575 – 8280 – 85
Tabel 3. Kriteria desain dan kinerja prosesanaerobik yang mengolah limbah cair industri.
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MODEL PERSAMAAN KINETIKA : UNTUK REAKTOR TERADUK SEMPURNA (COMPLETE MIXED, STEADY STATE )
( )( )c
c
bSSY
Xθθ
θ+
−=
10
dimana :X = Konsentrasi pertumbuhan mikroorganismaθ = Waktu detensi hidrolis (HRT)θc = Umur lumpur (SRT) atau mean cell residance timeY = Koefisien pertumbuhan mikroorganismeS0, S = Konsentrasi influen dan effluen substrat pembatas pertumbuhanb = Koefisien kematian mikroorganisma
LAJU PERTUMBUHAN MIKROORGANISME ANALOGIS
XdtdX µ=
Dimana :µ = Laju pertumbuhan mikroorganisme spesifik
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Maka :
bSKsS
−+
= maxµµ
Di mana :S = konsentrasi substrat dalam reaktor (massa/volume)µmax = kY = Laju penggunaan substrat spesifik (waktu –1)
k = Laju maksimum penggunaan substrat per unit berat mikroorganisma (waktu –1)
Ks = Koefisien setengah jenuh, sama dengan konsentrasi air buangan atau substrat ketika µ = 1,5 µmax
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bSKs
akSUSRT
−+
==1
Biological Solids Retention Time ( SRT )
SRT > SRT m = 1 / µ
SRT=µ1
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Tabel 4. Koefisien Kinetika Untuk Penggunaan Substrat danPertumbuhan Biologis
Substrat Suhu (0C)
k*(mg/mg-
hr)
Ks(mg/l)
Y**(mg/m
g)
B(hr-1)
SRTm(hr)
Asam AsetatLumpur buangan kotaAsam AsetatAsam PropionatLumpur buangan kotaBuangan susu sintetisAsam asetatAsam asetatAsam PropionatAsam butiratLumpur buangan kotaBuangan pengepakan
20
25
3035
3,6
5,07,8
0,385,18,77,78,3
0,32
2130
869613
24333254325
5,5
0,04
0,050,051
0,370,0540,04
0,0420,047
0,76
0,015
0,0110,04
0,070,0370,0190,010,027
0,017
7,810,0
4,22,87,5
4,74,23,13,22,7
2,8
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PRINSIP REKAYASA PERENCANAAN
1. EFISIENSI PENGOLAHAN
Efisiensi pengolahan pada HRT 4 – 6 jam adalah :COD (total/ total): 50 - 70 %COD (total/ filtered): 70 - 95 %BOD (total/ total): 70 - 90 %COD (filtered/ filtered): diatas 60 %TSS : 60 – 85 %
2. PRODUKSI GAS METHAN0,19 N m3/kg CODremoved
0,33 CH4 COD/kg CODremoved
56 – 63 % gas methan akan keluar bersama efluen
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3. KONVERSI TSS
40 % TSS berada dalam lumpur25 % TSS terkonversi menjadi methane30 % TSS keluar reaktor bersama efluen
4. PRODUKSI LUMPUR
Umumnya 0,1 kg COD/ kg COD in
Nilai maksimum yang diperoleh 0,25 kg COD / kg COD in
0,4 – 0,6 kgTSS/kg TSS in (= 0,06 – 0,1 kg TSS/m3)
5. KONSENTRASI LUMPUR DALAM REAKTOR
31 – 37,5 kg TSS/m3 9,4 – 12,5 kg VSS/m3
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6. UMUR LUMPUR
35 – 100 hari (pada saat reaktor sudah penuh lumpur)7. KARAKTERISTIK LUMPUR
Kandungan abu : 55 – 56 %Specific methanogenic activity : > 0,1 kg/kgVSS.dayStabilitas : 20 – 50 L CH4/kg lumpurKarakteristik pengeringan : 20 kg/m2 dalam 7 hari dan menghasilkan 35 – 40 % DS.
