ORIGINAL_ARTICLE
Synthesis and Study of Gd3+ and Lu3+ Doped CdO via Sol-Gel Method
In this study pure CdO and Gd 3+, Lu3+ doped CdO oxides were synthesized successfully via a sol-gel method at 900°C. The SEM images indicate that with doping and changing the amounts of Gd 3+ or Lu3+ the morphologies of the obtained materials changed and indicated that the CdO composed of nanoparticles structures with grain size of about 150-300 nm. The structural properties of the CdO were investigated by powder X-Ray Diffraction (XRD) technique. The XRD patterns show that with doping the Gd 3+ or Lu3+ ions in CdO, the obtained phase is isostructural with the pure CdO materials. Also, cadmium oxide particles cell parameters determined using celeref software version 3. Optical properties of synthesized doped samples were investigated using ultra violet absorption spectra.
https://www.nsmsi.ir/article_9237_3a1d4e19a948aefa58d16b4659ceea20.pdf
2014-04-01
1
8
Cubic structure
Sol-gel process
Gadolinium oxide
Lutetium oxide
Gab band
Sajjad
Ahmadpour
sajjadahmadpour@yahoo.com
1
Chemistry Department, Tabriz University, Tabriz, I.R. IRAN
LEAD_AUTHOR
Abdolali
Alemi
2
Chemistry Department, Tabriz University, Tabriz, I.R. IRAN
AUTHOR
Shahin
Khademinia
3
Chemistry Department, Tabriz University, Tabriz, I.R. IRAN
AUTHOR
[1] نعمتی، زیارتعلی؛ ارتباط ریزساختارها و خواص الکتریکی در سرامیکهای باریم تیتانات، نشریه شیمی و مهندسی شیمی ایران، (1) 26، ص. 21 (1386).
1
[2] Fahrettin Y., Mujdat C., Yasemin C., Saliha I., Electrical Characterization of Nanocluster n-CdO/p-Si Heterojunction Diode, Journal of Alloys and Compounds, 506 (1), p.188 (2010).
2
[3] Moholkar A.V., Agawane G.L., Kyu-Ung Sim., Ye-bin Kwon., Doo Sun Choi., Rajpure K.Y., Kim J.H., Temperature Dependent Structural, Luminescent and XPS Studies of CdO:Ga Thin Films Deposited by Spray Pyrolysis, Journal of Alloys and Compounds, 506 (2), p. 794 (2010).
3
[4] Aksoy S., Caglar Y., Ilican Saliha., Caglar M., Effect of Heat Treatment on Physical Properties of CdO Films Deposited by Sol-Gel Method, International Journal of Hydrogen Energy, 34(12), p. 5191 (2008).
4
[5] توحیدی، سیدحسین؛ نوین روز، عبدالجواد؛ سنتز ترکیبهای مس (II) اکسید، روی بستر سیلیکا با ابعاد نانومتری به روش سل ـ ژل وبررسی طیف سنجی آن، نشریه شیمی و مهندسی شیمی ایران، (3)26، ص. 105 (1386).
5
[6] آزاد منجیری، جلال؛ سید ابراهیمی، سیدعلی؛ سنتز پودر فریت نیکل با ابعاد نانومتر به روش سل ـ ژل خود احتراقی، نشریه شیمی ومهندسی شیمی ایران، (1)24، ص. 83 (1384).
6
[7] Ristić M., Popović M., Musić S., Formation and Properties of Cd(OH)2 and CdO Particles, Materials Letters, 58(20), p. 2494 (2004).
7
[8] Fan D.H., Catalyst-Free Growth and Crystal Structures of CdO Nanowires and Nanotubes, Journal of Crystal Growth, 311(8), p. 2300 (2009).
8
[9] Dakhel A.A., Correlated Transport and Optical Phenomena in Ga-Doped CdO Films, Solar Energy, 82(6), p. 513 (2008).
9
[10] Zhang L., Wang W., Yang J., Chen Z., Sonochemical Synthesis of Nanocrystallite Bi2O3 as a Visible-Light-Driven Photocatalyst, Applied Catalysis, 308(10), p. 105 (2006).
10
[11] Fruth V., Ianculescu A., Berger D., Preda S., Synthesis, Structure and Properties of Doped Bi2O3, Journal of the European Ceramic Society, 26(14), p. 3011 (2006).
11
[12] Jayasimhadri M., Ratnam B.V., Jang Kiwan., Conversion of Green Emission into White Light in Gd2O3 Nanophosphors, Thin Solid Films, 518(22), p. 6210 (2010).
12
[13] Ristić M., Popović S., Musić S., Formation and Properties of Cd(OH)2 and CdO Particles, Materials Letters, 58(20), p. 2494 (2004).
13
[14] Ashoka S., Chithaiah P., Chandrappa G.T., Studies on the Synthesis of CdCO3 Nanowires and Porous CdO Powder, Materials Letters, 64(2), p. 173 (2010).
14
[15] Balamurugan S., Xu M., Takayama-Muromachi E., Magnetic and Transport Properties of High-Pressure Synthesized Perovskite Cobalt Oxide (Sr1–xCax)CoO3 (0⩽x⩽0.8), Journal of Solid State Chemistry, 178(11), p. 3431 (2005).
15
[16] احمدپور، سجاد؛ عالمی، عبدالعلی؛ خادمینیا، شاهین؛ مطالعه ساختاری و سیستماتیک نانو ذرات لیتیم متا سیلیکات (Li2SiO3) سنتز شده به روش گرمابی، مجله بلورشناسی و کانی شناسی ایران، (2)21، ص. 243 (1392).
16
ORIGINAL_ARTICLE
Modeling of Aroma Compound Recovery from Waste Streams by Membrane Contactors
Generated odorous contained effluents in food industries and interests in their recovery using non-destructive treatment method resulted in carrying out many research activities. The aim of this study is to develop an appropriate model to simulate the process of odorous substances recovery from different sources by membrane contactors using COMSOL and MATLAB softwares. The model was employed to evaluate effect of the important process variables such as the feed and solvent flow rates and concentrations on the rate of mass transfer and design a perfect process and also the effect of process parameters. Membrane contactor provides the required surface area for the two fluids contacts where aroma compounds are transferred from one phase to another phase through membrane pores by diffusion and convection mechanisms. The feed flow rate has a significant impact on the rate of aroma compounds mass transfer. The feed concentration increment has the same effect as increasing feed flow rate. Due to the low mass transfer rate from the feed side of the membrane contactor (e.g. transferred mass is governed by the feed side), effect of the solvent flow rate in this process was not detected. The simulated results has a good agreement with experimentally measured data (increment in the feed and solvent flow rates increases the simulated results error. The average error of the simulated results was calculated as 17 %).
https://www.nsmsi.ir/article_9238_6e102ee425a9f144bf29c42c1f952893.pdf
2014-04-01
9
19
Recovery
Aroma compounds
Simulation
Membrane contactor
Hollow Fiber
Membrane extraction
Sepideh
Soroush
1
Research Lab for Membrane Separation Processes, Department of Chemical Engineering, Iran University of Science and Technology, Tehran, I.R. IRAN
AUTHOR
Omid
Bakhtiari
obakhtiari@razi.ac.ir
2
Membrane Research Center, Department of Chemical Engineering, Razi University, Kermanshah, I.R. IRAN
LEAD_AUTHOR
Toraj
Mohammadi
torajmohammadi@iust.ac.ir
3
Research Lab for Membrane Separation Processes, Department of Chemical Engineering, Iran University of Science and Technology, Tehran, I.R. IRAN
AUTHOR
[1] Karlsson H.O.E., Tragardh G., Pervaporation of a Model Apple Juice Aroma Solution: Comparison of Membrane Performance, Membr. Sci., 119,p. 229 (1996).
