PRARANCANGAN PABRIK XYLIDINE DARI NITROXYLENE DENGAN PROSES HIDROGENASI KAPASITAS 10.000 TON/TAHUN

Xylidine plant from nitroxylene and hydrogen with capacity 10,000 tons/year is designed to meet the demand of domestic xylidine and also international demand especially in Southeast Asia. The needs of xylidine in 2018 will be around 1,300 ton/year,and it will getting higher each year, and reach about 2,602.85 tons/year in 2028. The plant will be operated for 330 days/year. Xylidine product is in liquid phase and its purity is 99%. The raw materials used are 14,175.3942 tons/year nitroxylene and 744.5898 tons/year hydrogen. Based on the operating conditions, the selection of raw materials used, and the type of product produced, the plant is classified as medium-risk plants. The process of making xylidine from nitroxylene and hydrogen consists of three main processes, the first is the preparation of raw materials, the second is synthesis process, and the third is purification process of reaction products. In the first process, the raw materials operating condition is adjusted at temperature 60�C and pressure 10 bar. In the synthesis process, the reaction between nitroxylene and hydrogen is very exothermal using continuous stirred tank reactor with sparger and cooling coil. This reaction needs palladium on charcoal as a catalyst for 176.93 kg/year. The enthalpy of reaction is -488 kJoule/mol of nitroxylene reacted. The resulting products are xylidine and water. In purification process, water will be separated from other organic compounds using decanter and it will flow to waste water treatment unit. The last purification process is purifying the main product, xylidine, using distillation column. The yield on distillation such as xylidine 10,000 tons/year with 99% purities. The plant will be located in Tuban, East Java with a land area of 4,5 hectares because in Tuban, there are PT. Petrokimia Tuban and PT. Samator Tuban as a supplier of hydrogen, and also the plant is located near the port to make export and import activities easier. The plant will employ 231 employees. To support this process, the utility takes steam as much as 25,924.24 kg/hour, cooling water 28,986.32 kg/hour, 533.80 kVA electrical needs, and compressed air as much as 100 m 3 /hour. Fixed capital required amounted to US$7,622,910.39 + Rp 64,083,702,722.89 and working capital US$ 19,852,753.46 + Rp 11,173,132,807.53. Profit before tax is Rp 40,831,662,478.21 and profit after tax is Rp 20,415,831,239.11. From the results of calculations, the Return on Investment (ROI) before taxes is 29.44%, and 14.72% after tax. Pay Out Time (POT) before taxes is 2.54 years, 4.05 years after tax. Break Even Point is 56.65% capacity, Shut Down Point is 37.45% and Discounted Cash Flow Rate Of Return is 19.7821%. From the results of the feasibility study plants through economic evaluations that have been done on xylidine from nitroxylene and hydrogen with a production capacity of 10,000 tons / year, it can be concluded that the plant deserves to be studied further

SISTEM CO2-ETANOL DALAM BENTUK GAS-EXPANDED LIQUID (GXL) SEBAGAI PELARUT UNTUK EKSTRAKSI SENYAWA XANTHONE DARI KULIT MANGGIS

CO2-eXpanded Liquid (CXL) has been known as a promising system in various applications. In this research, CO2 gas is introduced to Ethanol to form CO2-expanded Ethanol and used as a solvent to extract xanthone from mangosteen fruit rind. Ethanol was mixed with mangosteen fruit rind powder at ratio 5:1 (v/wt) and then CO2 was introduced at various pressures (0.50 MPa to 5.25 MPa) at room temperature for 24 hours until reach its equilibrium state. Xanthone which dissolved in ethanol were obtained from the extraction apparatus as CO2 degassed out from the system. Quantitative analysis method was developed by using High Performance Liquid Chromatography (HPLC) containing methanol:water as mobile phase to determine number of xanthone extracted at various pressures. Number of CO2 disolved in ethanol was calculated theoritically using Peng-Robinson EoS and UNIQUAC Excess Gibbs Energy equation by assuming that the system was in binary composition of ethanol-CO2. Thermodynamic analysis was carried to predict the non-ideality (activity coeficient) of the xanthone solubility in etanol-xanthone-CO2 system by using Two-Suffix Margules, Van Laar, Three-Suffix Margules, and UNIQUAC (Model I, II, III, and IV) equation of Excess Gibbs Energy. Xanthone solubility in CO2-expanded Ethanol is reaching its maksimum point (1.3380x10-05) at 2.80 MPa pressure or at 0.3272 mol fraction of CO2 disolved in ethanol. Thermodynamic binary parameters for each model were predicted by using Sum Square of Error (SSE) by fitting experimental data into the models. Activity coefficient of xanthone was obtained at 303 K at various pressure, 3,040.86 � 6,151.86 (model I), 2,765.21 � 5,966.26 (model II), 2,757.37 � 6,050.47 (model III), and 2,996.19 � 6,067.50 (model IV), while the lowest SSE was occurred by using van Laar eqution (Model II)

PENGARUH LUAS PERMUKAAN DAN LEBAR PORI KARBON AKTIF PADA SISTEM ADSORBED NATURAL GAS (ANG)

