13 research outputs found

    PRARANCANGAN PABRIK PHTHALIC ANHYDRIDE DARI NAPHTHALENE DAN UDARA

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    Phthalic anhydride plant is designed with capacity 80.000 ton/year. It is operated for 330 day/year. The purity of phthalic anhydride in product is 99,93% with maleic anhydride and naphthoquinone as impurities. The method for production of phthalic anhydride is partial oxidation of naphthalene using air. The raw materials are 99.421,66 ton/year naphthalene 99,9% and 1.118.915,90 ton/year air to produce 80.000 ton/year phthalic anhydride. Naphthalene solid is melted from the storage prior to further be evaporated. The pressure and temperature of naphthalene vapor and air are increased to the operating conditions of the fluidized bed reactor (3 atm and 360 oC). Products out from reactor are cooled and then are separated from non-condensable gas. Furthermore, phthalic anhydride is separated from maleic anhydride in the distillation column-01. Phthalic anhydride is purified from naphthoquinone in the distillation column-02. Phthalic anhydride 99,93% go to prilling tower. Product from prilling tower is phthalic anhydride prill (diameter = 3 mm). Phthalic anhydride is packed and is stored in storage. The plant of phthalic anhydride will be bulid in Cilegon, Banten. The area of plant is 100.000 m2 and it has 321 labour. The plant of phthalic anhydride with capacity 80.000 ton/year needs water 1.337.703,861 kg/hour, pressure air 400 m3/hour, 12.995,4965 electricity kW and fuel 1.140,6003 kg/hour. Fixed capital of phthalic anhydride plant is US45,456,757.47+Rp244.554.676.901,73,workingcapitalUS 45,456,757.47 + Rp 244.554.676.901,73, working capital US 17,297,530.58 + Rp 36.631.450.571,92. Profit before taxes is Rp 192.712.735.480,10and profit after taxes is Rp 96.356.367.740,05. The economic evaluation shows that the plant has Return on Investment (ROI) before taxes 27,70%, after taxes 13,85%. Pay Out Time (POT) before taxes is 2,65 years, after taxes is 4,19 years. Break Event Point (BEP) 41,69%, Shut Down Point (SDP) 16,51% and Discounted Cash Flow Rate of Return (DCFRR) 19,34%. Based on the economic analysis, the design of phthalic anhydride plant from naphthalene and air with capacity ton/year is interesting to be studied further

    PRARANCANGAN PABRIK PHTHALIC ANHYDRIDE DARI NAPHTHALENE DAN UDARA KAPASITAS 80.000 TON/TAHUN

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    Phthalic anhydride plant is designed with capacity 80.000 ton/year. It is operated for 330 day/year. The purity of phthalic anhydride in product is 99,93% with maleic anhydride and naphthoquinone as impurities. The method for production of phthalic anhydride is partial oxidation of naphthalene using air. The raw materials are 99.421,66 ton/year naphthalene 99,9% and 1.118.915,90 ton/year air to produce 80.000 ton/year phthalic anhydride. Naphthalene solid is melted from the storage prior to further be evaporated. The pressure and temperature of naphthalene vapor and air are increased to the operating conditions of the fluidized bed reactor (3 atm and 360 oC). Products out from reactor are cooled and then are separated from non-condensable gas. Furthermore, phthalic anhydride is separated from maleic anhydride in the distillation column-01. Phthalic anhydride is purified from naphthoquinone in the distillation column-02. Phthalic anhydride 99,93% go to prilling tower. Product from prilling tower is phthalic anhydride prill (diameter = 3 mm). Phthalic anhydride is packed and is stored in storage. The plant of phthalic anhydride will be bulid in Cilegon, Banten. The area of plant is 100.000 m2 and it has 321 labour. The plant of phthalic anhydride with capacity 80.000 ton/year needs water 1.337.703,861 kg/hour, pressure air 400 m3/hour, 12.995,4965 electricity kW and fuel 1.140,6003 kg/hour. Fixed capital of phthalic anhydride plant is US45,456,757.47+Rp244.554.676.901,73,workingcapitalUS 45,456,757.47 + Rp 244.554.676.901,73, working capital US 17,297,530.58 + Rp 36.631.450.571,92. Profit before taxes is Rp 192.712.735.480,10and profit after taxes is Rp 96.356.367.740,05. The economic evaluation shows that the plant has Return on Investment (ROI) before taxes 27,70%, after taxes 13,85%. Pay Out Time (POT) before taxes is 2,65 years, after taxes is 4,19 years. Break Event Point (BEP) 41,69%, Shut Down Point (SDP) 16,51% and Discounted Cash Flow Rate of Return (DCFRR) 19,34%. Based on the economic analysis, the design of phthalic anhydride plant from naphthalene and air with capacity ton/year is interesting to be studied further