8. KONSENTRASI LUMPUR DALAM SLUDGE BEDDapat mencapai 100 kg TSS/m3 pada bagian bawah reaktor, bergantung pada jenis air limbah domestik yang diolah. Karakteristik air limbah ini dapat mempengaruhi settleability lumpur dan kandungan ash (debu)
9. FAKTOR DESAIN LAIN
Minimum HRT rata-rata adalah 4 jamKetinggian 4 mTitik inlet limbah :1 per 4 m2 apabila reaktor penuh berisi lumpur1 per 1 m2 apabila reaktor terisi sedikit lumpur
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9. FAKTOR DESAIN LAIN
Tekanan statis pada kotak inlet air limbah : sampai dengan 50 cmKecepatan keatas pada saat bukaan: rata-rata harian 4 m/jam, selama 2-4 jam 8 m/jam.Material untuk konstruksi: stainless steel atau plastik (untuk gutter), beton tahan asam dan gunakan bahan anti karat untuk pemisah gas dan pelapisan bagian tertentu.
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JENIS REAKTOR ANAEROBIK Suspended Growth
Complete mixed suspended growth Anaerobic contact process Anaerobic sequencing batch reactor (ASBR)
Anaerobic Sludge Blanket Upflow anaerobic sludge blanket (UASB) Anaerobic baffle reactor (ABR) Anaerobic migrating blanket reactor (AMBR)
Attached Growth Upflow packed-bed reactor Anaerobic expanded-bed reactor Anaerobic fluidized-bed reactor
Covered Anaerobic Lagoon
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UPFLOW ANAEROBIC SLUDGE BLANKET
UASB
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PRINSIP UMUM
•Aliran dalam reaktor = aliran vertikal ke atas ( up flow )•Sludge untuk mendegradasi bahan organik dalam air buangan berada di dasar reaktor
• influen dasar reaktor mengalir ke atas (upflow)
Gas Solid Liquid Separator Gas ditampung GLSS, sludge kembalike zona sludge blanket, air limbahdipompake ke outlet
KEUNTUNGAN•Beban Loading tinggi•Waktu detensi lebih rendah u/ skala anaerobik•Tidak perlu suplai Oksigen / hemat biaya•Dapat mereoval PO4 ( fosfat ) & NH3 ( Nitrat ) menjadi gas N2 melaluiproses denitrifikasi
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SKEMA REAKTOR UASB
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BEBAN VOLUMETRIK
COD air limbah( mg / L )
Fraksi COD partikulat
Volumetric Loading ( Kg COD / m3.hari)
Sludge Flocculant
Granular Sludge Removal TSS tinggi
Granular Sludge Removal TSS rendah
1000 - 2000 0.1 – 0.30.3 – 0.60.6 – 1.0
2 – 42 – 4n.a
2 – 42 – 4n.a
8 – 128 – 14n.a.
2000 - 6000 0.1 – 0.30.3 – 0.60.6 – 1.0
3 – 54 – 84 - 8
3 – 52 – 62 - 6
12 – 1812 – 24
n.a.
6000 - 9000 0.1 – 0.30.3 – 0.60.6 – 1.0
4 – 65 – 76 – 8
4 – 63 – 73 - 8
15 – 2015 – 24
n.a
9000-18000 0.1 – 0.30.3 – 0.60.6 – 1.0
5 – 8n.a.n.a.
4 – 63 – 73 – 7
15 – 24n.a.n.a.
