BAB IV KESIMPULAN DAN SARAN
5.2 Saran
Adapun saran yang dapat diberikan untuk penelitian selanjutnya adalah
1. Sebaiknya dilakukan penelitian lanjutan dengan variasi suhu yang berbeda untuk melihat peningkatan produksi biogas pada suhu yang lebih tinggi.
2. Sebaiknya pada penelitian selanjutnya sebelum pergantian HRT dan laju pengadukan ditunggu hingga laju produksi biogas konstan untuk mengetahui waktu di mana laju produksi biogas tertinggi pada kondisi tersebut.
3. Sebaiknya pada variasi pengadukan agar dapat terlihat dengan jelas pengaruh pengadukan terhadap perkembangbiakan mikroorganisme.
4. Sebaiknya ditambah satu reaktor baru pada rangkaian peralatan dengan umpan dari aliran keluar reaktor pertama agar degradasi bahan organiknya lebih baik.
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DAFTAR PUSTAKA
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Semarang.
Azmi, Nazatul Shima, Khairul Faezah Md Yunos, Azhari Samsu Baharuddin dan Zanariah Md Dom, “The Effect of Operating Parameters on Ultrafiltration and Reverse Osmosis of Palm Oil Mill Effluent for Reclamation and Reuse of Water”, BioResources 8(1), 76-87.
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Bala, Jeremiah David, Japareng Lalung, Norli Ismail, “Biodegradation of Palm Oil Mill Effluent (POME) by Bacterial’, International Journal of Scientific and Research Publications, (Maret 2014) Volume 4, Issue 3.
Chaisri, R Boongsawang, Prasertsan, dan Chaiprapat. 2007. Effect Of Organic Loading Rate on Methane and Volatile Fatty Acids Production From Anaerobic TreatmentOf Palm Oil Mill Effluent In UASB and UFAF Reactors. Departemen Industri Bioteknologi. Fakultas Agro-industri.
Universitas Songkla.
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Christy E. Manyi-Loh, Sampson N. Mamphweli, Edson L. Meyer, Anthony I.
Okoh, Golden Makaka dan Michael Simon. “Microbial Anaerobic Digestion (Bio-Digesters) as an Approach to the Decontamination of Animal Wastes in Pollution Control and the Generation of Renewable Energy”. International Jurnal Environment Resources Public Health , 10, hal. 4390-4417, ISSN 1660-4601. 2013.
Chunseng Zhang, Haijia Su, Jan Baeyens, Tianwei Tan, “Reviewing the Anaerobic Digestion of Food Waste for Biogas Production”, Jurnal Renewable and Sustainable Energy Reviews, 338 (2014): hal. 383-392.
CN Osuji, EU Nwabueze, TO Akunna, EO Ahaoutu, “Rapid Fermention Process of Fruit Waste and Abtoir Effluent,” Internional Journal Of Applied Sciences And Engineering, (04 Juli 2013), page 52.
Fang, C., Angelidaki, I., dan Boe, K. 2010. “Biogas production from food-processing industrial wastes by anaerobic digestion”. Kgs. Lyngby, Denmark: Technical University of Denmark (DTU).
Fang, Cheng, Sompong O-Thong, Kanokwan Boe, dan Irini Angelidaki. 2011.
Comparison of UASB and EGSB Reactors Performance, for Treatment of Raw and Deloiled Palm Oil Mill Effluent (POME). Journal of Hazardouz Materials.
Ghanimeh, Sophia, Mutasem El Fadel, and Pascal Saikaly. Mixing Effect on Thermophilic Anaerobic Digestion of Source-Sorted Organic Fraction of Municipal Solid Waste. “Bioresource Technology Journal”. 117, hal : 63-71. 2010.
Goswami, Shyam. “Optimization of Methane Production from Solid Organic Waste”. (2005).
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Hosseini, Seyed Ehsan dan Mazlan Abdul Wahid. “Feasibility study of biogas production and utilization as a source of renewable energy in Malaysia”.
