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A.S. Nasution
Research and Development Centre for Oil and Gas Technology "LEMIGAS"
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ZEOLIT CRACKING CATALYST A.S. Nasution; E. Jasjfi; Evita H. Legowo
Scientific Contributions Oil and Gas Vol 26 No 1 (2003)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.26.1.993

Abstract

Nowadays, refiners are facing a continuing need to add bottom processing by catalytic process (catalytic cracking and hydro cracking processes) capacity a result of gradually deteriorating crude oil quality and flat-to-declining for residualfuel oil.
PRODUCTION OF UNLEADED GASOLINE IN ASEAN COUNTRIES A.S. Nasution; E. Jasjfi
Scientific Contributions Oil and Gas Vol 29 No 2 (2006)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.29.2.1026

Abstract

Worldwide crude supply is experiencing a mod- est trend towards heavier and high sulfur content. The Middle East, being traditionally the world's ma- jor oil exporting region, will continue to be the princi- pal supplier of lower quality crude's in the future", For the period 1992-2005, the average annual demand growth rate for light products ( gasoline, kero- sene, diesel oil) is higher than for residual fuel oil21, These data clearly show that the need will continue for converting additional bottom fraction into light products, by both thermal or catalytic conversions. The passage of the Clean Air Act Amendement of 1990 in the USA has forced American refineries to install new facilities to comply with stricter speci- fications for fuels such as gasoline and diesel oil such as Asia-Pacific, California Air Resources Board (CARB) and European Commission (EC) [3.4. 5). Various terms in the models address qualities and the gasoline blended such as benzene, total aromatics and olefin contents, RVP, the T90 of distillation range, sulphur content, and oxygenates content. Comparison of fue l specifications between ASEAN countries and reformulated fuels and typi- cal compositions of gasoline and gas oil components for production of commercial unleaded gasoline is included in this report.
DRIVEABILITY INDEX OF COMMERCIAL GASOLINE IN ASEAN COUNTRIES A.S. Nasution; E. Jasjfi
Scientific Contributions Oil and Gas Vol 29 No 3 (2006)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.29.3.1031

Abstract

Motor gasoline is essentialy a complex mixture of hydrocarbons distilling between about 40°C and 225°C and consisting of compounds generaly in the range C5 to C12. Small amounts of additives are also used to exchange various aspects of the performance of the fuel. Gasoline produced from different refin[1]eries can vary widely in compositions, even at the same octane level.The primary requirement of a gasoline is that should burn smoothly without exploding, under the conditions existing in the combustion chamber of the spark-ignition, so that themaximum amount of useful energy is liberated[1].The volatility of a gasoline has a vital influence on the both performance of a car emission. It affects the way car starts, the time it takes to warm up, the exten to which ice will form in the carburator, causing stalling and other problems; it influences vapour lock in the fuel system and indirectly it determines overall fuel economy. Volatility is a measure of the ability of a fuel to pass from the liquid to the vapour state under varying conditions.In cold weather, cars can take a very significant time to warm-up i.e., be capable of smooth, non-hesitating accelerations without the use of the choke. The fuel parameter that is found to have the grestest influence on warm-up is the mid-boiling range volatility as characterized by for example; the 50 per cent distillation temperature. Even after the car has warmed up, fuel volatility can still have an influence on acceleration time. Low volatility fuels obviously give leaner mixture and as mixtures leaner, acceleration performance can fall off quite rapidly.The fraction of the fuel that influences acceleration behaviour to the greatest extent is in the mid and to a lesser extent the higher boiling range. Thus, the 50% distillation temperature, sometimes together with the 90% distillation, must be controlled to ensure optimum acceleration behaviour. The factors which influence vapour lock is the volatility characteristics of the fuel. The degree to which a fuel is liable to give vapour lock depends mainly on its front end volatility. A number of different front-end volatility parameters have been used to define the vapour locking tendency of a fuel, such as RVP, percentage evaporated at 70°C, the 10 and 15% slope of the distillation curve, the vapour/liquid ratio at a given temperature and pressure. These distillation characteristics affect the following performance characteristics: starting, vapour lock and driveability.ASTM D4814-98a the standard specification for Automotive Spark-Ignition Engine Fuel has included Driveability Index as an item of performance requirement of the fuel. The inclusion of the parameter is to provide control of distillation parameters that influence cold start and warm up driveabilities.
PRODUCTION OF CLEAN DIESEL OILS A.S. Nasution; E. Jasjfi; Evita H. Legowo
Scientific Contributions Oil and Gas Vol 28 No 2 (2005)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.28.2.1038