1
[2] Lipnizki F., G. Tragardh J.O., Scale-up of Pervaporation for the Recovery of Natural Aroma Compounds in the Food Industry. Part 1: Simulation and Performance, Journal of Food Engineering, 54, p. 183 (2002).
2
[3] Lipnizki F., G. Tragardh J.O., Scale-up of Pervaporation for the Recovery of Natural Aroma Compounds in the Food Industry Part 2: Optimisation and Integration, Journal of Food Engineering, 54, p. 197 (2002).
3
[4] Schafer et al., Recovery of Aroma Compounds from a Wine-Must Fermentation by Organophilic Pervaporation, Biotech. and Bioeng, 62, p. 412 (1999).
4
[5] Karlsson H.O.E., Tragardh G., Aroma Recovery During Beverage Processing, Food Eng, 34, p. 159 (1997).
5
[6] Yeon S.H. et al., Application of Pilot-Scale Membrane Contactor Hybrid System for Removal of Carbon Dioxide from Flue Gas, Membr. Sci., 257, p. 156 (2005).
6
[7] Cussler E.L., “Membrane Process in Separation and Purification: Hollow Fiber Contactor”, Kluwer Academic Publishers, Netherlands, (1994).
7
[8] Kiani A., Bhave R.R., Sirkar K.K., Solvent Extraction with Immobilized Interface in a Microporous Hydrophobic Membrane, Membr. Sci., 20, p. 125 (1984).
8
[9] Seibert A.F. et al., Hydroulic and Mass Transfer Efficiency of a Commercial-Scale Membrane Extractor, Sep. Sci. Technol, 28, p. 343 (1993).
9
[10] Qi Z., Culsser E.L., Microporous Hollow Fibers for Gas Absorbtion. II. Mass Transfer Across the Membrane, Membr. Sci., 23, p. 333 (1985).
10
[11] Drioli E., Criscuoli A., Curcio E., Membrane Contactor: Fundamentals, Application and Potentialities, Membr. Sci., 11 (2006).
11
[12] Gabelman A., Hwang S.-T., Hollow Fiber Membrane Contactors, Journal of Membrane Science, Journal of Membrane Science, 159, p. 61 (1999).
12
[13] Diban N. et al., Vacuum Membrane Distillation of the Main Pear Aroma Compound: Experimental Study and Mass Transfer Modeling, Journal of Membrane Science, 326, p. 64 (2009)..
13
[14] Baudot A., Floury J., Smorenburg H.E., Smorenburg H.E., Liquid-Liquid Extraction of Aroma Compounds with Hollow Fiber Contactor, AIChE Journal, 47, p.1780 (2001).
14
[15] Bocquet S. et al., Membrane-Based Solvent Extraction of Aroma Compounds: Choice of Configurations of Hollow Fiber Modules Based on Experiments and Simulation, Journal of Membrane Science, 281, p. 358 (2006).
15
[16] Rezakazemi M., Shirazian S., Ashrafizadeh S.N., Simulation of Ammonia Removal from Industrial Wastewater Streams by Means of a Hollow-Fiber Membrane Contactor, Desalination, 285, p. 383 (2012).
16
[17] Pierre F.X., Souchon I., Marin M., Recovery of Sulfur Aroma Compounds Using Membrane-Based Solvent Extraction, Journal of Membrane Science, 187, p. 239 (2001).
17
[18] Bird R.B., Stewart W.E., Lightfoot E.N., "Transport Phenomena", John Wiley & Sons: New York (1960).
18
[19] Happel J., Viscous Flow relative to Arrays of Cylinders, AIChE Journal, 5, p. 174 (1959).
19
[20] Constantinou A. et al., CO2 Absorption in a High Efficiency Silicon_Nitride Mesh Contactor , Chemical Engineering Journal, 207–208, p. 766 (2012).
20
[21] Miramini S.A. et al., CFD Simulation of Acetone Separation from an Aqueous Solution Usingsupercritical Fluid in a Hollow-Fiber Membrane Contactor, Chemical Engineeringand Processing, 72, p. 130 (2013).
21
[22] Jiraratananon R., Uttapap D., Sampranpiboon P., Crossflow Microfiltration of a Colloidal Suspension with the Presence of Macromolecules, Membrane Science, 140, p. 57 (1998).
22
[23] Aimar P., A.Howell J., Concentration Polarisation Build up in Hollow Fibers : A Method of Measurment and Its modeling in Ultrafiltration, Membrane Science, 59, p. 81 (1991).
23
ORIGINAL_ARTICLE
Preparation of an Experimental Setup for Separation of Hydrogen Sulfide and Carbon Dioxide from Methane by Using Membrane Contactor
In this work, an experimental setup was designed and prepared in order to study the effects of various parameters on membrane contactor efficiency in separation of H2S and CO2 from natural gas. Polyethersulfone (PES) membrane was prepared and applied in this study for separation of H2S and CO2 form CH4. The methyldiethanolamine (MDEA) aqueous solution was used as the liquid phase absorber. The prepared membrane structure was investigated by using Scanning Electron Microscopy (SEM), and it showed that the membrane has porous structure. The results obtained from membrane contactor setup indicated that in constant liquid flow rate the separation efficiency increased by increasing of gas flow rate, and in constant gas flow rate the liquid flow rate enhanced the separation factor. Also, results revealed that the operation temperature enhancement led to better separation of H2S and CO2 form CH4-H2S-CO2 mixture.
https://www.nsmsi.ir/article_9239_c43fe7c0ec1c374b861f0020fc19abfd.pdf
2014-04-01
21
30
Separation
Hydrogen Sulfide
Carbon dioxide
Membrane contactor
Polyethersulfone
Farzad
Ashoubi
1
Department of Chemical and Petroleum Engineering, Sharif University of Technology, Tehran, I.R. IRAN
AUTHOR
Seyyed Abbas
Mousavi
musavi@sharif.edu
2
Department of Chemical and Petroleum Engineering, Sharif University of Technology, Tehran, I.R. IRAN
LEAD_AUTHOR
Reza
Roostaazad
3
Department of Chemical and Petroleum Engineering, Sharif University of Technology, Tehran, I.R. IRAN
LEAD_AUTHOR
[1] Klaassen R., Feron P., Jansen A., Membrane Contactor Applications, Desalination, 224, p. 81 (2008).
1
[2] Mansourizadeh A., Ismail A.F., Hollow Fiber Gas–Liquid Membrane Contactors for Acid Gas Capture: A Review, Journal of Hazardous Materials, 171, p. 38 (2009).
2
[3] Li J.L., Chen B.H., Review of CO2 Absorption Using Chemical Solvents in Hollow Fiber Membrane Contactors, Separation and Purification Technology, 41, p. 109 (2005).
3
[4] Gabelman A., Hwang S.T., Hollow Fiber Membrane Contactors, Journal of Membrane Science, 159, p. 61 (1999).
