The Role of Chemical Engineering In Reducing The ...

PROCEEDINGS

INTERNATIONAL SEMINAR ON FUNDAMENTAL & APPLICATION OF CHEMICAL ENGINEERING NOVEMBER 3 - 4, 2010 Inna Kuta Beach Hotel, Bali, INDONESIA

The Role of Chemical Engineering In Reducing The Effects of Global Warming

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Organized by : Department of Chemical Engineering Faculty of Industrial Technology Sepuluh Nopember Institute of Technology, Surabaya - Indonesia

The 1st International Seminar on Fundamental and Application of Chemical Engineering

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ISFAChE 2010 November 3-4, 2010, Bali-Indonesia

PROCEEDINGS International Seminar on Fundamental & Application of Chemical Engineering Department of Chemical Engineering Faculty of Industrial Technology Sepuluh Nopember Institute of Technology, Surabaya Indonesia Desain Sampul : Nila Permatasari © 2010, ITS PRESS, Surabaya Hak cipta dilindungi Undang-undang Diterbitkan pertama kali oleh Penerbit ITS PRESS, Surabaya 2010

Anggota IKAPI

Sanksi Pelanggaran Pasal 22 Undang-Undang Nomor 19 Tahun 2002 Tentang Hak Cipta: 1. Barangsiapa dengan sengaja dan tanpa hak melakukan perbuatan sebagaimana dimaksud dalam Pasal 2 ayat (1) atau Pasal 49 ayat (1) dan ayat (2) dipidana dengan pidana penjara masing-masing paling singkat 1 (satu) bulan dan/ atau denda paling sedikit Rp1.000.000,00 (satu juta rupiah), atau pidana penjara paling lama 7 (tujuh) tahun dan/ atau denda paling banyak Rp5.000.000.000,00 (lima milyar rupiah). 2. Barangsiapa dengan sengaja menyiarkan, memamerkan, mengedarkan atau menjual kepada umum suatu ciptaan atau barang hasil pelanggaran Hak Cipta atau Hak Terkait sebagaiman dimaksud pada ayat (1) dipidana dengan penjara paling lama 5 (lima) tahun dan/ atau denda paling banyak Rp500.000.000,00 (lima ratus juta rupiah).

Dilarang keras menerjemahkan, memfotokopi, atau memperbanyak sebagian atau seluruh isi buku ini tanpa izin tertulis dari penerbit. Dicetak oleh Percetakan ITS Press Isi di luar tanggung jawab percetakan



The 1st International Seminar on Fundamental & Application of Chemical Engineering

EDITORIAL BOARD Prof. Achmad Roesyadi (ITS - Indonesia) Prof. Nonot Soewarno (ITS - Indonesia) Prof. Ali Altway (ITS - Indonesia) Prof. Mahfud (ITS - Indonesia) Prof. Sugeng Winardi (ITS - Indonesia) Prof. Tri Widjaja (ITS - Indonesia) Prof. Renanto Handogo (ITS - Indonesia) Dr. Tontowi Ismail (ITS - Indonesia) Ir. Minta Yuwana MS (ITS - Indonesia) Prof. Herri Susanto (ITB - Indonesia) Prof. M. Nasikin (UI - Indonesia) Prof. Wahyudi Sediawan (UGM - Indonesia) Prof. Huang Hsiao Ping (NTU-Taiwan) Prof. Yi-Hsu Ju (NTUST-Taiwan) Prof. J.C. Liu (NTUST-Taiwan) Prof. Bing Hung Chen (NCKU-Taiwan) Prof. Kikuo Okuyama (Hiroshima Univ – Japan) Prof. Ashar Ahmad (UTM-Malaysia) Prof. GP. Rangaiah (NUS-Singapore) Prof. Moses Tade (Curtin Univ- Australia) Prof. Jan Degreve (KUL-Belgium) Prof. Hiroyasu Ogino (Osaka Prefecture Univ – Japan) Dr. Sunit Hendranata (LIPI Bandung - Indonesia) Dr. Agus Haryono (LIPI Serpong - Indonesia)




PREFACE Chemical Engineering Department of Sepuluh Nopember Institute of Technology (ITS) jointly collaborated with APTEKINDO, BKK-PII and Indonesian Polymer Association for the first time organizing International Seminar on Fundamental & Application of Chemical Engineering, ISFAChE 2010. The committee received 165 abstracts and accepted around 120 papers and forty papers of them came from Japan, Taiwan, Korea, Malaysia, Thailand, and Australia. All the papers have been reviewed with the help of experts in the areas. The topics are classified into Biochemical Engineering, Clean Energy System & Environment, Conventional & Renewable Energy, Analytical Chemistry, Nano Material & Nano Technology, Catalyst & Chemical Reaction Engineering, Process System Engineering, Thermodynamics, Transport Phenomena, and Polymer Technology & Material Process We wish to thank reviewers, plenary speakers, keynote speakers, and session moderators for their cooperation and valuable suggestions. We would like to extend our appreciation to members of organizing committees of all events during two days of conference.

