Liquid simulated distillation

The MAT tests using North Sea gas oil were run at 482 C while the hydrotreated resid was run at 510 C. Simulated distillations on the recovered liquid products were run using 217 and 343 C gasoline and LCO cut points. All data have been normalized to a lOOX material balance. 

Standard cut points from ASTMD 2887 simulated distillation were used for liquid product yield calculation gasoline was defined as the C5-221°C fraction, light cycle oil (LCO) as the 221°C-343°C fraction and slurry oil as the 343°C fraction. Gasoline quality was determined by gas chromatography using PONA column and a variation of the methodology described by Anderson [1]. 

The flue gas and the product gas are analyzed with a rehnery gas analyzer from Varian. The liquid products are analyzed by simulated distillation on a Varian gas chromatograph. 

Sulfur compounds in the gas oil fractions from two bitumens (Athabasca oil sand and Cold Lake deposit)> a heavy oil (Lloydminster) from Cretaceous reservoirs along the western Canada sedimentary basin, and a Cretaceous oil from a deep reservoir that may be mature (Medicine River) are investigated. The gas oil distillates were separated to concentrates of different hydrocarbon types on a liquid adsorption chromatographic column. The aromatic hydrocarbon types with their associated sulfur compounds were resolved by gas chromatographic simulated distillation and then by gas solid chromatography. Some sulfur compounds were further characterized by mass spectrometry. The predominant sulfur compounds in these fractions are alkyl-substituted benzo- and dibenzothiophenes with short side chains which have few dominant isomers. 

Chromatographic Separations. The distillates from the oils were separated first by liquid chromatography, then by gas chromatographic-simulated distillation according to boiling point, and finally by gas chromatography on lithium chloride-coated silica, as shown in Figure 2. 

The first polyaromatic polar fraction from the Athabasca oil was similar to the largest fraction in this class from the Lloydminster oil. All the simulated distillation chromatograms of the first polyaromatic polar fractions in the C region of the liquid chromatograms are shown in Figures 14-17. Sulfur peaks from the three oils are fairly well resolved,... 

Simulated Distillation of Bitumen Sample. The boiling-range distribution of the recovered bitumen was determined by simulated distillation gas-liquid chromatography using the procedure of Poulson et al. (15). Boiling points are determined by calibration with a mixture of n-paraffins ranging from Cn to C42. The upper limit for boiling point determination in this analysis is about 540°C (1000°F). 

The SRC-II liquid was obtained from the Pittsburg and Midway Coal Mining Co. The liquid was produced from Material Balance Run No. 77 SR-12 on coal from the Pittsburg seam from Consol s Blacksville No. 2 Mine in West Virginia. The middle (177-288° C) and heavy (288-454°C) distillates were blended to the same ratio as produced by the material balance run, e.g., 75.5 percent middle distillate and 24.5 percent heavy distillate. The feed contained 0.23 wt-pct sulfur, 1.06 wt-pct nitrogen and 3.29 wt-pct oxygen and boiled between 185 and 380° C (5-95 percent) by simulated distillation. 

Gases were analyzed by GC and separated by a Porapak-Q plus silica column. Liquids were analyzed by simulated distillation. 

Silica, while the liquid products were analyzed by simulated distillation. The amount of coke was measured from the weight of water and carbon dioxide generated during regeneration. 

Product Evaluation. Gaseous products were analyzed by gas chromatography (GC) using an alumina column. Liquid products were evaluated by physical properties, elemental analysis, liquid chromatographic separation (9), and simulated distillation (10). Distillation to produce a gasoline fraction was accomplished with a spinning band distillation column. Gasoline analysis and evaluation was obtained from an industrial analysis laboratory. 

Evaluations of steamed catalysts were performed with a MAT unit using a standard mid-continent gas oil. The MAT conditions varied and are identified in the tables. Selectivities were determined from gas chromatographic analysis of liquid and gaseous products by Hewlett-Packard, simulated distillation hardware and Carle.,... 

The amount of liquid product was measured to find out the reaction yield for each experiment. Density and boiling-point distribution were analyzed by ASTM D97 and ASTM D2S87 (simulated distillation) standard methods. Simulated distillations were converted to ASTM D86 distillations to allow calculating cetane indexes according to ASTM D4737. Liquid products were also analyzed by MS-GC to obtain their qualitative composition, and by elemental analysis (C, H, S and O) to check the extent of hydrogenation. 

The Microactivity Test (MAT) reactor is used primarily for cracking catalysts, such as those based on zeolites. In the MAT test, a given amount of feed is pumped within 1-75 s over a measured amount of catalyst in a fixed bed. Liquid and vapor products can be collected separately and analyzed. The MAT and TOS techniques are similar in principle, hence results for these two can be expected to be similar. Comparison with commercial reactors is carried out by empirically adjusting the test conditions. Conversion and simulated distillation results between MAT units can be compared by using standard catalysts and feeds using ASTM D-3907. 

Equihbrium-based simulation) distillation, liquid-hquid extraction. Additional strippers and pump-arounds can be added. All models support two or three phases tuid reactions. Physical property models are available for petroleum refining applications. 

In all experiments, the amount of catalyst employed was 9 g, and vacuum gas oil feed rate was 72 for times on stream 60,75,100 and 150 s. The reactions were carried out at temperatures of 480, 500 and 520 C. Gas products (dry gas and LP gas) were analyzed by cromatography. The liquid product (gasoline, light and heavy cycle oils) was analyzed after simulated distillation (ASTM-D-2887). The amount of coke on the catalyst was determined through the IR analysis of CO2 produced by the coke burning in air at 695 °C. The mass balance calculated from product recovery was in the range 97.2 to 100.9 %. 

The liquid products were characterized by simulated distillation in a gas chromatograph. Aromaticity was evaluated by UV absorption spectroscopy. 

In a study using EU-approved food simulants, antimony migration from PET containers into distilled water, 3 % acetic acid, and 10 % and 20 % ethanol was measured (Sanchez-Martinez et al. 2013). Migration values ranged from 0.5 to 1.2 pg/L, with pentavalent antimony being the only species found in aqueous liquids. Antimony trioxide, the form used as catalyst in PET manufacture, was not detected in the liquid simulants. The authors suggest it is possible that the trioxide... 

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