4
[5] مرتضی افخمیپور، رضا آذین، شهریار عصفوری، مدلسازی جذب انتخابی گاز هیدروژن سولفید توسط محلول متیل دی اتانول آمین در برج جذب پرشده، نشریه شیمی و مهندسی شیمی ایران، دوره 31، شماره2، ص. 27، (1391).
5
[6] گلمحمد مجرد، اسماعیل فاتحیفر، سعید ساعدی، حذف زیستی هیدروژن سولفید در راکتور ایرلیفت بیوفیلمی سوسپانسیونی،نشریه شیمی و مهندسی شیمی ایران، دوره 30، شماره2، ص. 1، (1390).
6
[7] Rajabzadeh S., Yoshimoto S., Teramoto M., Al-Marzouqi M., Matsuyama H., CO2 Absorption by Using PVDF Hollow Fiber Membrane Contactors with Various Membrane Structures, Separation and Purification Technology, 69, p. 210 (2009).
7
[8] Atchariyawut S., Jiraratananon R., Wang R., Separation of CO2 from CH4 by Using Gas–Liquid Membrane Contacting Process,Journal of Membrane Science, 304, p. 163 (2007).
8
[9] Dindore V.Y., Brilman D.W.F., Geuzebroek F.H., Versteeg G.F., Membrane–Solvent Selection for CO2 Removal Using Membrane Gas–Liquid Contactors, Separation and Purification Technology, 40, p. 133 (2004).
9
[10] Hughes M. N., Centelles M. N., Moore K. P., Making and Working with Hydrogen Sulfide, The Chemistry and Generation of Hydrogen Sulfide in Vitro and Its Measurement in Vivo: A Review, Free Radical Biology & Medicine, 47, p. 1346 (2009).
10
[11] American Gas Association, "Gas Engineers Handbook: Fuel Gas Engineering Practices", Industrial Press, New York, NY, First Edition (1965).
11
[12] فرزاد آشوبی، "ساخت یک تماسدهنده غشایی برای جداسازی H2S، CO2 و CH4، "، پایاننامه کارشناسی ارشد، دانشگاه صنعتی شریف، 1389.
12
[13] سید عباس موسوی، "بررسی ساخت غشاهای پلیمری به منظور جداسازی گازها"، پایاننامه کارشناسی ارشد، دانشگاه صنعتی شریف، 1380.
13
[14] Kierzkowska-Pawlak H., Chacuk A., Kinetics of Carbon Dioxide Absorption into Aqueous MDEA Solutions, Ecological Chemistry and Engineering S, 17, p. 463 (2010).
14
ORIGINAL_ARTICLE
Diffusivity Measurement of DMAZ in Air and Determining Minimum Storage Radius
Due to physico-chemical and performance properties of dimethyl amino ethyl azide (DMAZ), it is a good replacement liquid fuel for hydrazine group in space industries. After production of the fuel, it’s storage is a main parameter. It is necessary to determine the storage radius of the fuel for operators’ safety in storing zoon because of probable leakage. Calculating the storage radius of the fuel needs to diffusivity data of DMAZ in air. In this article, first of all, storage radius will be derived in general case according to the basic equation of mass transfer equation. Then, diffusivity of the fuel in air will be measured on the basis of Stefan tube method at atmospheric pressure. Storage radius of the fuel will be determined at different temperatures. At atmospheric pressure, results showed that the storage radius is 2.9 m, 3.2m, 3.7m and 4.2m with respect to temperatures of 15.95oC, 25.05oC, 39.45oC and 60.05oC.
https://www.nsmsi.ir/article_9240_09010440f94c9868a511cf444d18a708.pdf
2014-04-01
31
35
DMAZ
Storage
Storage radius
Diffusivity
Stefan-Maxwell method
Shahram
Ghanbari Pakdehi
sh_ghanbari73@yahoo.com
1
Faculty of Chemistry & Chemical Engineering, Malek Ashtar University of Technology, Tehran, I.R. IRAN
LEAD_AUTHOR
Azadeh
Pour Mazaheri
2
Faculty of Chemistry & Chemical Engineering, Malek Ashtar University of Technology, Tehran, I.R. IRAN
AUTHOR
Jafar
Towfighi Darian
3
Faculty of Chemical Engineering, Tarbiat Modares University, Tehran, I.R. IRAN
AUTHOR
Ali
Farrokhi
4
Faculty of Engineering, Tehran South Brach, Islamic Azad University, Tehran, I.R. IRAN
AUTHOR
[1] Edwards T., Liquid Fuels and Propellants for Aerospace Propulsion, Journal of Propulsion and Power, 19, p. 1903 (2003).
1
[2] Schmidt E.W., “Hydrazine and Its Derivatives”, John Wiley & Sons, New York (2001).
2
[3] Meyers C.J., Kosowski B.M., “Dimethylamino Ethylazide–A Replacement of Hydrazine Derivatives in Hypergolic Fuel Applications”, International Annual Conference of ICT, Fraunhofer, Germany, pp. 1-4 (2003).
3
[4] Thompson D., “Tertiary Amine Azides in Hypergolic Liquid or Gel Fuels Propellant System”, US Patent 6,013,143, (2000).
4
[5] Niknam M., Pakdehi S.G., Zarei A., Investigation of Effective Parameters on Liquid Propellant Storage, 1st International Conference On Propellants, Explosives And Pyrotechnics, Tehran, Iran, (2011).
5
[6] Wayne B. Geyer “Handbook of Storage Tank Systems - Codes, Regulations And Designs."; Marcel Dekker Inc., New York, (2000).
6
[7] Taylor R., Krishna R., “Multi-Component Mass Transfer.”, John Wiley & Sons, Inc., 2nd Ed (1993).
7
[8] روهنده، ح.، "پارامترهای مؤثر بر خالصسازی سوخت مایع DMAZ با روش منتخب در مقیاس بنچ و طراحی فرآیند در مقیاس پایلوت"، پایان نامه کارشناسی ارشد، دانشگاه صنعتی مالک اشتر، بهار (1390).
8
[9] Slattery J.C., Mhetar V.R., Unsteady-State Evaporation and the Measurement of a Binary Diffusion Coefficient, Chem. Eng. Sci., 52, p. 1511 (1997).
9
[10] Timothy S. Kokan, John R. Olds, Jerry M. Seitzman, Peter J. Ludovice, Characterizing High-Energy-Density Propellants For Space Propulsion Applications, Acta Astronautica, 65, p. 967 (2009).
10
[11] Bruce E. Poling, John M. Prausnitz, John P. O’Connell "The Properties of Gases and Liquids", Mcgraw-Hill Press, 5th Ed., Chapter1 ((2004))1.