Editorial Board International Seminar on Fundamental & Application of Chemical Engineering, ISFAChE 2010



CONTENTS Editorial Board Preface Contents Plenary Lectures PL01

Nanomaterials Processing Technology and Its Future Trend Kikuo Okuyama, I Made Joni, Widiyastuti and Agus Purwanto

PL02

On Relationship Between the Rate of Erosion Wear of a Axial High – Speed Impellers and Their Process Characteristics Ivan Fořt and Tomáš Jirout

PL03

Chemical and Biochemical Engineering for Mitigation of Greenhouse Gases Yi-Shan Huang, Chih-Hung Hsieh, Chun-Chong Fu and Wen-TengWu

Invited Speakers IS01

Development Of Organic Solvent-Tolerant Enzymes Hiroyasu Ogino

IS02

CFD Prediction Of Macro-Instabilities Of The Flows In A Stirred Tank Jahoda M., Mostek M., Fort I., Antecky T. and Hasal. P

IS03

Halloysite Nanotubes (Hnts) As A New Filler In Ethylene Propylene Diene Monomer (EPDM)/HNT Nanocomposites H. Ismail, P. Pasbakhsh, A.F.Mohd Nor and A.Abu Bakar

IS04

New Functional Polymers For The Potential Application On Optical And Elctrochromic Materials Der-Jang Liaw, Kueir-Rarn Lee, Juin-Yih Lai

IS05

Saving Energy Technology and its Application to Chemical Plant for reducing Carbon Dioxide (CO2) S. Yamamoto

Biochemical Engineering A001

Kinetic Model Based On Michaelis – Menten Mechanism For Non Alcohol Route Of Biodiesel Synthesis Using Biocatalyst Heri Hermansyah , Rita Arbianti, Tania Surya Utami and Endrika Andini

A002

Enchancement Of Enzymatic Hydrolysis Of Oil Palm Empty Fruit Bunches By Decreasing Cellulose Cristallynity Index Silvi Octavia, Ilona Sárvári Horváth, Tatang H. Soerawidjaja, Ronny Purwadi and I.D.G. Arsa Putrawan

A003

Development Of Blood Reproductive Hormones Test Using FTIR to Monitor Phases In Mammals Reproductive Cycle: A Preliminary Study Luthfiralda Sjahfirdi and Franciscus D Suyatna and M.Nasikin



B015

Alternative Technologies for Domestic Wastewater Management and Their Contributions to Reduce Global Warming Maria Prihandrijanti

B016

Biodiesel Production from Palm Oil Using Cao/Γ Al2O3 as Solid Base Catalyst Nyoman Puspa Asri, Farisa Rizki, Aiyum Anisa, Achmad Rosyadi, Kusno Budikarjono, Suprapto and Ignatius Gunardi

B017

Laboratory Experiments on the Use Of Locally Available Natural Catalyst For Tar Cracking For Biomass Gasification Unit Marina Agustina, Subagjo and Herri Susanto

B018

Development of Ni/Al2O3 Catalyst for Steam Reforming of Tar in Biomass Gasification Process Deviana Pramitasari, Herri Susanto and Subagjo

B019

Liquid Phase Synthesis of Aromatic Compounds from Castor Oil using ZSM-5 Based Catalyst Mohammad Nasikin, Falah Fakhriyah, Ayu Dahliyanti and Nerissa Arviana

Conventional & Renewable Energy C001

Biodiesel from Crude Rubber Seed Oil (CRSO)-Hevea Brasiliensis Sp. via NonCatalytic Process Reaction I Wayan Susila, Orchidea Rachmaniah and M. Rachimoellah

C002

The Effect of Reactant Ratios, Reaction Time and Catalyst Weight Ratios on Production of Biodiesel from Coconut Palm Oil using Heterogeneous Catalyst M. Said, A. R. Fachry and T.I. Sari

C003

Hydrogen Production Systems Design through Plasma Non-Thermal Electrolysis Process Nelson Saksono, Jainal Abidin and Setidjo Bismo

