Science.gov (United States)

... closely correlated to the amount of re- centration. The molar extinction coefficients were agent added to the enzyme. The naphtha- ...

Energy Technology Data Exchange (ETDEWEB)

This document demonstrates the commercial status of the process units to be used in the Tri-State Synfuels Project at Henderson, Kentucky. The basic design philosophy as established in October, 1979, was to use the commercial SASOL II/III plants as a basis. This was changed in January 1982 to a plant configuration to produce gasoline via a methanol and methanol to gasoline process. To accomplish this change the Synthol, Oil workup and Chemical Workup Units were eliminated and replaced by Methanol Synthesis and Methanol to Gasoline Units. Certain other changes to optimize the Lurgi liquids processing eliminated the Tar Distillation and Naphtha Hydrotreater Units which were replaced by the Partial Oxidation Unit. The coals to be gasified are moderately caking which necessitates the installation of stirring mechanism in the Lurgi Dry Bottom gasifier. This work is in the demonstration phase. Process licenses either have been obtained or must be obtained for a number of ...

Energy Technology Data Exchange (ETDEWEB)

A preliminary assessment of the future refining impacts of the Clean Air Act Amendments of 1990 has been performed with the Navy Mobility Fuels Forecasting Systems. The assessment suggests that gasoline reformulation costs in domestic coastal and near-coastal refining regions in the year 2000 could be 3.5 to 5.6 cents per gallon (in terms of 1989 currency). For heating value equivalent to one gallon of conventional gasoline, the regional total added costs (including reformulation costs) for reformulated gasoline could be 5.9 to 8.0 cents. In blending reformulated gasolines, the reduction of butane for lower Reid vapor pressure and the reduction of reformate for lower aromatics are generally compensated by increased percentages of alkylate and/or straight run naphthas. Relatively larger refinery process capacity additions are required for butane isomerization, alkylation, aromatics recovery, and distillate hydrotreating. 21 refs., 3 figs., 18 tabs.

Energy Technology Data Exchange (ETDEWEB)

The scope of the present study was upgrading a set of heavy aromatic hydrocarbons mixtures whose commercial value ranks close to fuel oil and should become even lower in the next future because of the introduction of more stringent regulations on fuels, through hydro-conversion to a synthetic feed for steam-cracking. The resulting process provides an opportunity to improve the economic return of a steamcracking plant, offering the chance of converting low-value mixtures produced by the plant itself, such as fuel oil of cracking (FOK), saving an equivalent amount of naphtha. The method can also be used for converting pyrolysis gasoline (pygas). Although pygas has at present a fair commercial value, it could suffer a significant penalization in the future due to further limitations on total aromatic content in gasoline. Pygas hydro-conversion to a synthetic steam-cracking feedstock has been recently reported. Fractions from refinery, such as heavy distillates (e.g. ...