Renewable and Sustainable Energy Reviews 19 (2013) 454–462.
Jeong, Joo-Young., Sung-Min Son., Jun-Hyeon Pyon., dan Joo-Yang Park.
“Performance Comparison Between Mesophilic and Thermophilic Anaerobic Reactors for Treatment of Palm Oil Mill Effluent”, Jurnal
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Bioresource Technology, 165 (2014).Menteri Lingkungan Hidup, 2014, No.1815, 2014.
Jhon C. Kabaouris, Ulas Tezel, Spyrus G. Paulustis, Michael Engelmann, James A Daulane, Allen C. Todd,Robert A. Gillette, “Meshophilic and Thermophilic Anaerobic Digestion pf Municipal Sludge And F, Oil, Grease”, Proquest, Wer Environtment Research, Vol. 81, No. 5, (Mei 2009) page 476-485.
Jingquan, Lu. “ Optimizion Of Anaerobic Digestion Of Sewage Sludge Using Thermophilic Anaerobic Pre-Trement” Dissertion, The Technology University, Denmark, 2006, page 6 – 25.
Jin-Young Jung, Sang-Min Lee, Pyong-Kyun Shin, Yun-Chul Chung, “Effect of pH on Phase Separated Anaerobic Digestion”, Jurnal Biotechnology Bioprocess Engineering, 5(6) 2000: hal 456-459.
Johan Lindmark,” Developing The Anaerobic Digestion Process Through Technology Integration”, Mälardalen University Press Dissertations, (2014) No. 165.
Joko Padmono. 2007. Kemampuan Alkalinitas Kapasitas Penyanggaan (Buffer Capacity) dalam Sistem Anaerobik Fix Bed. Pusat Teknologi Lingkungan, Jurnal Teknik Lingkungan Vol. 8, No.2, Hal 119-12.
I. J. Dioha, C.H. Ikeme, T. Nafi’u, N. I. Soba and Yusuf M.B.S, “Effect Of Carbon To Nitrogen Rio On Biogas Production,” Internional Research Journal of Nural Sciences, Vol. 1, No. 3, (September 2013), page 1 -10.
Karena Ostrem. 2004. “Greening Waste: Anaerobic Digestion for Treating The Organic Fraction of Municipal Solid Wastes”. Thesis. Earth Resources Engineering. Columbia Univesity.
Kaviyarasan, K. 2014. Application of UASB Reactor in Industrial Waste Water Treatment – A Review. International Journal of Scientific & Engineering Research, 5 (1).
Kementrian Lingkungan Hidup, 2014, No.1815, 2014.
Khemkhao, Maneerat, Boonyarit Nuntakumjorn, Somkiet Techkarnjanaruk, dan Chantaraporn Phalakornkule. 2012. UASB Performance and Microbial Adaptation During a Transition from Mesophilic to Thermophilic
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Treatment of Palm Oil Mill Effluent. Journal of Environmental Management.
Lemmer, Andreas, Hans-Joachim Naegele, Jana Sondermann,”How Efficient are Agitators in Biogas Digesters? Determination of the Efficiency of Submersible Motor Mixers and Incline Agitators by Measuring Nutrient Distribution in Full-Scale Agricultural Biogas Digesters”, Energies, (2013), 6, hal. 6255-6273.
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Lubis, A. Haikel. 20018. Pengaruh Rasio Recycle Terhadap Produksi Biogas Menggunakan Reaktor Tangki Berpengaduk dengan Bantuan Membran Ultrafiltrasi pada suhu 45 oC. Departemen Teknik Kimia, Universitas Sumatera Utara. Medan.