Natural gas (NG) is one of the best alternative fuel to replace gasoline due to its clean properties, higher HHV, cheap price, and its vast proved reservoirs in the world. The main problem to NG utilization are its transportation and storage system. So far, there are three known technologies for on-board NG storage: liquefied natural gas (LNG), compressed natural gas (CNG) and adsorbed natural gas (ANG). In recent years, ANG has attracted considerable attention as a possible alternative to CNG and LNG. NG consists of mainly methane (85-95%) with a minor amount of ethane, and higher-order hydrocarbon compounds, therefore, the characteristics of NG are similar to methane. In this experiment, we used CNG as the substitute for NG because they have the same composition. The amount of adsorbed gas in ANG system depends on adsorbent types and properties. Previous experiment showed that activated carbon is the most potential material for ANG storage adsorbent. The objective of this study is to evaluate the effect of activated carbon pore structure (BET surface area and pore width) to the amount of adsorbed methane. We also discuss the heat of adsorption as well as the optimum pore width which are important factors in ANG performance. In order to evaluate the effect of adsorbent surface area, adsorption of methane and CNG in three activated carbons with 1,000-3,000 m2/g BET surface area (carbon Maxorb, RTBPF, Ajax) has been done. Another experiment of methane adsorption in two activated carbon with same BET surface area but different pore width (Ajax and RPF-EG2) is used to evaluate the effect of pore width. The methane and CNG adsorption and desorption equilibrium data were measured by a static volumetric adsorption system at operational pressures ranges (0-4 MPa) and temperature ranges (303-323 K). The experimental data is well fitted by Langmuir, Freundlich, Sips, Unilan, and Toth models. The Toth model provided the best fit to the experimental adsorption isotherms. The activated carbon which have the biggest adsorption intake is ordered as follows: Maxsorb > RTBPF > Ajax > RPF-EG2. The results indicates that the amount of adsorbed methane is proportional to the surface area while pore width also have effect on it. The heat of adsorption is ordered as the opposite of the order of the amount of adsorbed methane. Grand Canonical Monte Carlo (GCMC) method has been used to calculate the adsorption isotherms and optimum pore width for a simple model of methane confined in slit carbon micropores at various temperatures (303 K-323 K) and pore widths (4-60 A). Methane molecules are modeled as the Lennard-Jones spherical molecules, and Steele�s 10-4-3 potential is used to represent the interaction between the methane molecule and the adsorbent wall. Good agreement between simulated and experimental data indicates that our model represents well the mechanism of methane adsorption on an activated carbon. Our simulation found that the optimum pore width for methane adsorption are 8,35 � (303 K), 8,51 � (313 K), and 8,79 � (323 K)

LIFE CYCLE ASSESSMENT MODUL AIRBAG KEMUDI PADA MOBIL UKURAN KECIL

Airbag has long been mandatory safety equipment in car. Its production will continue to grow along with the continued increase in the number of cars produced. In addition to its benefits to reduce the risk of injury to the rider, airbag may have environmental impacts during their life cycle. In a country with high environmental awareness, a mass-made product such as airbag, have to go through a holistic and comprehensive environmental impacts study, which started from raw materials extraction, production, use and disposal. Airbag was manufactured from several components. Each component has the potential to contribute to environmental impacts. In addition, when the airbag was used in the vehicle, the weight of airbag will increase the car's weight, the consequences will increase its energy needs. The purpose of the study are to determine the environmental impact of the airbag of the whole life cycle using the methodology of Life Cycle Assessment (LCA). The methodology was chosen because until recently, LCA was recognized by the International Standard Organization (ISO) as a standardized scientific method for systematic analysis of environmental impacts associated with a product. The study began with determining the scope of research. The next step is collecting data for each constituent component of the airbag, which are label, nut, cover, can, cushion and inflator. The data collected includes data on the number of raw materials used and discarded, the energy and water consumed, wastes which to be disposed of, as well as emission data released during the life cycle of airbag. Emissions data are then grouped according to the environmental impacts caused by the emissions and subsequently weighted in accordance with the level of danger in the environment. The results of this study indicate that during the life cycle of airbag has a global warming potential equivalent to 31.42 kg of CO2, acidification equivalent to 44.14 g of SO2, eutrophication is equivalent to 32.82 g of NOx, toxic effects on aquatic environment equivalent to 399 m 3 of contaminated water, and the impact of human toxicity equivalent 57.53 g bodyweight. The entire life cycle of airbag is also produces 4.93 kg of waste and consumes 561.67 MJ and 79.24 kg of water. While the most dominant phase in the life cycle is the production stage steering wheel airbag, because it becomes the dominant source of 4 of the 5 categories of environmental impact. At the production stage, the dominant process is the production of iron and nylon. While the use phase is contribute mostly for global warming, where the airbag is adding fuel consumption during car use. Therefore, the improvements that can be done for example by reducing the heavy metal components, thereby reducing the environmental impact of the use phase. In addition, the reduction of environmental impact nylon material can be done by reducing the severity or by substitution with other polymeric materials. The results of this study are to be used as starting knowledge in product development research airbag smaller environmental impacts