Beban volumetrik COD yg diijinkan untuk removal COD UASB 85 - 95%
Sumber : Lettinga & Hulshoff Pol, 1991
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BEBAN VOLUMETRIKBeban Organik volumetrik yg dianjurkan berdasarkan suhu substrat COD soluble
Untuk removal COD 85 – 95%, konsnetrasi rata-rata sludge = 25 mg / L
SUHU ( C)
VOLUMETRIC LOADING ( Kg s COD / m3.hari )
VFA WASTEWATER NON – VFA WASTEWATER
TIPIKAL RANGE TIPIKAL RANGE
15 3 2 – 4 2 2 – 3
20 5 4 – 6 3 2 – 4
25 6 6 – 12 4 4 – 8
30 12 10 – 18 10 8 – 12
35 18 15 – 24 14 12 – 18
40 25 20 – 32 18 15 – 24
Sumber : Lettinga & Hulshoff Pol, 1991
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BEBAN VOLUMETRIK
Hidraulic Retention Time ( HRT ) τ yang dipakai untuk pengolahan air buangan domestik
Pada kedalaman reaktor UASB = 4 m
SUHU ( C) τ RATA-RATA (jam)
Τ MAKSIMUM, 4 – 6 peak (jam)
16 – 19 10 – 14 7 – 922 – 26 7 – 9 5 – 7
> 26 6 - 8 4 - 5
Sumber : Lettinga & Hulshoff Pol, 1991
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UPFLOW VELOCITY ( v )Upflow Velocity & Reactor Heights Recommended for UASB Reactor
Jenis air buanganUpflow Velocity
( m / jam)Tinggi Reaktor
(m)Range Tipikal Range Tipikal
COD hampir 100% soluble 1 – 3 1.5 6 – 10 8
COD sebagian soluble 1 – 1.25 1 3 – 7 6
Air buangan domestik 0.8 - 1 0.7 3 – 5 5
Sumber : Lettinga & Hulshoff Pol, 1991
ν = Q / A
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DIMENSI REAKTORVOLUME
Vn = Q . S0
Lorg
Vn = volume reaktor nominal ( efektif ) liquid, m3
Q = debit influen , m3/ jamLorg = organic loading rate, Kg COD / m3.hariSo = influen COD, Kg
VL = Vn
E
VL = volume reaktor total liquid , m3
Vn = volume reaktor nominal ( efektif ) liquid, m3
E = faktor efektif, tanpa satuan
A = Q / v
HL = VL / A HT = HT + HG
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Petunjuk Ukuran Luas / Area yang dilayani oleh Saluran Pipa Inlet
Sludge Type COD loading
(Kg/m3.hari)
Area per feed
inlet, m3
Dense flocculent sludge, > 40 kg TSS/m3
Medium Flocculent Sludge, 20 – 40 kg TSS / m3
Granular Sludge
<11 – 2> 2
>1 – 2 > 3
1 – 22 – 4> 4
0.5 – 11 – 2 2 – 31 – 2 2 – 5
0.5 – 1 0.5-2
>2
Sumber : Lettinga & Hulshoff Pol, 1991
Contoh perhitungan UASB Treatment Process Design dapat dilihat pada Metcalf&Eddy,2003 Chapter 10:1012-1016
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INLET
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GENERAL DESCRIPTION High rate reactor firstly developed by Bahman & Mc Carty Consists of several compartments producing gaseous,
designed by using several vertical baffles couraging upflow by activated sludge which allowed contact between microorganism & wastewater
Bacterias tend to grow, move & settle horizontally within each compartment, low velocity, increase Solid Retention Time (SRT) equal to 100 days on Hydraulic Retention Time (HRT) equal to 20 hours
Less HRT ≈ minimizer reactor size ≈ less O&M cost Consists of 3 zone : Acidification Zone Methanation Zone Buffer Zone
ANAEROBIC BAFFLED REACTOR
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ZONE CLASSIFICATION
1. Acidification ZoneOccurred mostly on intial compartmentVolatile fatty acid ( VFA) formation decrease pH valueBuffer capacity increased, pH value = increased
2. Methanation ZoneMethane gas produced
3. Buffer ZoneDetermined to stabilize the process
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ADVANTAGES ( Barber & Stuckey, 1999 )
1. Constructiona. simply designb. no need mechanical mixingc. minimize cloggingd. minimize sludge bed expansione. low construction costf. low O & M cost
2. Biomassaa. no need biomass with special settlingb. low sludge growthc. high SRTd. no need fixed medium / solid settling chambere. no need gaseous / sludge separation
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ADVANTAGES ( Barber & Stuckey, 1999 )
3. Operationala. Low HRTb. allowed intermittent operationalc. stabil hydraulic shock loadingd. long operational without sludge disposal
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ATTACHED GROWTH ANAEROBIC PROCESSES
• Upflow Packed-Bed Attached
• Upflow Attached Growth Anaerobic Expanded-Bed Reactor
• Attached Growth Anaerobic Fluidized-Bed Reactor
• Downflow Attached Upflow Attached Growth Processes
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Nitrogen removal
Nitrification and denitrification
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Nitrogen CycleNO2
-
NH2 groupof protein
NON2O
NH3
N2
N2
NO3-
NH2 groupof protein
NO2-