C004

Biomass Waste and Biomass Pellets Characteristics and Their Potential in Indonesia Widodo Wahyu Purwanto, Dijan Supramono and Hanani Fisafarani

C005

Performance of Venturi Ejector for Absorption of Tar from Producer Gas Suhartono, Dwiwahju Sasongko, Azis Trianto and Herri Susanto

C006

Two Stage Continuous Transesterification Process for Biodiesel Production Sufriadi Burhanuddin, Chakrit Tongurai and Sukritthira Ratanawilai

C007

Analysis of Petroleum Fuel Substitution with Natural Gas and Its Financial and Environmental Effects to Indonesia A. Qoyum Tjandranegara, Arsegianto and Widodo Wahyu Purwanto

C008

Production of Biodiesel by Ultrasound Assisted Esterification of Rubberseed Oil Hadiyanto, Widayat and Tomy Berkah Fajar

C009

Biodiesel Production from Rice Bran by In-Situ Esterification: The Effect of Methanol Concentration and Reaction Time Setiyo Gunawan, Syahrizal Maulana, Khairiel Anwar, Raden Darmawan, Tri Widjaja and Achmad Roesyadi



PERFORMANCE OF VENTURI EJECTOR WITH WATER-OIL MIXTURE FOR ABSORPTION OF TAR FROM PRODUCER GAS Suhartono, Dwiwahju Sasongko, Azis Trianto and Herri Susanto Research Group on Energy and Chemical Processing System Department of Chemical Engineering, Institut Teknologi Bandung Jl. Ganesa No 10, Bandung, Indonesia (40132) e-mail : [email protected] and [email protected] Abstract The conventional methods of water scrubber still has absorption limitation for tar removal from the gaseous product obtained from a biomass gasification process. Experiments were carried out in the laboratory-scale using a venturi column and a spray column. This experimental study was also related with the selection of absorbing liquid. Toluene was used as a model compound of tar. These experiments showed that palm oil had a much larger absorption capacity than water. But by adding small amount of palm oil into water, the absorption capacity of water could be increased significantly (up to 0.73 g/L at 35 0C compared to 0.53 g/L for pure water at 25 0C). Our experiments also showed that the venturi column had a better absorption efficiency that the spray column in term of absorption efficiency. Keywords: toluene absorption, venturi column, spray column, Henry's constant, mass transfer rate

I. Introduction Producer gas obtained from gasification process contains particulate and tar organic contaminants. If not removed, these contaminants may cause operational problems in the use of ther producer gas. For application of the producer gas in an internal combustion engine, the particulates contents of in the gas must be below 50 mg/Nm3 and its tar contents must be less than 100 mg/Nm3 [Hasler dan Nussbaumer, 1999]. Tar composes of various aromatic nonpolar compounds. Typical tar composition and solubilties of tar compounds are presented in Table 1.

No. 1 2 3 4 5 6

Table 1. Solubilities of tar compounds in water at 25 oC [Mackay, et.al, 1979] Compounds Solubility (g/L) No. Compounds Solubility (g/L) Phenol 87 7 Etilbenzene 0,16 Cresol 23 8 Naphtalene 0,03 Quinoline soluble 9 Biphenyl 0,007 Piridine miscible 10 Anthracene insoluble Toluene 0,53 11 Flouranthene 0,000265 Xilene 0,17 12 Pyrene 0,000135

Several organic solvents are reported to be very effective for absorption of volatile organic compounds (VOC) from industrial waste gas stream. Unfortunately those organic solvents are relatively expensive for the use in gas producer cleaning system in a biomass gasification plant. Palm oils are presumably more suitable than water for tar absorption as palm oil has more or less a similar chemical structure with tar compounds. Furthermore palm oils have relatively higher boiling point than water, so they can be used in a high temperature gas stream. But palm oil has a relatively high viscosity that may hinder the absorption rate [Heymes, et al 2009]. A venturi column (venturi scrubber or venturi ejector) has some advantages compared to spray column. A venturi column is still simple in design/manufactured, and causes a relatively low gas pressure drop.

