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Technical View
Published in Eberhard Lucke, Edgar Amaro Ronces, Leveraging Synergies Between Refining and Petrochemical Processes, 2020
Eberhard Lucke, Edgar Amaro Ronces
The numbers in Table 4.1 represent an example for a high complexity conversion refinery with a fluid catalytic cracker and a CCR for gasoline production, a hydrocracker for diesel production, and a visbreaker/delayed coker section for residue cracking and asphalt production. For clarification, all energy coming from the refinery utilities such as steam or cooling electricity has been assigned to each process unit based on its consumption of the respective energy form. Consequently, reduction in energy consumption in one or several process units will impact the overall load of the utility units and may reduce their efficiency. For example, if steam consumption is reduced drastically and goes past the minimum load point at which the steam boiler can be operated, it will most likely keep operating at its safe minimum load and excess steam will be vented to the atmosphere. This is an extreme example, but it highlights the need to evaluate and optimize the energy system as a whole and look at every aspect of the energy networks within the refinery or integrated complex.
Introduction to Refining Processes
Published in James G. Speight, Refinery Feedstocks, 2020
A solvent deasphalting unit processes the residuum from the vacuum distillation unit and produces DAO, used as feedstock for a fluid catalytic cracking unit, and the asphaltic residue (deasphalter tar, deasphalter bottoms) which, as a residual fraction, can only be used to produce asphalt or as a blend stock or visbreaker feedstock for low-grade fuel oil (Parkash, 2003; Gary et al., 2007; Speight, 2014; Hsu and Robinson, 2017; Speight, 2017). Solvent deasphalting processes have not realized their maximum potential. With on-going improvements in energy efficiency, such processes would display its effects in a combination with other processes. Solvent deasphalting allows removal of sulfur and nitrogen compounds as well as metallic constituents by balancing yield with the desired feedstock properties (Ditman, 1973).
Basic Principles of Catalytic Reforming Processes
Published in Soni O. Oyekan, Catalytic Naphtha Reforming Process, 2018
In summary, it is appropriate to emphasize that naphthas vary with respect to the crude oils from which they are derived. Naphthas also vary greatly with respect to the downstream processing units such as a coking, visbreaker, or cracking unit that produced them. These factors are clearly highlighted by the data in Table 4.8, which compare the properties of naphthas from a hydrocracker unit and from Mid Continent and light Arabian crude oils. As shown in Table 4.8, the naphtha from light Arabian crude oil is highly paraffinic, with N+2A quality of 33, and those of the hydrocracker and Mid Continent crude oil are greater than 60. In addition, the octane numbers of the hydrocracker and Mid Continent naphthas are 62 and 55, respectively, and that of the Light Arabian naphtha is 33.
Exergy cost accounting thermoeconomic analysis of an oil refinery operating at off-design conditions
Published in Energy Sources, Part A: Recovery, Utilization, and Environmental Effects, 2023
Morteza Khosravirad, Amir Heydarinasab, Fatemeh Joda, Seyed Abolhassan Alavi
An oil refinery, with a capacity of 250,000 barrels per day is considered in this study. Figure 2 shows the main streams in and out of the refinery. As shown, the refinery products are LPG, gasoline, jet fuel, ATK1 solvent, kerosene, diesel, fuel oil, lube cut, and asphalt. The main units of the refinery are: CDU, VDU, Kerosene treating (Desulfurization) unit, Isomerization unit, Visbreaker unit, Naphta unifier & Platformer Unit (CRU), LPG treating, Isomax Reactor (Hydrocracking Process) unit, Hydrogen plant unit, Nitrogen generation unit, H2S removal-sulfur recover unit, blending units (which are Gasoline blending, Jet fuel blending, Kerosene blending, Diesel blending, and fuel oil blending unit), and Utility generator unit. Additional refinery information is provided in the supplementary file.
Residence time distribution studies using radiotracers in chemical industry—A review
Published in Chemical Engineering Communications, 2018
Meenakshi Sheoran, Avinash Chandra, Haripada Bhunia, Pramod K. Bajpai, Harish J. Pant
The RTD of soaker and visbreaker unit of a petroleum refinery was measured using 82Br as radiotracer (Sharma et al., 2016). The study was performed at very high temperature (430°C) and pressure (≈11 kg/cm2) which was not possible using conventional tracers. The system consisted of three sections, i.e., feed section, furnace section, and the product recovery section. The feed is preheated in the feed section and pumped to the furnace for further heating. The outlet of the furnace was connected to the soaker where cracking took place and different fractions of hydrocarbon of hydrocarbons were produced. Ten radiotracer experiments were performed successfully using short residue and vacuum gas oil as feed at different operating conditions.
Functional influence of depressor and depressor-dispersant additives on marine fuels and their distillates components
Published in Petroleum Science and Technology, 2018
Natalia K. Kondrasheva, Viacheslav A. Rudko, Dmitrey O. Kondrashev, Rostislav R. Konoplin, Ksenia I. Smyshlyaeva, Viktoria S. Shakleina
As analyzed components for marine fuel blending the following products of the industrial oil refinery plant were used: hydrotreated straight-run diesel fraction (HSRDF), hydrocreaking diesel fuel with extra low sulfur (ULHDF), light heavy gas oil delayed coking (LGODC and HGODC), light vacuum gas oil (LVGO) and visbreaker residue. The physical and chemical performance requirements of the selected compounds are presented in Table 1.