11
ORIGINAL_ARTICLE
The Effect of Ce and Zr Loading over HZSM-5 to Produce Light Olefins from Naphtha
The effect of Ce and Zr loading over HZSM-5 to increase light olefin yields has been investigated in this research. Catalysts with 2 and 8% wt loading were synthesized by impregnation method. The physicochemical features of catalysts were characterized by mean of Scanning Electron Microscope (SEM), X-Ray Diffraction (XRD), Brunauer-Emmett-Teller (BET) and Temperature-Programmed Desorption (NH3-TPD). Performance of samples for naphtha thermal catalytic cracking at 650°C and 700°C, steam ratio 0.5 g/g and WHSV 60h-1 was reported. The maximum yield of light olefins achieved at 650˚C over 2%Zr/HZSM-5 due to moderate acidity.
https://www.nsmsi.ir/article_9286_05c496eca58242145573242722b4d14f.pdf
2014-04-01
37
47
Thermal catalytic cracking
Light olefins
HZSM-5
Cerium
zirconium
Forough
Momayez
1
Departman of Chemical Engineering, Tarbiat Modares University, Tehran, I.R. IRAN
AUTHOR
Jafar
Towfighi Darian
towfighi@modares.ac.ir
2
Departman of Chemical Engineering, Tarbiat Modares University, Tehran, I.R. IRAN
LEAD_AUTHOR
Ali
Mohammadalizadeh
3
Gas Research Division, Research Institute of Petroleum Industry (RIPI), Tehran, I.R. IRAN
AUTHOR
[1] Yan H.T., Le Van MaoR., Hybrid Catalysts Used in the Catalytic Steam Cracking Process (CSC): Influence of the Pore Characteristics and the Surface Acidity Properties of the ZSM-5 Zeolite-Based Component on the Overall Catalytic Performance, Applied Catalysis A: General, 375, p. 63 (2010).
1
[2] Al-Yassir, N., Le Van Mao R., Physico-Chemical Properties of Mixed Molybdenum and Cerium Oxides Supported on Silica-Alumina and Their use as Catalysts in the Thermal-Catalytic Cracking (TCC) of n-Hexane, Applied Catalysis A: General. 305, p.130 (2006).
2
[3] Li X., Shen B., Guo Q., & Gao, J., Effects of Large Pore Zeolite Additions in the Catalytic Pyrolysis Catalyst on the Light Olefins Production, Catalysis Today. 125, p. 270 (2007).
3
[4] Keyvanloo K., Towfighi J., Comparing the Catalytic Performances of Mixed Molybdenum with Cerium and Lanthanide Oxides Supported on HZSM-5 by Multi Objective Optimization of Catalyst Compositions Using Non Dominated Sorting Genetic Algorithm, Journal of Analytical and Applied Pyrolysis, 88, p. 140 (2010).
4
[5] TeimouriSendesi S.M., Towfighi J., Keyvanloo K., The effect of Fe, P and Si/Al Molar Ratio on Stability of HZSM-5 Catalyst in Naphtha Thermal-Catalytic Cracking to Light Olefins, Catalysis Communications.27, p.114 (2012).
5
[6] Gao X., Tang Z., Lu G., Cao G., LiD., Tan Z., Butene Catalytic Cracking to Ethylene and Propylene on Mesoporous ZSM-5 by Desilication, Solid State Sciences.12, p.1278 (2010)
6
[7] Nawaz Z., Qing S., Jixian G., Tang X., Wei F., Effect of Si/Al Ratio on Performance of Pt-Sn-Based Catalyst Supported on ZSM-5 Zeolite for n-Butane Conversion to Light Olefins, Journal of Industrial and Engineering Chemistry.16, p.57 (2010).
7
[8] Li X., Shen B., Xu C., Interaction of Titanium and Iron Oxide with ZSM-5 to Tune the Catalytic Cracking of Hydrocarbons, Applied Catalysis A: General, 375, p. 222 (2010).
8
[9] Wei Y., Liu Z., Wang G., Qi Y., Xu L., Xie P., He Y., Production of Light Olefins and Aromatic Hydrocarbons Tthrough Catalytic Cracking of Naphtha at Lowered Temperature, Studies in Surface Science and Catalysis, 158, p. 1223 (2005).
9
[10] Feng X., Jiang G., Zhao Z., Wang L., Li X., Duan A., Liu J., Xu C.,Gao J., Highly Effective F-Modified HZSM-5 Catalysts for the Cracking of Naphtha To Produce Light Olefins, Energy and Fuel. 24, p. 4111 (2010).
10
[11] Lu J., Zhao Z., XuC., Duan A., Zhang P., CrHZSM-5 Zeolites - Highly Efficient Catalysts for Catalytic Cracking of Isobutane to Produce Light Olefins, Catalysis Letters.109, p. 65 (2006).
11
[12] Li J., Qi Y., Xu L., Liu G., Meng S., Li B., Li M., Liu Z., Co-reaction of Ethene and Methanol Over Modified H-ZSM-5, Catalysis Communications. 9, p. 2515 (2008).
12
[13] Sugi Y., Kubota Y., Komura K., Sugiyama N., Hayashi M., Kim, J.H., Seo G., Shape-Selective Alkylation and Related Reactions of Mononuclear Aromatic Hydrocarbons Over H-ZSM-5 Zeolites Modified with Lanthanum and Cerium Oxides, Applied Catalysis A: General. 299, p.157 (2006).
13
[14] Setiabudi H.D., Triwahyono S., Jalil A.A., Kamarudin N.H.N., Aziz M.A.A., Effect of Iridium Loading on HZSM-5 for Isomerization of n-Heptane, Journal of Natural Gas Chemistry, 20, p. 477 (2011).
14
[15] Setiabudi H.D., JalilA A., Triwahyono S., Ir/Pt-HZSM5 for n-Pentane Isomerization: Effect of Iridium Loading on the Properties and Catalytic aActivity, Journal of Catalysis, 294, p.128 (2012).
15
[16] Jiang G., Zhang L., Zhao Z, Zhou X., Duan A., Xu C ., Gao J., Highly Effective P-Modified HZSM-5 Catalyst for the Cracking of C4 Alkanes to Produce Light Olefins, Applied Catalysis A: General.340, p. 176 (2008).
16
[17] Xiaoning W., Zhen Z., Chunming X., Aijun D., Li Z., Guiyuan J., Effects of Light Rare Earth on Acidity and Catalytic Performance of HZSM-5 Zeolite for Catalytic Cracking of Butane to Light Olefins, Journal of Rare Earths., 25, p. 321 (2007).
17
[18] Inaba M., Murata K., Takahara I., Inoue K., Production of C3+Olefins and Propylene from Ethanol by Zr-ModifiedH-ZSM-5 Zeolite Catalysts, Journal of Rare Earth., 2012, p.1 (2011).
18
[19] Song Z., Takahashi A., Mimura N., Fujitani T., Production of Propylene from Ethanol Over ZSM-5 Zeolites, Catalysis Letters., 131, p. 364 (2009).
19
[20] Yoshimura Y., Kijima N., Hayakawa T., Murata K., Suzuki K., Mizukami F. et al., Catalytic Cracking of Naphtha to Light Olefins, Catalysis Surveys from Japan, 4, p.157 (2001).
20
[21] HanS Y., Lee C.W., Kim J.R., Han N.S., Choi W.C., Shin C.H. et al., Selective Formation of Light Olefins by the Cracking of Heavy Naphtha Over Acid Catalysts, Studies in Surface Science and Catalysis., 135, p. 157 (2004)
21
[22] Liu W., Meng X., Zhao X., Wang G., Gao J., Xu C., Pyrolysis Performances of Catalytic Cracking Naphtha and Coker Naphtha on Inert Carriers and an Active Catalyst, Energy and Fuels., 23, p. 5760 (2009).