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LAMPIRAN 1 DATA HASIL ANALISA
L1.1 KARAKTERISTIK LIMBAH CAIR PABRIK KELAPA SAWIT Tabel L1.1 Hasil Analisis Karakteristik LCPKS dari PTPN III Rambutan
No. Parameter Satuan Hasil Uji Metode Uji
1. pH - 3,90-4,50 APHA 4500-H
2. Chemical Oxygen Demand (COD)
mg/L 40.288 APHA 5220B
3. Total Solid (TS) mg/L 14.000-28.000 APHA 2540B 4. Volatile Solid (VS) mg/L 10.000-26.000 APHA 2540E
5. Total Suspended Solid (TSS)
mg/L 21.040-25.160 APHA 2540D 6. Volatile Suspended
Solid (VSS)
mg/L 9.040-17.160 APHA 2540E 7. Soluble Chemical
Oxygen Demand (SCOD)
mg/L 19.424 APHA 5220B
Sumber : Lubis, 2018
L1.2 DATA HASIL PENELITIAN PROSES METANOGENESIS
Tabel L1.2 Data Hasil Analisis pH, Alkalinitas, TS dan VS pada Proses
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Tabel L1.3 Data Hasil Analisis TSS dan VSS pada Proses Metanogenesis
HRT Hari ke TSS 1 TSS 2 TSS 3 VSS 1 VSS 2 VSS 3
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L1.3 DATA HASIL ANALISIS BIOGAS PADA PENGARUH HRT
Tabel L1.5 Data Hasil Analisis Komposisi Biogas pada Pengaruh HRT HRT Hari ke
Biogas (%)
Metana Karbondioksia Hidrogen Sulfida
Tabel L1.6 Data Produksi Biogas pada Pengaruh HRT
HRT
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LAMPIRAN 2
CONTOH PERHITUNGAN
L2.1 PERHITUNGAN NILAI ALKALINITAS Dari Tabel L1.2 diperoleh:
Pada HRT 6
L2.2 PERHITUNGAN NILAI VOLATILE SOLID (VS) Dari Tabel L1.2diperoleh:
L2.3 PERHITUNGAN NILAI VOLATILE SUSPENDED SOLID (VSS) Dari Tabel L1.2 diperoleh:
Pada HRT 6 sampling 1 Volume Sampel = 5 ml A= 23,54 mg
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L2.4 PERHITUNGAN REDUKSI COD Dari Tabel L1.4 diperoleh:
Pada HRT 6
COD influent = 40.288 mg/L COD effluent = 24.761,9 mg/L
Degradasi COD (%) = 100%
L2.5 PERHITUNGAN PERSENTASE VS YANG TERDEGRADASI Dari Tabel L1.2 diperoleh:
Pada HRT 10 sampling 1
VS input = 26.000 mg/L
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L2.6 PERHITUNGAN PRODUKSI BIOGAS / VS HRT 6
Produksi Biogas = 0,441 L/hari VS input = 26.000 mg/L
VS Discharge = 19.693 mg/L
VS Terdegradasi = 26.000 – 16.133 = 9.867 mg/L Produksi Biogas/VS =
9.867 1,346
= 0,00004466 L/mgVS.hari
= 4,47 x 10-5 L/mgVS.hari
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LAMPIRAN 3 DOKUMENTASI
Gambar L3.1 Tangki Umpan
Gambar L3.2 RangkaianPeralatan
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Gambar L3.3 Gas Meter
Gambar L3.4 Gas Detector
Gambar L3.5 Peralatan Analisis pH
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Gambar L3.6 Peralatan Analisis M-Alkalinity
Gambar L3.7 Peralatan AnalisiS TS
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Gambar L3.8 Peralatan Analisis TSS
Gambar L3.9 Peralatan Analisis Chemical Oxygen Demand (COD)
Gambar L3.10 Timbangan Analitik
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Gambar L3.11 Desikator
Gambar L3.12 Oven
Gambar L3.13 Furnace
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LAMPIRAN 4
FLOWCHART PENELITIAN
L4.1 FLOWCHART PROSEDUR LOADING UP DAN OPERASI TARGET
Gambar L4.1 Flowchart Prosedur Percobaan Mulai
Ya
Dilakukan analisa terhadap pH, M-Alkalinity, TS, VS, TSS, VSS dan volume biogas pada setiap titik sampling yang telah ditentukan setiap hari
Setelah kondisi stabil campuran starter dan LCPKS dimasukkan kedalam reaktor dengan variasi HRT
Apakah masih ada variasi HRT ?
