Existing refinery

Practice is quite different. The main reason for the current rapid growth of biomass conversion systems is the feasibility of using existing refinery systems and installed secondary energy systems. 

Thus, the Clean Air Act Amendments of 1990 aimed to encourage voluntary reductions above the regulatory requirements by allowing facilities to obtain emission credits for voluntary reductions in emissions. These credits would serve as offsets against any potential future facility modifications, resulting in an increase in emissions. Other regulations established by the amendments, however, will require the construction of major new units within existing refineries to produce... 

This example illustrates the performance of the proposed approach on a single site total refinery planning problem. The refinery scale, capacity and configuration mimic an existing refinery in the Middle East. Figure 7.1 is a state equipment network (SEN)... 

Both of these processes direct the SO2 absorbed from the FCCU flue gas to the refinery SRU, where it is converted to elemental sulfur and added to the marketable sulfur that is generated by the SRU from H2S. Alternately, the SO2 can be converted to sulfuric acid in a dedicated sulfuric acid plant, or in combination with an existing refinery spent acid regeneration unit. When the SO2 is directed to the SRU, 1 ton of SO2 captured in the scrubber is converted to 0.5 tons of marketable elemental sulfur and less than 0.1 ton of sodium sulfate waste is generated per ton of SO2 absorbed. In an acid plant, 1 ton of SO2 generates 1.5 tons of 98% sulfuric acid. Steam is also generated from the conversion of SO2 in both the SRU and the acid plant, which moderates somewhat the steam consumption rate of the solvent regenerator for both the LABSORB and CANSOLV systems. 

Offsite costs for the addition of individual process units in an existing refinery can be assumed to be about 15 to 20% of the process unit costs. Items considered to be offsites in this work are as follows ... 

The results of this study are, therefore, quite encouraging. Shale oil appears to be an attractive feed for processing in existing refineries that have appropriate hydrotreating facilities. 

Zeolites are widely used in acidic processes and they are an obvious catalyst choice. The suitability of commercial cracking catalysts to degrade polymer waste is vital as one of the options of commercializing this polymer recychng method is to co-feed polymer waste to existing refinery crackers [13]. Furthermore, in the search for cheaper catalysts, clays and their pillared analogues are also introduced in the polymer catalytic degradation [16, 17]. 

Generally, past practice has called for evaluating certain portions of the above liquids in existing refinery streams. This led to problems and did not allow for a detailed and comprehensive study of the very nature of the synthetic liquids. A primary purpose of this project was to attempt to define the operable, physical, and chemical nature of the liquids from coal and shale liquefaction, per se, and then contrast and compare with results from processing standard petroleum streams. 

The ultimate refinery configuration would approach that of the foreign refinery. Existing refineries would probably find it advantageous to expand the crude fractionation sections and redistribute product streams to conversion units. The expected result would be a decreased per cent conversion for the total crude oil feedstock. 

In general, the important factors governing the supply of a petroleum raw material are the (1) composition and cost of the raw material, (2) quantity and quality of the hydrocarbon desired, and (3) processing steps required and their relation to existing refinery operations. 

Compared to SMDS, this simplified process employs a different catalyst in the synthesis stage and does not include a Heavy Paraffinic Conversion stage for producing the finished middle distillate fractions. The syncrude product is a broad boiling range of hydrocarbons (Table 4), and the relative amounts of individual products can be varied by adjusting the reaction conditions. Alternatively, syncrude products can be processed in existing refineries into finished transportation fuels. 

Transportation. Pipelining the product out, for example, to existing refineries, might offer cost savings. 

Rebalancing of new and existing refinery process capacity to regard shale oil as a primary feed rather than a contaminant - analogous to shifting from a sweet crude refinery to a sour crude refinery - with a corresponding shift of product slate (consistent with overall market demand) to best exploit the different optimum product mixes from shale oil and petroleum. 

Several petrochemical companies have considered the possible feedstock recycling of plastic wastes in existing refinery facilities, which would avoid the need to invest and build new processing plants.19-21 This alternative is based on the similarity of elementary composition between plastics and petroleum fractions. Moreover, taking into account the differences in production between plastics and the total of petroleum-derived products, plastic wastes could be incorpo-... 

In this chapter we will discuss a number of commercial lube plants whose purpose is to make base stocks by hydrocracking and whose design basis has been outlined in papers from either the company that developed the specific technology or by a licensee. In the case of a licensee, the technology would have been adapted (and developed) as needed to meet that company s circumstances, including capital available, feedstocks and their qualities, existing refinery infrastructure, and eventual product marketplace. 

The following example hows the economic calculations required to justify a CO boiler. It will be assumed that no additional steam is needed. The boiler is to share the existing refinery steam load. 

An existing refinery cooling water system was to be expanded. There was a choice between once-through and re-use water, but the selection affected process cooler design and process operating conditions. An itemized check list was made to assist in the choice between the two cooling water systems. 

Secondly, it is important to note that requiring pool octane numbers above 96 RON at 0.15 gram lead/litre and above 93 RON for unleaded fuels would touch on the limits of technology for some existing refinery configurations. 

In the case it was assumed that the existing refinery facilities were fully utilized. Crude slates and product packages were those actually existing in each individual refinery. In the variable cases the output of all products was kept constant... 

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