22
[23] Wei Y., LiuZ., Wang G., Qi Y., Xu L., Xie P. et al., Production of Light Olefins and Aromatic Hydrocarbons Through Catalytic Cracking of Naphtha at Lowered Temperature, Studies in Surface Science and Catalysis., 158, p. 1223 (2005).
23
ORIGINAL_ARTICLE
Prediction of Oxygen Solubility in Organic Solvents Using Artificial Neural Networks
In this paper, solubility of oxygen in organic solvents has been estimated using Artificial Neural Networks (ANN). Solubility data were studied for wide ranges of temperature (298.2-348.29 K) and pressure (0.0535 to 9.2338 MPa). Solvents are included of methanol, n-propanol, octane, toluene, dibutyl ether and 2-methyltetrahydrofuran. Network model consists of four inputs in input layer for acentric factor, molecular weight, TR and PR of the system and one neuron in output layer corresponding to solubility of oxygen. The best structure for feed-forward back propagation neural network is logarithmic sigmoid transfer function for hidden layer, 13 neurons in this layer and linear transfer function for output layer. Results show that optimum neural network architecture is able to predict the solubility of oxygen in organic solvents with an acceptable level of accuracy, R2 of 0.999997, ARD % of 0.8103 and AAD% of 0.0042. Sensitivity analysis shows that TR has the greatest effect on the solubility of oxygen.
https://www.nsmsi.ir/article_9287_de0afa12df9d5f64d1fbae83635c8520.pdf
2014-04-01
49
55
Oxygen solubility
Organic solvents
Neural network
Levenberg-marquardt
Transfer function
Ali
Tarjoman Nejad
ali_tarjoman@yahoo.com
1
Department of Chemical Engineering, Faculty of Chemistry, University of Tabriz, Tabriz, I.R. IRAN
LEAD_AUTHOR
Mahnaz
Yasemi
2
Eivan-e-Gharb Branch, Islamic Azad University, Eivan-e-Gharb, Ilam, I.R. IRAN
AUTHOR
[1] Guimaraes P.R.B., McGreavy, C., Flow of Information through an Artificial Neural Network, Comput. Chem. Eng., 19, p. 741 (1991).
1
[2] Sharma R., Singhal D., Ghosh R., Dwivedi A., Potential Applications of Artificial Neural Networks to Thermodynamics: Vapour-Liquid Equilibrium Predictions, Comput. Chem. Eng., 23, p. 385 (1999).
2
[3] Lashkarbolooki M., Shafipour Z., Zeinolabedini A., Farmani H., Use of Artificial Neural Networks for Prediction of Phase Equilibria in the Binary System Containing Carbon Dioxide, Journal of Supercritical Fluids, 75, p.144 (2013)
3
[4] Laugier S., Richon D., Use of Artificial Neural Networks for Calculating Derived Thermodynamic Quantitiesfrom Volumetric Property Data, Fluid Phase Equilib, 210, p. 247 (2003).
4
[5] Potukuchi W., Wexler A.S., Predicting Vapor Pressures Using Neural Networks, Atmos. Environ., 31, p. 741 (1997).
5
[6] Shyam S.S., Oon-Doo B., Michele M., Neural Networks for Predicting Thermal Conductivity of Bakery Products, J. Food Eng., 52, p. 299 (2002).
6
[7] BouchARD% C., A Neural Network Correlation for Variation of Viscosity of Sucrose Aqueous Solutions with Temperature and Concentration, Lebensm- Wiss.U. -Technol., 28, p.157 (1995).
7
[8] Eya H., Mishima K., Nagatani M., Iwai Y., Arai Y., Measurement and Correlation of Solubilities of Oxygen in Aqueous Solutions Containing Glucose, Sucrose and Maltose, Fluid Phase Equilibria, 97, p. 201 (1994).
8
[9] Millero F.J., Huang F., Laferiere A.L., Solubility of Oxygen in the Major Sea Salts as a Function of Concentration and Temperature, Marine Chemistry, 78, p. 217 (2002).
9
[10] Dias A.M.A., Freire M., Coutinho J.A.P., Marrucho I.M., Solubility of Oxygen in Liquid Perfluorocarbons, Fluid Phase Equilibria, 222, p. 325 (2004).
10
[11] Tan Z., Gao G.H., Yu Y.X.,Gu C., Solubility of Oxygen in Aqueous Sodium Carbonate Solution at Pressures up to 10 MPa, Fluid Phase Equilibria, 180, p. 375 (2001).
11
[12] Parker, R.,Whitcombe, M. J., Ring, S. G., Oxygen Solubility and Permeability of Carbohydrates, Carbohydrate Research, 340, p. 1523 (2005).
12
[13] Kaskiala T., Determination of Oxygen Solubility in Aqueous Sulphuric Acid Media, Minerals Engineering, 15, p. 853 (2002).
13
[14] Merker T., Vrabec J., Hasse H., Gas Solubility of Carbon Dioxide and of Oxygen in Cyclohexanol by Experiment and Molecular Simulation, The Journal of Chemical Thermodynamics, 49, p. 114 (2012).
14
[15] Safamirzaei M., Modarress H., Solubility of Oxygen in the Ionic Liquid [bmim][PF6]: Experimental and Molecular Simulation Results, ThermochimicaActa, 545, p. 125 (2012).
15
[16] حسن آبادی، مرتضی، طراحی شبکه عصبی برای بهینه سازی اندازه سطح مقطع شیرهای درون چاهی با اندازه ثابت در چاه هوشمند، نشریه شیمی و مهندسی شیمی ایران، (2)31، ص. 55 (1391).
16
[17] Perry, D. Green (Eds.), “Perry's Chemical Engineers Handbook”, 7th Edition, McGraw-Hill, New York, (1997).
17
[18] Fischer K., Wilken M., Experimental Determination of Oxygen and Nitrogen Solubility in Organic Solvents up to 10 MPa at Temperatures Between 298 K and 398 K, J. Chem. Thermodynamics, 33, p. 1285 (2001).
18
[19] Safamirzaei M., Modarress H., Correlating and Predicting Low Pressure Solubility of Gases in [bmim][BF4] by Neural Network Molecular Modeling, ThermochimicaActa, 545, p. 125 (2012).
19
[20] Garson, G.D., “Interpreting Neural-Network Connection Weights”, AI Expert, 6, p. 46 (1991).
