Column liquefaction products

Process solvents SRC s, and liquefaction products also were examined by column chromatography (11). The sample was dissolved in chloroform or THF, pre-adsorbed on neutral alumina (12), and eluted from neutral alumina to give saturates, aromatics, and three polar fractions. The saturate fraction was analyzed quantitatively by mass spectrometry, and compound identification in distillates and solvents was confirmed by combined GC-MS or high-resolution MS analysis of column chromatography fractions. 

Figure 1. Column chromatographic data for SRC s and coal liquefaction products 1. P M 308 3. P ir M 122 3. Project Lignite SRL-M5C 4. Wilsonville SRC-Pitt 8 5. P ir M 11 SR 6. CO-Steam Product 7.

The indirect liquefaction basehne design is for a plant of similar size. Unhke the direct hquefaction basehne, the design focuses on producing refined transportation fuels by use of Sheh gasification technology. Table 27-17 shows that the crude oil equivalent price is approximately 216/m ( 34/bbl). Additional technological advances in the production of synthesis gas, the Fischer-Tropsch synthesis, and product refining have the potential to reduce the cost to 171/m ( 27/bbl) (1993 US dollars), as shown in the second column of Table 27-17. 

A related reactor is that for coal liquefaction, which can be carried out in a three-phase slurry bubble column (see Fig. 5). Hydrogen can be supplied at the bottom of a column of downcoming product—oil. The solid coal reactant is blended with the product or carrier oil and fed at the top. The generic process depicted in Fig. 5 is a generalization of the liquefaction reactor in the Exxon Donor Solvent Process. As the gas flow rate increases, the bubbles change from uniformly small to chaotic. In the H-coal process, both the gas and a coal-oil slurry are fed from the bottom in an ebullating-bed reactor. Catalyst solids are fed from the top. This reactor operates as an expanded... 

During the period from 1995-96, attempts to operate the direct liquefaction reactor in a F-T mode were successful in that a clear wax product could be obtained. However, the initial activity observed in the bubble column was about 10-15% less than that of comparable CSTR... 

Air liquefaction made it possible to distill air. Attempts to do so using a single distillation column produced a gas product consisting of 40 percent to 50 percent oxygen. Cleverly exploiting his patent for this process, Linde marketed this oxygen-enriched gas as Linde Air (19),... 

The most frequent synthetic use of electrolytic hydrogen is the production of HCl, which is covered in Section 9.1.9.2. This is a natural outlet for a chlor-alkali producer, who can use HCl to acidify cell feed brine or depleted brine and to regenerate ion-exchange columns. It also allows profitable use of the chlorine contained in the liquefaction tail gas. The HCl that can be consumed internally, and so the amount of... 

Column chromatography is a very useful sample preparation method. In the work reported by Ruberto et al. [23], five liquid products from different pilot plant-scale coal liquefaction processes were examined. Column chromatography was used to isolate a fraction of each sample that contained the nitrogen compounds, and this fraction was analyzed by GC-MS, LV-MS, and... 

The absorption in alkanolamine solutions (MEA, DEA, ADIP, DGA, etc.) is the commercially most important process for the removal of CO2 from synthesis gas for ammonia and methanol production, for the production of hydrogen, in natural gas purification, coal liquefaction, and the like. In the present example a gas containing 13.55 mole-% of CO2 is to be purified by absorption into an aqueous solution of 13.6 wt-% MEA. The column, filled with 0.05 m steel Pall rings, has a diameter of 1.05 m and is operating at a temperature of 315 K and a pressure of 14.3 bars. The inlet flow rates of gas and liquid are 497 kmol/h and 76.9 mVh, respectively. Determine the packed column height necessary to reduce the mole fraction of CO2 to 5 x 10 at the top of the column. 

The primary purpose of this paper is to describe the kinetics of coal liquefaction derived from a pilot-scale unit. The specific coal studied was Big Horn subbituminous coal. The experimental data were obtained in a pilot-scale Gulf patented (13) reactor. The data illustrate the effects of reactor space time and temperature on the product distribution. Since the reactor behaves as a bubble column, the intrinsic kinetics of the liquefaction process can be extracted by means of a kinematic model of the reactor. The experimental data were found to be... 

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