Abstract

Cars and fuels have been developed simultaneously and nowadays cars demand a very sophisticated fuel indeed. Environmental restriction and efforts to minimize the pollution problem by exhaust gases are causing de- sign changes in cars that in turn are having some effects on fuel quality. The development of processes for making high cetane number gas oil blending components and the widespread use of additives to enhance fuel properties have all contributed to the highly developed motor fuel used today". Gas oil components produced in the refineries generally consist of predominantly straight-run gas oil (SRGO) obtained from the fractional distillation of crude oils. There are two types of straightrun gas oil ie a sulfur rich (0.9-1.9 wt.%) aromatic source, and a low- sulfur (<0.2 wt.%) paraffinic crude source121, To satisfy the growing demand for diesel fuel, increased use of cracked stocks is anticipated. The primary requirement in diesel oil properties is that it should burn smoothly, without exploding, under the condition existing in the combustion chamber, so that maximum amount of useful energy is liberated. The ignition quality of a diesel oil is measured by its cetane number, which depends on its hydrocarbon composition. Different refineries produce diesel oil of different compositions, depending on the blending components available. Hydrocarbon compositions of the gas oil components show marked variation in their precombustion and ignition characteristics and so differ in their combustion behavior in an engine. Such a selective hydrocracking process has the following reaction: desulfurization, denitrogenation, deoxygenation, saturation and isomerization which could improve the flowing properties of gas oil components: sulfur, nitrogen, polycyclic aromatics and total aromatics, product stability, colour, neutralization number and distillation temperature (T50 and T90). The properties of the straight-run and cracked gas oil components, and improving their quality by a hydrotreating process to meet the clean diesel oil specification and production of gas oil components in Indonesia's refineries are described. A brief deliberation is offered on the impact of the changing diesel oil quality requirement, particularly due to the environmental restriction, on the refinery configuration.
PRODUCTION OF ENVIRONMENTAL FRIENDLY FUEL IN INDONESIAN REFINERY A.S. Nasution; Oberlin Sidjabat; Abdul Gafar; Rasdinal Ibrahim; Morina Morina
Scientific Contributions Oil and Gas Vol 28 No 2 (2005)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.28.2.1039

Abstract

Worldwide crude supplies are experiencing a mod- est trend toward heavier and high sulfur content. The average annual demand growth rate for light products (gasoline, kerosene and diesel oil) is higher than that for residual fuel oil, Therefore, converting additional bot- toms into light product by either thermal or catalytic pro- cesses will be needed. Vehicles and fuels have been developed simulta- neously and nowadays vehicles demand a very sophisti- cated fuel indeed. Environmental restriction, and efforts to minimize the pollutant problem by exhaust gases are causing design and changes in cars that in turn are hav- ing some effects on fuel quality. To reduce exhaust emission by fuel combustion, the specification of gasoline and diesel oil is now stricter. Various term in the models address qualities of the re- formulated gasoline, such as benzene, total aromatics and olefin content, RVP, the T of distillation range, sul- fur content, and oxygenate contents (Table 1)18.13.16). Diesel oil specification is limited as follows: aromatics, polyaromatics, sulfur content, T and cetane number (Table 2) (19.23,26) To improve the specification of commercial gasoline into the stricter specification of reformulated gasoline, refiners are forced in install new facilities to increase the production for high-octane mogas components. For the stricter diesel oil specification in the years 2000's, over 50% by volume of the total gas oil components (ex- cept hydrocracked gas oil) must undergo improvement by hydrotreating processes in order to achieve a suitable specification. In Indonesia, there are seven refineries with total crude oil capacity of 1,063 MBCD to produce fuel oils, lube base stocks and petrochemical products. Process- ing units and fuel oil production in Indonesia's refineries are given in Table 3 and 4, respectively. The production of gasoline and diesel oil components is review in this paper. Influence of hydrocarbon composition of those fuel components on their performances is discussed. A brief discussion is offered on the impact of the changing specification of gasoline and diesel oil on the refinery configuration.
THE MANAGEMENT OF SPENT CATALYST IN RCC/FCC UNITS IN ASEAN REFINERIES A.S. Nasution; E. Jasjfi
Scientific Contributions Oil and Gas Vol 28 No 3 (2005)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.28.3.1041