    PIROLISIS LIMBAH BATANG DAUN TEMBAKAU

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    Fuel scarecity can be overcome by developing the potential of renewable energy sources such as biomass, as an alternative energy source. The potential of tobacco leaf stem and the bone waste is abundant in Indonesia, with the amount of 49966 tons per year or 151.41 tons per day. The purposes of this study are divided into three purposes. First, to know the effect of temperature and kind of tobacco leaf stems waste to the yield of pyrolysis product. Second, to know the effect of temperature to the components and compositions of pyrolysis product. Third, to find the model of reaction kinetics which can be used to product liquid mass (bio oil) and gas mass in pyrolysis process. The experiment was conducted by using a batch reactor equipped with an electric heater with thermo controls to regulate the temperature. The Steps of the experiment are: raw materials preparation process, extraction process, and pyrolysis process. During the pyrolysis process the liquid weigh and the gas volume were measured every 15 minutes for 90 minutes. After the pyrolysis was done the liqid was taken to be analyzed by using GS-MS, the solid was analyzed with the method of proximate and ultimate and gas was analyzed by using gas cromatography. The results of the experiment showed that the highest yield of liquid (biooil) was obtained at the temperature of 500o C as 39.74% for tobacco leaves bone and 36.76% for tobacco leaves butt. The main composisitions of the liquid are ketones, acids, phenols and some aromatic compounds. The highest fixed carbon content in the solids (char) was obtained at the temperature of 500o C for 37.40% with a calorific value produced ranged from 18.44 up to 20.09 MJ/Kg which equal to the medium quality of coal. While the highest hydrogen content was obtained at the temperature of 500oC as 15.04% and the highest carbon dioxide content was obtained at temperatures of 2500C as 78.27%. The reaction of rate constants is exponentially affected by the temperature with the value of k1 = 0,051e �340,4/T , k2 = 0,076e � 420,8/T for tobacco leaves bone and the value of k1 = 0.063e -668,2/T, k2 = 0,060e -503,3/T for tobacco leaves butt

    TUGAS PRARANCANGAN PABRIK UNIT CARBON BLACK DARI MINYAK BERAT KAPASITAS 100.000 TON/TAHUN

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    Carbon black plant of heavy oil is design with a capacity of 100,000 tons/year through the furnace combustion process in the two pieces of furnace reaktor, which are arrange parallel Gravley. The reaction occurs at a pressure of 9.914 atm at a temperature of 1200 to 1700 °C. Heavy oil as fuel 126,914.8115 tons/year go into the reactor at 160°C by heating steam which is using the heat from hot process gases. 1,563,084.6820 tons/year air for combustion are burn along with oil burning heavy fuel that produces heat to vaporize the heavy oil feed to the cracking temperature of 1650 °C. The vapor of cracking heavy oil will become carbon black and hydrogen gas and experience quenching with 249,502.3776 tons/year of water. Conversion occurs at 90%. Cracking process gases with carbon black separated via cyclones 2-4 series parallel. Carbon black powder with molasses, then mixed in the surge tank, and then formed into pellets in a pelletizer and dried by rotary dryer. The plant will be establish in Balongan, West Java in the area of 120000 m2 including area for expansion with 131 people labor needed. Factory work continuously for 24 hours a day for 330 days a year. Time to do the turn around is 35 days per year, including the time to start up and shut down. From the evaluation of economic, the results are Rp 471,975,782,980.45 + U.S. $ 69,248,894.23 of fixed capital, Rp 355,123,331,890.51 of working capital, Rp 1,123,811,825,682.89 of manufacturing cost, Rp 868,726,516,820.03 of general expenses. Profit before and after tax are Rp 510,136,657,497.08 / year and Rp 255,068,328,748.54 / year. Pre-tax and after taxes of ROI are 43.81% and 21.90%. POT before and after tax are 1.86 and 3.13 years, and then 47.57% of BEP, 29.79% of SDP, and 36.57% of DCFRR. From the economic evaluation, it can be conclude that the carbon black plant with a capacity of 100,000 tons/year is quite interesting to study further