20
ORIGINAL_ARTICLE
Simulation of Volatile Organic Compounds (VOCs) Photocatalytic Removal in a Fluidized Bed Reactor
Photocatalytic oxidation within reactors, as a promising method from economical and environmentally friendly points of view, is used to VOC treatment; and among various types of reactor, the fluidized bed reactor as an efficient reactor is employed for this aim. Modeling and simulation of photocatalytic fluidized bed reactors are essential for scale-up, optimization, and control. In this study, Methyl Ethyl Ketone (MEK), TriColor Ethylene (TCE), and toluene were considered as pollutant models, and photocatalytic conversion of these chemicals in the fluidized bed reactor was simulated. In order to simulate the performance of the photocatalytic fluidized bed reactor, the kinetic sub-model and the hydrodynamic sub-model were coupled together and solved simultaneously. The Langmuir-Hinshelwood (LH) kinetic model was adopted for photocatalytic conversion of pollutants and its kinetic parameters were determined experimentally. The dynamic two-phase models were considered as the hydrodynamic sub-model and its validity was investigated through comparing the simulation data and the experimental results. It was observed that there is close agreement between the model and the experimental data. The modeling and simulation results of this study can be used to predict the performance of the photocatalytic fluidized bed reactor.
https://www.nsmsi.ir/article_9307_c72eae0dcc39ad5bf1820d991439762c.pdf
2014-04-01
57
65
Photocatalytic oxidation
Fluidized bed reactor
Reactor simulation
Dynamic two-phase model
AmirMotamed
Dashliborun
1
School of Chemical Engineering, College of Engineering, University of Tehran, Tehran, I.R. IRAN
AUTHOR
Rahmat
Sotudeh Gharebagh
sotudeh@ut.ac.ir
2
School of Chemical Engineering, College of Engineering, University of Tehran, Tehran, I.R. IRAN
LEAD_AUTHOR
Mohammad
Hajaghazadeh
3
Department of Occupational Health, Health Faculty, Urmia University of Medical Sciences, Urmia, I.R. IRAN
AUTHOR
Hossein
Kakooei
4
Department of Occupational Health, School of Public Health, Tehran University of Medical Sciences, Tehran, I.R. IRAN
AUTHOR
[1] Alberici R.M., Jardim W.F., Photocatalytic Destruction of VOCs in the Gas-Phase Using Titanium Dioxide, Applied Catalysis B: Environmental, 14, p. 55 (1997).
1
[2] Avila P., Bahamonde A., Blanco J., Sanchez B., Cardona A., Romero M., Gas-Phase Photo-Assisted Mineralization of Volatile Organic Compounds by Monolithic Titania Catalysts, Applied Catalysis B: Environmental, 17, p. 75 (1998).
2
[3] Beauchet R., Magnoux P., Mijoin J., Catalytic Oxidation of Volatile Organic Compounds (VOCs) Mixture (Isopropanol/o-xylene) on Zeolite Catalysts, Catalysis Today, 124, p. 118 (2007).
3
[4] Sano T., Negishi N., Takeuchi K., Matsuzawa S., Degradation of Toluene and Acetaldehyde with Pt-Loaded TiO2 Catalyst and Parabolic Trough Concentratorr, Solar Energy, 77, p. 543 (2004).
4
[5] Kim K.J., Kang C.S., You Y.J., Chung M.C., Woo M.W., Jeong W.J. et al., Adsorption-Desorption Characteristics of VOCs Over Impregnated Activated Carbons, Catalysis today, 111, p. 223 (2006).
5
[6] Samantaray S.K., Parida K., Modified TiO2/SiO2 Mixed Oxides: Effect of Manganese Concentration and Activation Temperature Towards Catalytic Combustion of Volatile Oorganic Compounds, Applied Catalysis B: Environmental, 57, p. 83 (2005).
6
[7] Bouzaza A., Laplanche A., Photocatalytic Degradation of Toluene in the Gas Phase: Comparative Study of Some TiO2 Supports, Journal of Photochemistry and Photobiology A: Chemistry, 150, p. 207 (2002).
7
[8] Sano T., Negishi N., Kutsuna S., Takeuchi K., Photocatalytic Mineralization of Vinyl Chloride on TiO2, Journal of Molecular Catalysis A: Chemical, 40, p. 168 (2001).
8
[9] Motamed Dashliborun A., “Experimental Study and Modeling of Photocatalytic Oxidation of Volatile Organic Compound(VOC) by Titanium Dioxide Nanoparticles in a Fluidized Bed Reactor,” M.Sc. Thesis, University of Tehran, Iran (2012).
9
[10] Jafari R., Sotudeh‐Gharebagh R., Mostoufi N., Modular Simulation of Fluidized Bed Reactors Chemical Engineering & Technology, 27, p. 123 (2004).
10
[11] Karimi Golpayegani M., "Photocatalysis for Waste Gas Treatment: Kinetics and Fluidized Bed Reactor Modeling," M.Sc. Thesis, University of Calgary, Canada (2008).
11
[12] Jafari R., Sotudeh-Gharebagh R., Mostoufi N., Two-Phase Simulation of Gas-Solid Fluidized Bed Reactors by Tanks-in-Series Model, Nashrieh Shimi va Mohandesi Shimi Iran, 23(2), p. 33 (2004). [in Persian].
12
[13] Mostoufi N., Cui H., Chaouki J., A Comparison of Two-and Single-Phase Models for Ffluidized-Bed Reactors, Industrial & Engineering Chemistry Research, 40, p. 5526 (2001).
13
[14] Cui H., Mostoufi N., Chaouki J., Characterization of Dynamic Gas-Solid Distribution in Fluidized Beds, Chemical Engineering Journal, 79, p. 133 (2000).
14
[15] Wen C., Yu Y., A Generalized Method for Predicting the Minimum Fluidization Velocity, AIChE Journal, 12, p. 610 (1966).
15
[16] Cai P., Schiavetti M., De Michele G., Grazzini G., Miccio M., Quantitative estimation of bubble size in PFBC, Powder technology, 80, p. 99 (1994).
16
[17] Kunii D., Levenspiel O., “Fluidization Engineering”: Butterworth-Heinemann Boston; (1991).
17
[18] Fogler H. S., “Elements of Chemical Reaction Engineering”, London: Prentice-Hall International; (1999).
18
[19] Peral J., Domnech X., Ollis F., Heterogeneous Photocatalysis for Purification, Decontamination and Deodorization of Air, Wiley Online Library, p. 117 (1997).
19
[20] Lim T.H., Kim S.D., Trichloroethylene Degradation by Photocatalysis in Annular Flow and Annulus Fluidized Bed Photoreactors, Chemosphere, 54, p. 305 (2004).
20
[21] Tomašić V., Jović F., Gomzi Z., Photocatalytic Oxidation of Toluene in the Gas Phase: Modelling an Annular Photocatalytic Reactor., Catalysis Today, 137, p. 350 (2008).
21
[22] Hajaghazadeh M., Kakooei H., Motamed Dashliborun A., Sotudeh-Gharebagh R., Golbabaie F., Afshar S. et al., Photocatalytic Degradation of Methyl Ethyl Kketone by Nano TiO2 in a Fluidized Bed Reactor, Fresenius Environmental Bulletin, 22 (2012).
22
[23] Zhang X., Liao C., Photocatalytic Degradation of Toluene by Nano-TIO2 in a Fluidized Bed, Bepress, p. 73 (2007).
23
[24] Prieto O., Fermoso J., Irusta R., Photocatalytic Degradation of Toluene in Air Using a Fluidized Bed Photoreactor, International Journal of Photoenergy, 2007, p. 1 (2007).
24
[25] Lim T.H., Kim S.D., Photo-Degradation Characteristics of TCE (Trichloroethylene) in an Annulus Fluidized Bed Photoreactor, Korean Journal of Chemical Engineering, 21, p. 905 (2004).
25
[26] Kuo H., Wu C., Hsu R., Continuous Reduction of Toluene Vapours from the Contaminated Gas Stream in a Fluidised Bed Photoreactor, Powder Technology, 195, p. 50 (2009).