Abstract

Catalytic cracking processes convert heavy feed- stock (heavy distillate, residue) into gasoline and light cycle stock for middle distillate components. Due to high impurity of feedstock and limited operating condition of catalyst regeneration, fresh catalyst must be added to replace a portion of spent catalyst continously, to maintain the activity of equilibrium catalyst in the reactor. Spent catalyst must be disposed properly so that it does not cause hazard or environmental concern. A survey was conducted on the management of spent catalyst in RCC/FCC unit in ASEAN refineries as an ASCOPE Technical Committee work programme for 1996. Indonesia was tasked as the Coordinator with the support of Member Countries. The Coordinator for each Member Country is listed in the Table 1. This paper discusses briefly catalytic cracking process, deactivation of cracking catalyst and the management of spent cata- lyst in RCC/FCC units 
ROLE OF CATALYTIC REFORMING PROCESS FOR GASOLINE PRODUCTION IN ASEAN REFINERIES A.S. Nasution; E. Jasjfi
Scientific Contributions Oil and Gas Vol 28 No 3 (2005)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.28.3.1044

Abstract

The crude oils processed in refineries range from sweet crudes, such as Southeast Asian light Crudes, to sour crude, suck as Middle East. Far East, and Persian Gulf. For the period 1992-2005, the average annual demand growth rate for light products (gasoline, kerosene, diesel oil) is higher than residual fuel oil. These data clearly show that the need will continue for converting additional bottom into light products, by both thermal or catalytic conversions, The passage of the Clean Air Act Amendement of 1990 in the USA has forced American refineries to install new facilities to comply with stricter specifications for fuels such as gasoline and diesel oil such as Asia-Pacific, California Air Resources Board (CARB) and European Commission (EC), Various terms in the models address qualities of the gasoline blended such as benzene, total aromatics and olefm contents, RVP, the T90 of distillation range, sulphur content, and oxygenates content45, Motor gasoline is essentially a complex mixture of hydrocarbons distilling about 40°C and 220°C and consisting of compounds generally in the range C, to C2. Gasoline components can be produced by both the distillation of crude oil and the conversion of the crude oil fraction. Catalytic reforming process using bifunctional catalyst converts low octane number heavy naphthas into reformate with a high octane number. Bi-functional catalyst containing metal site (Pt, Pt/Ge) and acid site (A1,O,CI) are generally used. The balance is most important in a bifunctional reforming catalyst, and in fact it has to be different for different duties"l The end point of the naphtha feedstock is usually limited to about 185°C, partially because of increased coke deposition on the catalyst. The reforming cata- lyst exhibits a sensitivity to the conventional impurities of naphtha feed, such as: water (moisture), organic compounds of chlor, nitrogen and sulphur, and organometallic compounds (lead, copper, iron). Sintering of the metal phase becomes effective only beyond 500°C as measured by lowering of the dispersion of platinum atom condition, at the same time coke formation on the catalyst incrases tool71, The life of the catalyst will depend both on its stability and regenerability, expressed either in months or year, or in tonnage treated for unit weight of catalyst. This paper presents briefly composition of gasoline pool, specification of commercial gasoline in Indonesia as well as ASEAN refmeries, the catalyst improvements, catalyst deactivation and catalyst re- generation of the reforming process.
INFLUENCE OF HYDROCARBON COMPOSITION OF NAPHTHA FEED ON THE YIELD AND OCTANE NUMBER OF REFORMATE A.S. Nasution
Scientific Contributions Oil and Gas Vol 27 No 1 (2004)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.27.1.1045

