Synthoil liquid

Feedstocks. The Raw Anthracene Oil was obtained from the Reilly Tar and Chemical Corporation, and the Synthoil liquid from the Pittsburgh Energy Research Center. The properties of these two liquids are given in Table I. The feedstocks were used as received from suppliers without pretreatment. As is clear... 

Figure 6. HDS and HDN responses to the change in the volume hourly space time, synthoil liquid, 1500 psig, 371° C (700° F) (A) Monolith catalyst, (O)...

The precision of sulfur and nitrogen analyses was determined by multiple analysis of Raw Anthracene Oil and Synthoil liquid. The results of sulfur analysis of Raw Anthracene Oil were found to be precise within 0.25%. But the precision of other results was within 5.0%. 

Figures 5 and 7 indicate that on the volume and weight bases, the activity of the monolith catalyst when tested on Raw Anthracene Oil was less than that of Nalcomo 474 catalyst. On the other hand, Figures 6 and 8 show that when tested on Synthoil liquid, the desulfurization activities of the two catalysts were approximately the same on a volume basis, whereas on a weight basis, the Monolith catalyst was more effective. The denitro-genation activity of Nalcomo 474 was somewhat better even on this feedstock.

Figure 10 shows the comparison of the surface activities of the two catalysts on the heavier feedstock, Synthoil liquid. In this case the unit surface area activity of the Monolith catalyst is greater than that of the Nalcomo 474 catalyst. This behavior is different from that observed on the Raw Anthracene Oil, and as further discussion will show, this difference in the superiorities of the Monolith catalyst on the two feedstocks throws light on some interesting observations of this study. 

If one considers that the Monolith catalyst was intrinsically more active than the Nalcomo 474 catalyst then the observed superiority of the Monolith catalyst should be essentially the same, or at least be comparable, when tested on two different feeds. But as explained earlier the observed surface activities of the two catalysts for HDS are almost equal in the case of Raw Anthracene Oil, while, on Synthoil liquid the observed surface activity of the Monolith is about four times that of the Nalcomo 474 catalyst. Therefore, there is some basis to... 

Thus intraparticle diffusion was likely responsible for showing higher activity, on unit surface area basis, of the Monolith catalyst when processing the Synthoil liquid. 

To have a quantitative idea of the problem of intraparticle diffusion, effectiveness factors for the two catalysts were calculated from the observed second order rate constants (based on surface area) using the "triangle method" suggested by Saterfield (4). The effectiveness factors for Monolith and Nalcomo 474 catalysts on Synthoil liquid at 371°C (700 F) were calculated to be 0.94 and 0.216, respectively. In applying the relationship between the "Thiele Modulus," 4>> and the "effectiveness factor," n> the following simplifying assumptions were made ... 

The effectiveness factors calculated in this study are under the experimental conditions utilized in this study and give an idea of the magnitude of pore diffusion problem in the case of the Nalcomo 474 catalyst when Synthoil liquid is processed. On the other hand, the Monolith catalyst shows promise in this regard and warrants further investigation regarding its activity under different compositions of the catalyst and different reactor operating conditions. 

The hydrodesulfurization (HDS) and hydrodenitrogenation (HDN) activities of two Co-Mo-alumina catalysts were tested on two coal derived liquids using a trickle bed reactor system. The two liquids used were Synthoil liquid (high-boiling stock) and Raw Anthracene Oil (low-boiling stock). One of the two catalysts was prepared in the laboratory at Oklahoma State University by... 

Figure 4 HDS and HDN reaction extent as a function of surface area/volumetric rate of oil 643 K, 10.2 MPa. (a) Anthracene oil (b) Synthoil liquid, o pellets, A monolith. (From Ref. 25.)...

Raw anthracene oil COED filtered oil synthoil liquid 3.4-10 589-700 C0M0/AI2O3 (presulfided) Ahmed and Crynes (59)... 

Coal Products Isotopic Distribution by Structural Position. Other workers have also investigated deuterium uptake in coal pro-ducts by structural position. Schweighardt, et al. (26) examined a centrifuged liquid product from a Synthoil run which was heated to 450°C with deuterium gas, Kershaw and Barrass (27) examined the products from the reaction of coal with deuterium gas using SnCl2 as catalyst, and Franz (10) examined the products from the reaction of a subbituminous coal with Tetralin-1,l-d2 at 427°C and 500°C. 