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The objectives of our study were evaluation of the performance of a venturi column, and evaluation of typical types of absorbing liquid: palm oil, water and a mixture of water and oil. These absorption experiments were conducted in a semi batch operation, ie.: (i) continous gas flow and (ii) bacth operation for absorbing liquid. The liquid phase was in fract circulated by a pump, between the absorption column and an accumulation tank.The performances of venturi and spray columns were evaluated by measuring absorption efficiency, absorption capacity and mass transfer coefficient. 2. Theoritical Background Toluene was used as model compounds for tars having a specific characteristic of small quantity to dissolve in water. This type of organic compounds is condensable but forming a two-phase liquid/liquid [Boerrigter, et.al, 2005]. For a semi batch absorption like our system, the toluene concentration in the gas phase can usualy be measured at two points, ie.: gas inlet and gas outlet of the column. While the toluene concentration in the liquid phase is calculated based on mass balance of toluene, using the following equation. QG CL t (1) CG, CG, t dt VL

In the above equation: QG is gas flowrate; VL is solvent volume; CG,i is toluene concentration in gas phase at the inlet of column; CG,o is that at the outlet; and CL(t) is toluene concentration in liquid phase. The toluene concentration in the liquid phase will change progressively with time and approaches a saturated concentration CL,s. Similarly, CG,o will also approach CG,i at this liquid saturation condition. Assuming an equilibrium condition, toluene concentration in gas phase at the interface CG# can be related with that in liquid phase using Henry's law. The value of Henry’s constant can be calculated as follows: C# G

H

(2)

CL

Further assumption is made for this equilibrium condition that the toluene concentration at the interface of gas phase is the same with that in the body of the gas phase. So at the equilibrium condition, the following relation may be applied: CG# = CG,o. When experiments do not yet approach the equilibrium condition, mass transfer rates both in the gas side interphase and in the liquid interphase may still play important roles. In this condition, Henry’s constant; the mass transfer coefficient in the gas interphase (KGa) and the mass transfer coefficient in the liquid phase (KLa) may be evaluated simultaneously from experimental data [Mackay, et.al, 1979]. For the case of gas mass transfer limitation: CL For the case of liquid phase limitation: CL

KG

QG

KG H G H

KL

CG, CG,

QG CG,

KG H QG KL

CG,

(3) (4)

Having experimental data on CL(t), CG,o(t) and CG,i; values of H, KGa and KLa can be evaluated from slope and intercept of the above equations. 3. Experimental Set Up Experiments were conducted in two types of laboratory scale absorber: spray column and venturi column (see Figure 1). Gas model was made by flowing air into a liquid toluene with the flowrate of 99 L/min. Gas model was then fed into the spray column (counter current against liquid) or the venturi column (co-current with liquid). The venturi column system consisted of: a 6500 mL tank; a liquid flow of about fasility of 5 L/min and a gas flow system of about 1 L/min. The spray column system consisted of: a circulating tank of 6200 mL; liquid pump with a capacity of about 0,15 L/min; and a gas feeding line with a capacity of about 0,1 – 0,4 L/min. The absorbing liquid was fed by a circulating pump through a nozzel (diameter of about 1 mm) in the top of the column. Palm oil and water were used as absorbing liquid, and their absorption C005-2



characteristic were evaluated based on its capacity and mass transfer rate. The use of mixed liquid was also trialed, ie. a mixture of water with 5%-vol of oil. Toluene concentration in the gas phase was measured using gas chromatography with a carbowax separation column and a flame ionization detector.

Spray column

Venturi column

Figure 1. Scheme of experimental set up 4. Result and Discussion Variables in our experiments are presented in Table 1 and Table 2 (code S for spray column dan code V for venturi column. Results of our experiment are presented in Table 3 and Table 4. Table 1. Variables in experiment of toluene-water system Spray column oC

Temperature , Expt. code QG, L/minute QL, L/minute CG,in avg, mol/m3 CG,out eq., mol/m3 Solvent volume

30 S1 0.314 0.148 0.828 0.560

S2 0.343 0.148 0.776 0.543

S3 0.314 0.116 0.719 0.548

40 S4 S5 0.343 0.314 0.116 0.148 0.770 0.767 0.564 0.630 6200 mL

S6 0.343 0.148 0.759 0.656

S7 0.314 0.116 0.748 0.610

30 S8 0.343 0.116 0.851 0.721

V1 0.944 5.909 1.207 1.051

Ventury column 35

V2 1.187 5.909 1.025 0.833

V3 V4 0.944 1.187 5.909 5.909 1.039 1.188 0.769 1.082 6500 mL

V5 0.944 5.909 1.036 0.906

40 V6 1.187 5.909 1.263 1.263

Values of Henry’s constant are presented in 1/H; the higher 1/H is the higher solubility or the higher absorption capacity. In accordance with the principle of thermodynamic, 1/H is almost constant independent of flowrate and they may be dependent of temperature. Values of Henry’s constant obtained in our experiments were about 11 (Table 3), which were almost the same as literature data of 12 [Vuong,2009]. Actually, the use of pure oil as solvent has much higher absorption capacity than water and water-oil mixture. But the use of pure oil required a higher pumping energy due to a higher viscocity of oil. On the other hand, adding small amount of oil into water, the absorption capacity of this mixture was already significantly higher than that of water, i.e. the absorption capacity of water+oil mixture was 0.73 g/L at 35 0C, compared to pure water of 0.53 g/L at 52 oC [Mackay, 1979]. Table 2. Experimental absorption variables of toluene-(water+oil) system C005-3