26
ORIGINAL_ARTICLE
Optimization and Study on Effective Parameters of Salt Elimination from DMAZ Production Wastewater
Dimethyl amino ethyl azide (DMAZ) is a proper candidate for replacement of hydrazine fuels in space industries. There is very little fuel in wastewater in the process which is not proper to separated, economically. However, due to environmental reasons and less consumption of water, DMAZ-water mixture should be separated and returned to the production process. In this research, because of thermal sensitivity of DMAZ, vacuum evaporation was chosen as a separation method. So, effective parameters were studied for designing of the separation unit. Results showed that the separation efficiency is dependent on temperature of water bath, sub-atmospheric pressure, revolution speed of feed vessel, area of feed vessel and vacuum flow rate. Vacuum evaporation rate was studied under the optimized conditions. Highest efficiency, about 97%, was obtained at 50 minutes.
https://www.nsmsi.ir/article_9453_57cc3ada9a3dd494744865f5f1263fe0.pdf
2014-04-01
67
76
Dimethyl amino ethyl azide
Wastewater
Vacuum evaporation
Optimization
Evaporation rate
Shahram
Ghanbari Pakdehi
sh_ghanbari73@yahoo.com
1
Faculty of Chemistry & Chemical Engineering, Malek Ashtar University of Technology, P.O.Box: 16765-3454 Tehran, I.R. IRAN
LEAD_AUTHOR
Mansoureh
Doustmohammadi
2
Faculty of Chemistry & Chemical Engineering, Malek Ashtar University of Technology, P.O.Box: 16765-3454 Tehran, I.R. IRAN
AUTHOR
Asieh
Ghorbanfekr
3
Faculty of Chemistry & Chemical Engineering, Malek Ashtar University of Technology, P.O.Box: 16765-3454 Tehran, I.R. IRAN
AUTHOR
[1] McQuaid M.J., McNesby K. L., Rice B.M., Chablowski C. F., Density Functional Theory Characterization of the Structure and Gas-Phase, Midinfrared Absorption Spectrum of 2-Azido- N,N- Dimethylethaneamine (DMAZ), Journal of Molecular Structure (Theochem), 587, p.199 (2002).
1
[2] Mellor B., A Preliminary Technical Review of DMAZ: A Low-Toxicity Hypergolic Fuel; Proceeding of 2nd International Conference on Green Propellants for Space Propulsion, Calgiari, Sardinia, Italy 7-8 June, (2004).
2
[3] McQuaid M.J., Amine Azide Propellants, US Patent 6962633 B1 (2005).
3
[4] Meyers C.J., Kosowski B.M., Dimethylaminoethylazide–A Replacement of Hydrazine Derivatives in Hypergolic Fuel Applications, International Annual Conference of ICT, 177, pp. 1- 4 (2003).
4
[5] Schiemenz P., Engelhard H., Trimethoxyphenyl Derivatives.I. Synthesis of Amines - via Mixed Anhydrides, Chemische Berichte, 92, p.857 (1959).
5
[6] قنبری پاکدهی، شهرام؛ سبحانی، ستار؛ کهساری، ایرج؛ بررسی سینتیک واکنش سنتز سوخت مایع دی متیل آمینو اتیل آزید (DMAZ)، مجله علمی ـ پژوهشی مواد پرانرژی، 1، ص 45، (1389).
6
[7] جعفری خواه، خاطره؛ "بررسی پارامترهای مؤثر در تولید DMAZ در مقیاس بنچ و بهینه سازی آنها"، پایان نامه کارشناسی ارشد، دانشگاه صنعتی مالک اشتر، (1390).
7
[8] قنبری پاکدهی، شهرام؛ کهساری، ایرج؛ "تولید سوخت مایع DMAZ در مقیاس بنچ –گزارش فنی"، جلد 2، دانشگاه صنعتی مالک اشتر، (1388).
8
[9] سبحانی، ستار؛ قنبری پاکدهی، شهرام؛ بررسی فرایندهای جداسازی DMAZ، اولین کنفرانس علوم و مهندسی جداسازی، دانشگاه باهنر کرمان، اردیبهشت (1388).
9
[10] سبحانی، ستار؛ "طراحی فرایند جداسازی دی متیل آمینو اتیل آزید"، پایان نامه کارشناسی ارشد، دانشگاه صنعتی مالک اشتر، (1389).
10
[11] Perry R.H., Green D.W., "Perry’s Chemical Engineers’ Handbook"; 7th Edition, McGraw-Hill (1997).
11
[12] Abbenante G., Le G. T., Fairlie D. P., Unexpected Photolytic Decomposition of Alkyl Azides Under Mild Conditions, Chemical Communications, 43, p.4501 (2007).
12
[13] Karagiannis I.C., Soldatos P.G., Water Desalination Cost Literature: Review and Assessment, Desalination, 223, p.448 (2008).
13
[14] Mezher T., Fath H., Abbas Z., Khaled A., Techno-Economic Assessment and Environmental Impacts of Desalination Technologies, Desalination, 266, p.263 (2011).
14
[15] Alatiqi I., Ettouney H., El-Dessouky H., Process Control in Water Desalination Industry: An Overview, Desalination, 126, p.15 (1999).
15
[16] Schmidt E.W., " Hydrazine and Its Derivatives", 2nd edition, John Wiley & Sons (2001).
16
[17] باباپور، عزیز و روستا آزاد، رضا و حسام پور، مهرداد و رضوی ، جلیل، روش جدید درتصفیه پسابهای صنعتی حاوی روغن با استفاده ازسیستم ترکیبی MF-UF، دانشگاه صنعتی شریف، مجله شیمی ومهندسی شیمی ایران ، (1)28، (1388).
17
[18] شاهینی ، محمد و احمد پناه ، سید جواد و بهرامی آده ، نرمین، بررسی پارامترهای عملیاتی موثر بر دانه بندی نمک سدیم کلرید در متبلور کننده DTB در مقیاس رومیزی ، نشریه شیمی و مهندسی شیمی ایران، (1)25، (1385).
18
[19] سمنانی رهبر، مجتبی؛ علیزاده داخل، اصغر؛ پیش بینی افت فشار خشک کن بستر سیال سدیم پربورات با استفاده از دینامیک سیالات محاسباتی، نشریه شیمی و مهندسی شیمی ایران، (2)28، ص. 33 (1388).
19
[20] کنعان پناه، سمیه؛ ابوالقاسمی، حسین؛ بررسی اثرجریان حجمی روی منحنی عبور و ضریب انتقال جرم سالیسیلیک اسیددر فرآیند جذب سطحی توسط رزین آنیونی IRA-93 و ارایه جریان بهینه خوراک، نشریه شیمی ومهندسی شیمی ایران، (4)28، ص. 1 (1388).
20
[21] Director R.C., "Fundamentals of Engineering Heat and Mass Transfer", New Age Science (2009).
21
[22] Belfiore L.A., "Transport Phenomena for Chemical Reactor Design", John Wiley & Sons (2003).
22
[23] Louis T., Francesco R., "Mass Transfer Operations for the Practicing Engineer", John Wiley & Sons (2010).