Figure 6. SEC of coal liquids using the SEC-GC interface online (Figure 2). Fraction collection timing is similar to one used for Wyodak (Figure k) except for Western Kentucky Synthoil where 2M fractions were collected.

In the Energy Research and Development Administration s SYNTHOIL process, slurries of coal in recycle oil are hydrotreated on Co-Mo/Si02 Al203 catalyst in turbulent flow, packed-bed reactors. The reaction is conducted at 2,000 to 4,000 psi and about 450° C under which conditions coal is converted to low-sulfur liquid hydrocarbons and sulfur is eliminated as E2S. 

The objective of this work was to study the activity of the Monolith catalyst for removing sulfur and nitrogen from a Synthoil process liquid (heavy stock) and Raw Anthracene Oil (light feedstock), and to make a preliminary assessment of the advantages and/or disadvantages of the Monolith catalyst over a commercial catalyst used in the petroleum industry. 

Proposed methods for predicting heats of formation and absolute entropies are tested on two fractions of synthetic crude oil obtained by the EDS process, one sample of H-Coal, one sample of Synthoil, two samples of Solvent Refined Coal, and five pure compounds found in coal liquefaction products. For these samples, the heats of combustion are calculated using predicted values of AHf° and compared in Table IV with observed values. Note that Equations 8 and 9 were used to predict AHf° and S° of the EDS heavy naphtha. Equations 6 and 7 are applied to other samples of coal-derived liquids, and Equations 3 and 4 to the pure compounds. 

Figure 4. Upper curve liquid chromatogram (UV detector 254 nm) of a Synthoil sample in isopropyl alcohol the ticks denote fractions that were rechromatographed. Bottom curves chromatograms of each of the individual fractions after being passed through the same column (15J.

This chapter reports results of applying a catalytic hydrorefining process to four coal liquids solvent-refined coal (SRC) process filter feed, SRC extract product, Synthoil, and H-Coal process hydroclone underflow. The achieved upgrading is evaluated in terms of reduction in benzene and heptane insolubles, reduction in sulfur, nitrogen, and oxygen, an increase in hydrogen content, and a yield of lower boiling products. 

Both particulates and dissolved metals are probably involved in pore plugging when processing primary coal liquids. Analyses suggest that the former are more significant in the case of the Synthoil sample, and both are significant in the case of the SRC sample. 

For some reactions listed in Table 1-4A, the fixed-bed reactor is operated under cocurrent-upflow conditions. Unlike the trickle-flow condition, this type of operation is normally characterized by bubble-flow (at low liquid and gas rates) and pulsating-flow (at high gas flow rates) conditions. Normally, the bubble-flow conditions are used. In the SYNTHOIL coal-liquefaction process, both pulsating-and spray-flow conditions are used, so that the solid reactant (coal) does not plug the reactor. In bubble flow, the gas is the dispersed phase and the liquid Ls a continuous phase. In pulsating flow, pulses of gas and liquid pass through the reactor. In the spray-flow regime, the gas is a continuous phase and the liquid is a dispersed phase. 

The GSLI are often operated under very high gas and liquid flow rates (near flooding) compared to the ones used in GSLC (in particular trickle-bed) reactors. An exception is the SYNTHOIL reactor for coal liquefaction. 

Microstructure. The characterization of coal-derived asphaltene is quite similar to that of petroleum-derived asphaltene. Since it is anticipated that coal-derived asphaltene will have acid/neutral and base characteristics (26, 36), the average structure of both must be considered. In Table III, Structure I is amphoteric (or slightly basic), and Structure II is an acid/neutral representation. A mixture of both may be typical of the average structure of a coal-derived asphaltene. At present, we will illustrate this by an asphaltene obtained from coal liquid of the Synthoil process. (The coal is hvAb, West Kentucky, Homestead Seam the coal liquid is obtained by catalytic hydrogenation at 450° C and 4000 psig having %C, 86.7 %H, 8.38 %N, 0.93 %S, 0.09 %Q, 3.2 and %Ash, 0.7.)... 

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