Prarancangan Pabrik Etilen Glikol dari Etilen Oksida dan Air Kapasitas 250.000 ton/tahun

Ethylene glycol (mono ethylene glycol) plant from ethylene oxide and water with capacity of 250,000 tons / year is designed to meet the demand of domestic ethylene glycol, ethylene glycol projected domestic needs of 480,460 tons / year in 2015. The plant will operate for 330 days / year. Ethylene glycol product with a purity of 99.9%. The raw materials used are 229,999 ton/year ethylene oxide and 470,433 ton/year water. Based on the operating conditions, the selection of raw materials used and the type of product produced, the plant is classified as high-risk plants. Manufacturing process of ethylene glycol from ethylene oxide and water consists of three main processes, the first is the formation of ethylene glycol from ethylene oxide and water, sulfuric acid catalyst neutralized process, and the last is purification process of ethylene glycol as the main product. Formation process of ethylene glycol from ethylene oxide and water carried by the flow stirred reactor operating conditions 14 atm pressure and at temperature of 100 ° C using a catalyst H2SO4 (sulfuric acid) 98% as much as 62,707 ton/year. The products produced in the form of ethylene glycol, diethylene glycol, and triethylene glycol. The next stage is the removal of the catalyst H2SO4 with NaOH solution as much as 51.147 ton/year in neutralizer, neutralizer out products such as water and salt Na2SO4 then separated using a filter to be sold as byproduct. The last process is the main product of ethylene glycol purification using multilevel distillation to separate the water first, then the separation of ethylene glycol and diethylene glycol. The yield on distillation such as ethylene glycol 258,307 ton/year and the results in the form of diethylene glycol as 46,524 ton/year as byproduct. The plant will be established in Cilegon, Banten with a land area of 6 hectares and employs 132 employees. To support this process, the utility takes steam as much as 74,980.90 kg / hour, cooling water 1,272,431.54 kg / hour, 5993.81 kVA electrical needs, and compressed air as much as 75.6 m3/hour. Fixed capital required amounted to US$60,894,445 + Rp. 194,502,333,484 and working capital US$ 115,341,868 + Rp 21,840,345,345. Profit before tax is Rp. 344,583,634,311. And profit after tax is Rp. 172,291,817,156. From the results of calculations, the Return on Investment (ROI) before taxes 44,93% and 22.46% after tax. Pay Out Time (POT) before taxes 1.82 years, 3.08 years after tax. Break Even Point 40.08%, Shut Down Point 24.61% and Discounted Cash Flow Rate Of Return 25.83%. Ethylene glycol plant design of ethylene oxide in terms of raw material purchase price and selling price losses as prices of raw materials ethylene oxide is more expensive than the price of the product ethylene glycol per one ton of material. So the raw material of ethylene oxide manufactured its own raw materials ethylene and air to plant deserves to be studied. From the results of the feasibility study plants through economic evaluations have been done on plant ethylene glycol from ethylene, air, and water with a production capacity of 250,000 tons / year can be concluded that the plant deserves to be studied further

PENJERAPAN GAS RUMAH KACADENGAN MENGGUNAKAN BERBAGAI KARBON BERPORI

CO2 and CH4 gas are green house gasses which contribute to earth surface temperature increase (global warming) post industrial period, sea level rise and the other environment impacts. Some efforts have already performed to reduce green house gassses emission. One of those is by adsorption method. This research was done with a purpose to proof CO2 and CH4 gas physisorption capacity by phenolic-resin porous carbon using static volumetric method. The porous carbons have various internal surface area and pore structure. The research was conducted in several stages, namely assembling a highpressure adsorption test equipment by static volumetric method, characterization of porous carbon (internal surface area, pore volume, pore size distribution, SEM, FTIR), sample preparation and testing of porous carbon adsorption capacity for CO2 gas and CH4 gas either on wet or dry state. Dry porous carbon adsorption test performed on a different system temperatures (273K, 298K, 308K and 318K), while in wet porous carbon carried out at a temperature of 277K to see the possibility of gas hydrate formation. With reference of low pressure gas adsorption datas, isosteric heat of adsorption can be calculated specifically for this type of adsorbate and adsorbent (porous carbon). Then, the obtained isotherm curves were evaluated using the Toth equation. This research revealed that among all porous carbons samples, the highest CH4 adsorption capacity on 3.5 MPa and 298 K belongs to mesopore carbon MS1 (capacity 8.88 mmol/g) whereas the highest CO2 adsorption capacity on 3.4 MPa and 298 K belongs to mesopore carbon MS2 (capacity 25.78 mmol/g). Afterward, in order to increase CO2 and CH4 adsorption capacity, there are other options by creating gas hidrat or capillary condensation. The best option for CH4, is adsorption by wet porous carbon MS2 (gas hydrate) on 277K and 3.8 MPa (capacity 15.5 mmol/g). The best option for CO2 is adsorption by dry porous carbon (capillary condensation) on 273K and 3.8 7MPa (capacity 172 mmol/g)