23
ORIGINAL_ARTICLE
A Comprehensive Study of a Water Treatment Plant in one of the Iranian Oil Fields to Increase Yield and Productivity
Water injection is one of the most effective methods for enhanced oil recovery or reservoir pressure maintenance. The quality of the water is an important factor in the success of a water flooding. The major problem may be associated with water injection is corrosion and plugging of the reservoir that cause injectivity loss and increase in operational cost. The main objectives of sea water treatment plants are to control of important factors such as, oxygen level, bacteria, scaling and suspended solids.This paper presents an overview of optimization of water treatment steps for a seawater injection plant by focusing on corrosion and chemical management. To approach this purpose, a step-by-step review has been implemented on the plant consisting of 40km pipelines, 3-stage filtrations, a deaeration tower, and treatment chemicals. The plant treats seawater for injection into two of Iranian offshore oilfield. That has been in operation for 28 years. During these years, damages have been occurred in the system and relatively in the reservoir due to corrosion and poor control of suspended solids. Besides, it suffers from lack of corrosion monitoring system and has never been inspected for corrosion potential, even though pig cleaning has been run frequently. Field data and laboratory tests indicated that one of the major problems associated with seawater injection in this oilfield results from inadequate filtration and presence of scales, as well as Sulfate Reducing Bacteria. The finest filter size is determined to be lower than 2µm according to the permeability of productive reservoir layer while it is 10µm on the site. Use of poor quality oxygen scavengers in over dose concentration beside the deaeration tower raises the concentration of sulfate and consequently shows up as CaSO4 precipitate. Application of scale and corrosion inhibitor and biocide, as well as their efficacy, are discussed in details. Having NACE TM0299-99 Standard in mind, a corrosion monitoring system has been proposed for the plant. It was proved that with few replacements in chemical injection points, the system efficiency increased by 30%. The outcome of the study was, more effective treatment, less formation damage, as well as reduced cost and quantity of chemicals used per volume of oil produced and treated injected water.
https://www.nsmsi.ir/article_9454_3eed52e05f1d72dd497100d84f351888.pdf
2014-04-01
77
87
Corrosion monitoring
Water Flooding
Enhanced recovery
Inhibitor
scale
Water treatment
Chemicals
Filteration
Sakineh
Shokrolahzadeh
s_shokrolahzadeh@yahoo.com
1
National Iranian Oil Company, IOR Research Institute, Tehran, I.R. IRAN
LEAD_AUTHOR
Samaneh
Ashoori
2
National Iranian Oil Company, IOR Research Institute, Tehran, I.R. IRAN
AUTHOR
Mohammad
Zahedzadeh
3
National Iranian Oil Company, IOR Research Institute, Tehran, I.R. IRAN
AUTHOR
Mojgan
Radmehr
4
National Iranian Oil Company, IOR Research Institute, Tehran, I.R. IRAN
AUTHOR
Emad
Roayaei
5
National Iranian Oil Company, IOR Research Institute, Tehran, I.R. IRAN
AUTHOR
[1] Moghadasi J., Jamialahmadi M., Muller-Steinhagen H., Izadpanah M.R., Formation Damage in Iranian Oil Fields, SPE 73781, February (2002).
1
[2] Gao Chang, Factors Factors Affecting Particle Retention in Porous Media, Emirates Journal for Engineering Research, 12, p. 1 (2007).
2
[3] ASTM D4582-10, "Standard Practice for Calculation and Adjustment of the Stiff and Davis Index for Reverse Osmosis", American Society Testing and Materials, (2010).
3
[4] "PVT SIM Manuals"، Calsep Company, Version 15, (2005).
4
[5] صبوری, سمانه؛ لطف اللهی, نادر؛ متحدین, پویا؛ تعیین مقدار رسوب در فرایند تزریق آب به مخازن نفتی ایران, نشریه شیمی و مهندسی شیمی ایران, (1)31, ص. 115, (1391).
5
[6] Mitchell R.W., The Forties Field Seawater Injection System, SPE 6677, June (1978).
6
[7] Wheller D., Treating and Monitoring 450000 B/D Injection Water, Pet. Eng, November (1975).
7
[8] Ostroff, A. G., "Introduction to Oilfeild Water Technology", Prentice-Hall, (1965).
8
[9] Hamouda A.A., Water Injection Quality in Ekofisk – UV Sterilization and Monitoring Techniques, SPE 21048, February (1991).
9
[10] Barton Larry.L," Sulfate-Reducing Bacteria", Plenum Press, New York, p.277 (1995).
10
[11] Sequeira C.A.C., Tiller A.K., "Microbial Corrosion", Elsevier, p.191 (1988).
11
[12] Zettlitzer Michael, Busch Matthiass, Produced Water Cleaning and Re-Injection Experience - Zero Discharge to water, 4th International Conference on Produced Water Management, January (2007).
12
[13] Zahedzadeh M., Masoudi R., Saboormaleki M., Feasibility Study of Produced Water Re-Injection in Siri Oil Field in Iran, EAGE First International Petroleum Conference and Exhibition, May (2009).
13
[14] شکراله زاده, سکینه؛ زاهدزاده, محمد؛ رعایایی, عماد؛ رادمهر, مژگان؛ بررسی کارایی و تعیین غلظت بهینه بازدارنده رسوبات معدنی مورد استفاده در یکی ازمیادین نفتی ایران, پژوهش نفت, شماره 67, ص. 50 (1390).
14
[15] Bayona H.J., A Review of Well Injectivity Performance in Saudi Arabia΄s Ghawar Field Injection Program,
15
ORIGINAL_ARTICLE
Hydrodynamics Investigation of the Gas Centrifuge
Regard to the extensive applications of gas centrifuges to remove gas pollutants, detailed knowledge of the flow behavior inside a gas centrifuge is important and necessary to properly design and optimization of its operation. In this research, gas centrifuge hydrodynamic and heat transfer phenomena have been simulated in unsteady state condition, three dimensional and supposing gas phase as compressible flow using CFD technique. According to high speed rotation of gas centrifuge outer wall, Multiple Rotating Reference Frame (MRF) approach applying k-ε RNG and RSM turbulence model was implemented in computational model. Computational model results include pressure, velocity, temperature profile as well as fluid flow pattern in the gas centrifuge. Comparing the CFD simulation results applying the RNG k-ε and RSM turbulence models, indicate that there are little difference between the velocity and radial pressure of the fluid. Hence, considering the high computational cost of the RSM model, the RNG k-ε turbulence model seems efficient in determining the turbulent fluid characteristics in gas centrifuges. The CFD simulation results approved that fluid swirl in gas centrifuge, feed inlet as well as upper and bottom scoops, extremely affects fluid flow pattern and axial gas velocity.
https://www.nsmsi.ir/article_9455_1c7289ecc142324df101ca0c6a5bf18e.pdf
2014-04-01
89
101
Gas centrifuge
CFD Simulation
Hydrodynamic
Multiple Rotating Reference Frame (MRF)
Mohammad Reza
Mohammadi Jozani
1
Chemical Engineering Department, Iran University of Science and Technology, Tehran, I.R. IRAN
AUTHOR
Yaghoub
Behjat
behjaty@ripi.ir
2
Process Development and Equipment Technology Division, Research Institute of Petroleum Industry (RIPI), Tehran, I.R. IRAN
LEAD_AUTHOR
Shahrokh
Shahhosseini
shahrokh@iust.ac.ir
3
Chemical Engineering Department, Iran University of Science and Technology, Tehran, I.R. IRAN
AUTHOR
Ahad
Ghaemi
aghaemi@iust.ac.ir
4
Chemical Engineering Department, Iran University of Science and Technology, Tehran, I.R. IRAN
AUTHOR
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