AnoxicOxic
Nitrification
Nitrogenfixation
Denitrification
Nitrogenfixation
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Nitrogen removal
Ammonia nitrogen(NH4
+)
zNitrite (NO2-)
zNitrite (NO3-) zNitrogen (N2)
Organic nitrogen
(bacteria cells)
Organic nitrogen(net growth)
Organic nitrogen(protein;urea)
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Key Processes and Prokaryotes in the Nitrogen Cycle
Processes Example organisms
Nitrification (NH4+ NO3
-)NH4
+ NO2- Nitrosomonas, Nitrosospira
NO2- NO3
- Nitrobacter, Nitrospira
Denitrification (NO3- N2) Bacillus, Paracoccus, Pseudomonas
N2 Fixation (N2 + 8H NH3 + H2)Free-living
Aerobic Azotobacter, CyanobacteriaAnaerobic Clostridium, purple and green bacteria
Symbiotic (w/ plants) Rhizobium, Bradyrhizobium, Frankia
Ammonification (organic-N NH4+)Many organisms can do this
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Biological Removal of Nitrogen and Phosphorus
Anaerobic-Anoxic-Aerobic Process (A2/O)
Influent
Sludge recycle
Settler Settler
Mixed-liquor NO3- recycle
Effluent
Aerobic Anoxic Anaerobic
Sludge waste
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Step-Feed Biological Nitrogen Removal process
Low Energy Cost and High Removal Rate of Nitrogen
Influent
Sludge recycle
Settler
Settler
Mixed-liquor NO3– recycle
Effluent
Aerobic Anoxic Anoxic Aerobic
Sludge waste
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One-Sludge Denitrification by Biomass Storage and Decay
Sludge recycle
Aerobic Anoxic
Sludge waste
BOD0
TKN0 Low BODLow NO3
–
High NH4+
BOD oxidation Nitrification Biomass synthesis
NO3–
Biomass
Denitrification with biomass as donor
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One-Sludge Denitrification by Simultaneous nitrification with denitrification
Sludge recycle
Sludge waste
BOD0
TKN0 Low BODLow NO3
–
Low NH4+
Controlled Low D.O. Simultaneous nitrification, denitrification, and BOD oxidation θ X > 15 days
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Biofilm predenitrification
Aerobic biofilm reactor Nitrification Aerobic BOD oxidation
Anoxic biofilm reactor Denitrification
High effluent recycle to return NO3–
Influent Effluent
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Biological Nitrification
Conditions pH: 7.5 - 8.6DO: above 1 mg/L
Nitrosomonas
Nitrobactor
400NO2− + NH4
+ + 4HCO3 + HCO3− +195O2
→ C5H7O2N + 3H2O + 400NO3−
NH4+
NO2-
NO3-
3222275
324
1045754
1097655
COHOHNONOHC
HCOONH
+++→
++−
−+
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Biological DenitrificationNO3
- NO2- NO N2O N2
Microorganisms:
Achromobacter, Aerobacter, Alcaligenes, Bacillus, Brevibacterium,Flavobacterium, Lactobaillus, Micrococcus, Proteus, Pseudomonas, Spirillum
Conditios:pH: 7 - 8DO: anoxic
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Pond Treatment ProcessesAerobic Stabilization Ponds
Fig. symbiotic relationship between algae and bacteria
Factors: organic loading, degree of pond mixing,pH, nutrients, sunlight, temperature
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Pond Treatment Processes
Fig. Facultative Ponds
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Phosphorus Removal
C & N
C, N, &P
algae
EUTROPHICATION
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(mg/L)
municipal wastewater 12
conventional wastewater treatment 6
effluent standard for a protected watershed 1
Additional phosphorus removal is necessary
Total P concentration
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Phosphorus RemovalPhosphorus in wastewater
Orthophosphate (PH43-)
Polyphosphate (P2O7)Organically bound phosphorus 70% of influent
10 - 30 % removal by secondary biological treatment:Utilization for cell synthesis and energy transport
Additional phosphorus removal is necessary
Anaerobic zone
Aerobic zone(Oxic zone)
Enhanced Biological Phosphorus Removal
Release of stored phosphorus
Additional uptake of phosphorus
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Phosphorus RemovalPhoStrip process
Biological Release of Phosphorus
Concentrated phosphorus
Precipitationof phosphorus
Fig. (a)
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Activated Sludge Process
① ② ③
①, ③: Chemical precipitation
②: Biological treatment
Phosphorus removal from wastewater
Normal phosphorus uptake into biomass (11.1)
Precipitation by metal-salts addition to a biological process (11.2)
Enhanced biological phosphorus removal (11.3)
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