Dilakukankan adaptasi hidrolitik tanpa perlakuan penambahan LCPKS segar sampai pH dan alkalinitas stabil, pada suhu ambient (30 oC) danpH dijaga konstan pH 7 0,2 sampai
kondisi stabil
Dilakukan analisa COD dan komposisi biogas pada setiap titik sampling yang berbeda-beda sertiap 3 hari
Tidak
Dimasukkan starter dan LCPKS segar kedalam dalam tangki pengumpanan dengan perbandingan 20% starter dan 80% LCPKS segar
Selesai
Campuran starter dan LCPKS diaduk sampai homogen
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L4.2 FLOWCHART PROSEDUR ANALISIS DATA L4.2.1 Flowchart Prosedur Analisis M-Alkalinity
Mulai
Dimasukkan 5 ml sampel ke dalam beaker glass
Selesai
Dicatat volume HCl yang terpakai
Ditambahkan aquadest hingga volume larutan menjadi 80 ml
Diaduk campuran hingga homogen dengan magnetic stirrer
Dimasukkan pH elektroda ke dalam beaker glass
Apakah bacaan pH mencapai 4,8±0,02?
Dititrasi campuran dengan HCl 0,1 N
Tidak
Ya
Gambar L4.2 Flowchart Prosedur Analisis M-Alkalinity
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L4.2.2 Flowchart Prosedur Analisis Total Solids (TS) Mulai
Dipanaskan cawan penguap selama 2 jam pada suhu 105 oC
Diambil sampel dan masukkan ke dalam cawan
Selesai
Didinginkan cawan penguap selama 15 menit di dalam desikator
Ditimbang berat cawan
Didinginkan cawan penguap selama 15 menit di dalam desikator
Dimasukkan cawan berisi sampel ke oven pada suhu 103-105oC selama 1 jam
Didinginkan cawan penguap selama 15 menit di dalam desikator
Ditimbang berat cawan
Apakah berat cawan sudah konstan?
Tidak
Ya
Gambar L4.3 Flowchart Prosedur Analisis Total Solids (TS)
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L4.2.3 Flowchart Prosedur Analisis Volatile Solids (VS) Mulai
Dimasukkan cawan hasil analisis TS ke dalam furnace
Selesai
Dipanaskan pada suhu 550 oC selama 1 jam
Didinginkan cawan penguap di dalam desikator hingga suhunya mencapai suhu kamar
Ditimbang berat cawan
Gambar L4.4 Flowchart Prosedur Analisis Volatile Solids (VS)
L4.2.4 Flowchart Prosedur Analisis Total Suspended Solids (TSS) Mulai
Ditimbang kertas saring kering yang digunakan
Dibasahi kertas saring dengan sedikit air suling
Diaduk sampel dengan magnetic stirrer hingga homogen
Dipipetkan sampel ke penyaringan
Dicuci kertas saring atau saringan dengan 3 x 10 mL aquadest
A
63 Selesai
Dimasukkan sampel ke dalam oven pada suhu 103-105oC selama 1 jam
Didinginkan cawan penguap selama 15 menit di dalam desikator
Ditimbang berat cawan
Apakah berat cawan sudah konstan?
Tidak
Ya A
Dipindahkan kertas saring secara hati-hati ke wadah timbang aluminium
Gambar L4.5 Flowchart Prosedur Analisis Total Suspended Solids (TSS)
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L4.2.5 Flowchart Prosedur Analisis Volatile Suspended Solids (VSS) Mulai
Dimasukkan cawan hasil analisis TSS ke dalam furnace
Selesai
Dipanaskan pada suhu 550 oC selama 1 jam
Didinginkan cawan penguap di dalam desikator hingga suhunya mencapai suhu kamar
Dtimbang berat cawan
Gambar L4.6 Flowchart Prosedur AnalisisVolatile Suspended Solids (VSS)