Solvent Temperature (oC) Experimental code QG, L/minute QL, L/minute CG,in avg, mol/m3 CG,out eq, mol/m3 Column diameter Column height Nozel diameter Height of contact of gas-solvent Volume of liquid accumulation Flow direction


Spray column Water + 5% oil Water + 5% oil 35 40 S8 S9 S10 S11 0,314 0,343 0,314 0,343 0,148 0,148 0,148 0,148 0,350 0,981 0,331 0,386 0,094 0,243 0,094 0,101 50 mm 1030 mm 1 mm 550 mm 6200 mL counter current

Ventury column Oil 100% Oil 100% 35 45 V7 V8 V9 V10 0,944 1,187 0,944 1,187 4,260 4,260 4,260 4,260 1,152 1,145 1,089 1,113 0,058 0,108 0,057 0,002 50 mm 1060 mm 1 mm 550 mm 5000 mL co-current

Table 3. Henry constant, absorption efficiency, and mass transfer coefficient of toluene-water system Spray column Venturi column Temperature, oC 30 40 30 35 40 Experimental code S1 S2 S3 S4 S5 S6 S7 S8 V1 V2 V3 V4 V5 V6 QG, L/minute 0.314 0.343 0.314 0.343 0.314 0.343 0.314 0.343 0.944 1.187 0.94 1.187 0.944 1.187 QL, L/minute 0.148 0.148 0.116 0.116 0.148 0.148 0.116 0.116 5.909 5.909 5.91 5.909 5.909 5.909 KGa, m3/minx10-4 5.149 1.872 2.509 2.457 2.768 3.467 4.752 2.744 6.816 72.907 85.72 10.309 6.377 7.261 KLa, m3/minx10-5 6.260 0.848 3.467 3.046 6.268 9.366 9.578 6.630 6.148 29.986 37.38 8.510 5.541 0.071 Eff. %, at 22 min 58.54 38.80 44.99 60.55 42.92 45.18 48.49 40.51 83.70 77.99 86.47 59.10 54.43 31.74 Eff. %, at 340 min 33.37 34.45 23.86 26.76 17.90 13.60 19.76 16.54 12.96 18.71 26.03 8.91 12.53 0.002 Henry's constant, 0.122 0.045 0.138 0.124 0.198 0.240 0.159 0.201 0.096 0.041 0.06 0.083 0.068 0.158 (mol.m-3)/(mol.m-3) 1/H 8.226 22.08 7.238 8.067 5.050 4.166 6.296 4.963 10.371 19.611 17.64 9.380 14.705 6.331 1/H average 11.404 5.119 14.991 13.510 10.518 Abs. cap, eq., g/L 0.566 0.483 0.384 0.384 0.373 0,282 0,241 0,341 0,945 1,956 1,995 1,251 0,939 0,769 Abs. cap, avg, g/L 0.454 0.309 1.451 1.623 0.854 Notes: Eff.= absorption efficiency; abs. cap = absorption capacity; avg. = average; eq. = equilibrium

Table 4. Henry constant, absorption efficiency, and mass transfer coefficient of toluene-(water+oil) system Spray column Solven Water + 5% oil Water + 5% oil Temperature , oC 35 40 Experimental code S9 S10 S11 S12 QG. L/minute 0.314 0.343 0.314 0.343 QL. L/minute 0.148 0.148 0.148 0.148 KGa. m3/min X 10-4 4.812 2.288 1.706 1.954 KLa. m3/min X 10-5 1.541 4.017 2.748 3.158 Eff. %, at 22 min 92.61 94.20 86.34 84.68 Eff. %, at 340 min 73.68 74.63 72.05 73.91 H [mol.m-3/ mol.m-3] 0.018 0.014 0.016 0.016 1/H 54.627 71.998 62.104 61.881 1/H average 63.313 61.993 Abs. capacity, g/L 0.506 0.950 0.416 0.476 Abs. capacity, g/L 0.728 0.446 Notes: Eff.= absorption efficiency