    PEMBUATAN SODIUM LIGNO SULFONAT (SLS) DARI ISOLAT LIGNIN TANDAN KOSONG KELAPA SAWIT (TKS) DENGAN KATALIS NaOH PADA PROSES SULFONASI

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    intension of two liquid phases. One example is sodium ligno sulfonate (SLS) which is useful to enhance oil recovery in oil refinery industry. SLS is a result of the reaction of sulfite and lignin, which lignin is obtained from solid waste of oil palm bunches that we know it is very abundant, easy to obtain, and cheap. In design of a surfactant reactor we need some data of reaction kinetics. The purpose of this research is to understand the kinetics and the influence of some factors to the reaction of SLS-making process. SLS-making process is conducted by a sulfonation process in a stirred tank �batch� reactor. NaOH catalyst was added to decrease the activation energy in lignin and it is a pH regulator of the sulfonation reaction. SLS-making process is done by varying concentration of NaHSO3 reaction (10%, 15%, 20%, 25%, 30%) and reaction time (30, 60, 90, 120, and 180) minutes. Referring to the research results can be shown that the reaction kinetics is controlled by a chemical reaction using a model of liquid-liquid reaction of both sulfite and lignin which are activated in the liquid phases. The highest conversion of sulfonation process is 89% on the condition of the weight of lignin isolates 10 gram, the concentration of NaHSO3 30%, the concentration of catalyst 20% at pH 7, the temperature 950C, and the reaction time 180 minutes, respectively. The suitable model of this research is a quasi-order irreversible reaction. The correlation of the temperature influence to the constant of reaction rate can be expressed by the exponential equation: k = 6.6467 x 10 pangkat 4 exp (- 28961,9 / RT), (liter/mol.min)

    KAJIAN PENCEMARAN DETERJEN DAN FOSFAT AKIBAT LIMBAH DOMESTIK PERMUKIMAN KUMUH DI SUNGAI BRANTAS KOTA MALANG - JAWA TIMUR

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    One of the problems can never be solved, is a detergent sewage directly into water bodies. Waste detergents disrupt aquatic ecosystems. Beside that, phosphate as filler of detergent can caused eutrophication in waterways. he study aims to assess the concentration of detergents and phosphates, comparing the amount of use of detergent in each research area, and the influence of detergent phosphate pollution of chemical physical factor of river water, also aquatic organisms (phytoplankton ) as bio-indicators of organic pollution. This study used a survey method with purposive sampling method. Data collection was took three times in three research areas, upstream (Dinoyo and Ketawanggede), middle ( Penanggungan and Samaan) and downstream (Oro - oro Dowo and Kiduldalem). Sampling was carried out with considering the speed of the river flow and peak activity in the household wash. Detergents and phosphate concentration compared with Keputusan Gubernur No.45 Tahun 2002 and Peraturan Pemerintah No.82 Tahun 2001. Comparison of the use of detergent in each areas were analyzed by analysis of variance statistic. Effect of detergent concentration and phosphate to the physical chemical factors of river water and phytoplankton abundance analyzed by using of multiple regression statistics . The results showed : ( 1 ) concentration of detergents is not to exceed the quality standard designation yet, ranging from 0,050 to 0,309 mg / L, whereas the concentration of phosphate has goes exceed the designation of Class II quality standards ranging from 0,031 to 0,690 mg / L. ( 2 ) The average use of detergents slum society in Brantas river bank based on analysis of variance of the pathway , were significantly different in each area of study, the downstream use of detergents has declined. ( 3 ) Detergent and phosphate concentration in Brantas River influencing the change of turbidity about 61,6 % , dissolved oxygen ( DO ) 47,6% and a pH 15%. Concentration of phosphate detergents and also gives effect to the abundance of phytoplankton at 12,6 %
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