Gasoil feed

Figure 16.7 Influence of support type on product distribution in hydrocracking hydrotreated light Arabian gasoil feed hydrocracked over amorphous and high zeolite catalysts differential yields measured in 50°F (10°C) increments.

The experiments were carried out in a fixed-bed tubular reactor, heated by an electric furnace divided into three heating zones. Prior to each experiment the catalyst was stripped with N2 at 482°C (reaction temperature) for 20 minutes. Then the reactant (which characteristics are given in Table II) was charged at the top of the reactor by a constant-rate positive-displacement pump. The catalyst to oil ratio with respect to the zeolite content was varied between 0.09 and 0.23 g.g 1 by changing gasoil feed (4.45-1.78 g) while keeping the weight of zeolite constant (0.40 g). 

Feedstocks For either gaseous (ethane/propane) or liquid (C4/naphtha/ gasoil) feeds, this technology is based on Technip s proprietary Pyrolysis Furnaces and progressive separation. This method allows producing olefins at low energy consumption with particularly low environmental impact. 

Fig. 8. Classes of model components in aromatic fractions of gasoil feeds.

As already mentioned in the description of a fluid catalytic cracker the circulation rate of solids is determined by the heat balance between the reactor and the regenerator. Equating heat inputs and outputs over the reactor leads to the following ratio for the circulation rate between the reactor and the regenerator, m/kg/hr) and the gasoil feed rate,... 

Figure 3-6 illustrates how one combination tower was retrofitted to increase the pumparound draw temperature by 45°F. The heavy coker gasoil feed to the steam stripper was modified to be withdrawn from the tower in two streams. The 3,100 B/D of relatively light, cool gas oil was trapped out and drawn off the tower before it could fall into the pumparound section. Computer calculations predicted that segregating this lighter gas-oil cut from the pumparound section would increase both the pumparound draw and return temperatures, with only a 3% reduction in pumparound heat duty. 

Feed oils. Crude from the Wilmington oil field in California was distilled into four fractions of vacuum gasoil boiling between 360-502 (No. ), 381- 96 (No. 5), (No. 6) and 83-73% off at 5 80C (No. 7). 

From an FCC viewpoint, there is not a clear definition of resid cracking. If we consider the overall refinery scheme, all materials not qualifying for gas oil type specifications are resid, which in fact means that the traditional FCC feed, Vacuum Gasoil (VGO), is nearly 100% resid, or to be more specific a fuel oil. 

The temperature in the regenerator is conventionally controlled by the flowrate of air from the blower. However, many catalytic cracking units run at maximum airflow as limited by the air blower. In this situation catalyst cooling rates in the regenerator can be used to hold regenerator temperature. However, if air is at a maximum constraint, the amount of coke that can be burned is limited. Therefore, feed flowrate may have to be reduced or feed composition altered (feed more light gasoil and less heavy material). 

Feed vacuum gasoil. Radiotracer " C-labelled dotriacontane. 

Diluent in microflow test Silicon carbide, d = 0.05 mm. Feed Middle East heavy gasoil, 1.64 %w S.Operating conditions WHSV, WABT, hydrogen/oil ratio, partial pressures of hydrogen and hydrogen sulfide same in commercial and microflow reactor. 

Feed and catalysts. A regular Kuwait vacuum gasoil was used as a feed. Its characteristics can be found in Table II. Three commercial cracking catalysts with an increasing rare earth and alumina content, viz. A, B, and C, were tested. All catalyst were presteamed and deactivated to an equilibrium level by its supplier. Larger catalyst particles were removed with a 150 pm sieve. This step is followed by either a calcination or regeneration. Fresh, but pre-steamed catalyst was calcined at 773 K for 1 h, while coked catalyst was regenerated at 873 K for 2 h. 

In the case of kerosene and light gasoil also, density, TBP or ASTM D86 distillation curves and PINA analysis (if available) are used, and empirical correlations are derived to yield a detailed picture of hydrocarbon mixture composition. The aromatic fraction can vary greatly for the different feeds, and information, such as the H/C of the feed, is important when PINA is not available. 

Feedstocks Ethane, propane through liquid feeds up to heavy gasoil or up to 600°C EP. 

The DCC has two reactor operating modes DCC-I (Riser-plus fluidized dense-bed reactor, maximum propylene mode) and DCC-II (Riser reactor, maximum iso-olefins mode). The DCC can process different heavy feeds— VGO, DAO, coker gasoil, atmospheric residue, VR, etc. Paraffinic feedstocks are the best feeds for DCC. In DCC maximum propylene operation mode, over 20 wt% propylene yield can be obtained from paraffinic feedstocks. The naphtha and middle distillates streams from the DCC unit can be used as blending components for high-octane, commercial gasoline and fuel oil, respectively. 

Application GT-Styrene is an extractive distillation process that directly recovers styrene from the raw pyrolysis gasoline derived from the steam cracking of naphtha, gasoils and natural gas liquids (NGLs). The produced styrene is high purity and suitable for polymerization at a very attractive cost compared to conventional styrene production routes. The process is economically attractive for pygas feeds containing more than 15,000 tpy of styrene. 

Feeding PCs with conventional fuels such as coal, gasoil, gasoline, methanol or natural gas seems appropriate for stationary energy generation plants, to which a CCS technology can be added. For vehicle onboard PC applications, Plj is the adequate energy carrier. 

Mixing ofhot catalyst (from r enerator) and feed (vacuum gasoil)... 

D Eulerian-Eulerian simulation of fluid catalytic cracking of gas oil. Snapshot of fluctuations around the statistically stationary species field. Mass fraction in the gas phase (a) gasoil fraction of the feed, (b) gasoline fraction in the product, (c) Transient calculation of the meso-scale fluctuations around a statistically stationary state solids volume fraction and axial velocity at 0.1 m from the wall and 0.25 m from the bottom. 

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