Venturi column Oil 100% 35

Oil 100% 45

V7 V8 0.944 1.187 4.260 4.260 36.246 24.259 2.477 2.871 98.33 96.22 95.05 90.65 0.001 0.001 1463.387 1155.809 1309.598 2.231 6.629 4.430

V9 V10 0.944 1.187 4.260 4.260 24.726 147.076 1.225 2.271 96.44 99.94 94.79 99.86 0.001 0.001 1705.783 775.885 1240.834 4.553 6.405 5.479

For toluene-(water + 5% oil) system, values of 1/H were in the range of 63 to 1309 (Table 4). These values were comparable with toluene-polyethylene glycol system (1/H of 1645, [Vuong, 2009]). The characteristic of absorption column are as absorption efficiency, ie. the ratio of absorbed toluene to amount of toluene entering the column. The effect of the type of absorbing liquid can be seen on

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Figure 2(a) vs Figure 2(b), and also Figure 3(a) vs Figure 3(b). Again, the mixture of water and oil showed a much better absorption efficiency.

(a) Toluene-water system

(b) Toluene-(water + oil) system

Figure 2. Efficiency of toluene absorption in spray column

(a) Toluene-water system

(b) Toluene-oil system

Figure 3. Efficiency of toluene absorption in venturi column As expected, the venturi column had a better performance than the spray column, as indicated by values of 1/H, and absorption efficiency. The venturi column had of course an excellent mixing characteristic as the gas-liquid contact was facilitated using a throat. The gas flow across the venturi column also had a lower pressure drop, since gas and liquid flowed co-currently. Characteristic of the two columns can be comparer each other through Figure 2(a) vs Figure 3(a); and Figure 2(b) vs Figure 3(b). The absorption efficiency of venturi column was about 70% higher than that of spray column. Absorption capacity of venturi column with water+oil mixture could also maintained for a much longer time upto to 360 minutes. While the absorption efficiency of spray column dropped already to 40% after an absorption operation of 150 minutes. Furthermore, the absorption efficiency of spray column was clearly affected by liquid flow rate significantly. 5. Conclusions Adding a small amount of oil into water could increase the absorption capacity toward toluene, while maintaining the flow characteristic of water. As expected, the venturi column showed much better performance than the spray column in term of the absorption rate. Having a better absorption characteristic, the design of a venturi column was actually not so complicated compared to a spray

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column. Thus a system comprises of a venturi column and a mixture of water qith a small amount of oil has a potential application for a gas cleaning system in a gasification unit. 6. Acknowledgements This experimental work is one of our research topic in the development of biomass gasification technology for rural application, funded by TANOTO FOUNDATION, FY. 2007-2010. The authors would like to thanks to Mr Andri Ferdinan for all experimental works. References 1. Boerrigter H., S. van Paasen, and P. Bergman, (2003), Status update of OLGA technology development: Pilot demonstration of tar removal: Complete test facility & new OLGA research topic, Energy Research Centre of the Netherlands (ECN). 2. Bourgois D., J. Vanderschurer, and D. Thomas, (2008), Determination of liquid diffusivities of VOC (paraffin and aromatic hydrocarbon) in phthalate, Chemical Enginering and Proccesing, 47, 1357-1364. 3. Hadjoudj R., M. Hubert, C. Roizand, and F. Lapicque, (2008), Measurement of diffusivity of clorinated VOCs in heavy absorption solvents using a laminar film contactor, Chemical Engineering and Processing, 47, 1478-1483. 4. Hasler P., and Th. Nussbaumer, (1999), Gas cleaning IC engine applications from fixed bed biomass gasification, Biomass and Bioenergy, Switzerland, 385-395. 5. Heymes F., P. Manno-Demoustier, F. Charbit, J.L Fanlo, and P. Moulin, (2006), A new efficient absorption liquid to treat exhaust air loaded with toluene, Chemical Engineering Journal, 115, 225231. 6. Mackay D., W.Y. Shiu, and R.P. Sutherland, (1979), Determination of air-water Henry’s law constants for hydrophobic pollutant, Environmental Science and Technology, 13, 333-337. 7. Vuong, M.D., A. Couvert, C. Couriol, A. Amrane, P. Le Cloirec, and C. Renner, (2009), Determination of the Henry’s constant and the mass transfer rate of VOCs in solvent, Chemical Engineering Journal. xxx. xxx-xxx.

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