Abstract

The rapidly increasing demand for high octane num- ber gasoline and aromatic hydrocarbon as a petrochemical feedstock has promoted refiners to seek methods of improving yields of these valuable products. The purpose of catalytic reforming is to convert a low-octane distillate fraction boiling within the gasoline range into high-octane blending stock and low aromatic hydrocarbons. The increase in the octane number of low-octane naphtha reformer feed can therefore be regardel as the transformation of naphthenes and paraffins into aromatics; resulting in the highest octane improvement. Paraffin and C,ring naphthene aromatization are guided by the metal and acid sites of bifunctional reforming catalyst. In order to obtain more information about the influence of hydrocarbon composition of naphtha reformer feed on the yield and research octane number of reformate, an experiment has been carried out to study the conversion of pure hydrocarbon (ie cyclohexane, methylcyclopentane and n.hexane); and naphthenes, and peraffins of three types of naphtha feeds with various hydrocarbon compositions using bifunctional reforming catalyst. The operating conditions: temperatures: 400 to 500 C, pressure: 10 to 30 bars and H/HC ratio = 8 mole/mole. A Catatest Unit operated in a continuous system was used in this experiment. Gas and liquid product samplers taken from gas and liquid samplers, respectively, were analyzed for their hydrocarbon using a Gas Liquid Chromatography.
THE MANAGEMENT OF SPENT CATALYST OF HYDROCONVERSION PROCESSES IN ASEAN REFINERIES A.S. Nasution; E. Jasjfi
Scientific Contributions Oil and Gas Vol 27 No 2 (2004)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.27.2.1052

Abstract

Catalytic processing is a keystone of today’s petroleum refining. The catalytic processes applied in the potreleum industry are generally large scale. In today’s operating climate of increased attentiveness toward environmental and safety issues, spent catalyst management options have became an important consideration for refiners. A catalyst deactivation determines how it can be handled after it is discharged from the processing unit. The type of the catalyst and its condition (whether it is considered hazardous) often determines the disposal route selected. Because of the self-heating and leaching problems associated with spent hydrotreating catalyst,it is recommended that refiners ship their spent catalysts to what is called “true recycles”. The U.S. Environmental Protection Agency (EPA), for example, is in the process of reevaluating the designation of spent hydroprocessing catalyst as an hazardous waste. Out of 3,837 MBPSD total crude oil currently processed in ASEAN (Brunai Darussalam, Indonesia, Malaysia, Philippenes, Singapore, Thailand, not including Vietnam, Laos and Myanmar) arround 61 percent volume is passed through catalytic processes (included hydroconversion processes 58 vol.%) to produce various fuel components such as gasoline and diesel oil. These hydroconversion processes use about 3,279 tons of catalyst with about 28 tons per day of spent catalyst. The present paper discusses briefly a survey on the management of spent catalyst of hydroconverion processes in ASEAN refineries and some aspects of catalyst poisoning of major hydroconversion processes in petroleum refinery. A survey on the management of spent catalyst from hydroconversion processes in ASEAN refineries is described in this paper.
INFLUENCE OF THIOPENE ON THE CONVERSION OF METHYL-CYCLOPENTANE AND N.HEXANE TO BENZENE USING MONO-AND BI-METALLIC REFORMING CATALYSTS A.S. Nasution
Scientific Contributions Oil and Gas Vol 27 No 3 (2004)
Publisher : Testing Center for Oil and Gas LEMIGAS

Show Abstract | Download Original | Original Source | Check in Google Scholar | DOI: 10.29017/SCOG.27.3.1058

Abstract

Parrafin and naphthene hydrocarbons are usually the major component in the naptha reforming feedstock. Thus the conversion of these hydrocarbon to high octane motor gasoline and aromatic hydrocarbon is one of the important reactions of the catalytic reforming process, (Montamal., 1965). And aromatization reaction is guided by both metal and acid sites of bi-functional reforming catalyst (Hobson 1973).
Co-Authors Abdul Gafar Chairil Anwar E. Jasjfi Evita H. Legowo Morina Morina Oberlin Sidjabat Rasdinal Ibrahim