Kerosene feedstock

Comparable data for the pyrolysis of kerosene feedstocks are shown in Figure 2, Again the yields and selectivities of the products are in excellent agreement. 

In a single stage with liquid recycle, total conversion to products lighter than the feedstock is possible. The yield of kerosene plus diesel is between 70 and 73 weight %. 

Gas oil is a product hoiling slightly higher (235—425°C, or sometimes wider) than kerosene. The main feedstock to the catalytic cracking units (see Feedstocks), it received its name from use as an enriching agent in the production of city or manufactured gas. It is often used as diesel fuel. 

LAB is derived exclusively from petroleum- or natural gas-based feedstocks. Thus, it is referred to as a petrochemical (or synthetic) surfactant intermediate. Feedstocks for LAB production are generally paraffins (carbon chain length in the range of C8-C14) derived from kerosene and benzene. Internal olefins derived from ethylene are sometimes used in place of paraffins. 

In 1979, China produced approximately 106 million metric tons of oil (ranked ninth in the world) equivalent to approximately two million barrels a day. Of the total oil produced, China exported about 10 million metric tons. Assuming that China consumes 10% of its naphtha and kerosene domestically as feedstock, she should have been able to produce a theoretical maximum of 2.5 million tons of ethylene for 1979. Given the forecasted production figure of 170 million tons of oil in 1985, and if the allocation of oil for feedstock is increased to 15%, China should be able to produce a maximum of 3.6 million tons of ethylene. 

Petroleum is rarely used in the form produced at the well, but is converted in refineries into a wide range of products, such as gasoline, kerosene, diesel fuel, jet fuel, and domestic and industrial fuel oils, together with petrochemical feedstocks such as ethylene, propylene, butene, butadiene, and isoprene. Petroleum is refined, that is, it is separated into useful products (Figure 1.1 Chapter 3). 

This chapter reviews the adsorptive separations of various classes of non-aromatic hydrocarbons. It covers three different normal paraffin molecular weight separations from feedstocks that range from naphtha to kerosene, the separation of mono-methyl paraffins from kerosene and the separation of mono-olefins both from a mixed C4 stream and from a kerosene stream. In addition, we also review the separation of olefins from a C10-16 stream and review simple carbohydrate separations and various acid separations. 

The MMP Sorbex process has many similarities but also some differences when compared to the detergent Molex process. As with all of Sorbex processes, the MMP Sorbex process operates in the Uquid phase, employing suitable conditions (pressure, temperature) to overcome any diffusion constraints to achieve target performance. Table 8.4 highlights and contrasts the different characteristics of the detergent Molex and MMP Sorbex processes. The process was successfully demonstrated in a continuous countercurrent moving bed separation pilot plant using commercial n-paraffin-depleted kerosene (Molex raffinate) feedstock. A typical gas... 

Petroleum and Petrochemical Processes. I he first large-scale application of extraction was ihe removal of aromatics From kerosene to improve its burning properties. Solvent extraction is also extensively used to meet ihe growing demand for the high purity aromatics such as benzene, toluene, and xylene (BTXl as feedstocks for the petrochemical industry. Additionally, Ihe separation of aromatics from aliphaties is one of the largesi applications of solvent extraclion. 

In newer RDS applications the hydroprocessing unit is an integral part of the overall crude oil upgrading scheme to produce transportation fuels such as gasoline and kerosene. The RDS unit may operate independently of, or in combination with, other refinery conversion units, depending on the particular feedstock and product demand (Howell et al., 1985 Siewert etal., 1985). Hydroprocessing requirements and catalyst requirements are dictated by the processing route chosen. 

However, there are more chances of localized heating in the catalyst bed and (in addition to the more expensive reactor design per unit volume of catalyst bed) it may be more difficult to remove contaminants from the bed as part of the catalyst regeneration sequence. For this reason alone, it is preferable that this type of reactor is limited to hydrodesulfurization of low-boiling feedstocks such as naphtha and kerosene and application to the higher-boiling heavy oils and residua is usually not recommended. 

Distillation was the first method by which petroleum was refined, but this was not so much a refining method as a method for separation of the crude oil into fractions, such as kerosene, for which there was a demand and hence a ready market. Nevertheless, as petroleum refineries have evolved into present-day complexes, distillation units may still find a place, depending upon the characteristics of the crude oil feedstock, in a refinery sequence. A multitude of separations is accomplished by distillation, but its most important and primary function in the refinery is its use for the separation of crude oil into component fractions (Table 7-2) (Speight, 1999). 

The major goal of hydroconversion is the cracking of residua with desulfurization, metal removal, denitrogenation, and asphaltene conversion. The residuum hydroconversion process offers production of kerosene and gas oil, and production of feedstocks for hydrocracking, fluid catalytic cracking, and petrochemical applications. 

The purpose of hydrofining reactions may vary with the feedstock. Gasolines or coke-oven light oil are treated to remove gum formers, that is, readily polymerizing olefins and sulfur compounds, while hydrogenation of aromatics must be avoided. Hydrogenation of kerosenes and Diesel... 

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