Catalytic liquid products from

Antdysis of Liquid Product from Catalytic Cracking of n-Octenes... 

Liquid solvents are used to extract either desirable or undesirable compounds from a liquid mixture. Solvent extraction processes use a liquid solvent that has a high solvolytic power for certain compounds in the feed mixture. For example, ethylene glycol has a greater affinity for aromatic hydrocarbons and extracts them preferentially from a reformate mixture (a liquid paraffinic and aromatic product from catalytic reforming). The raffinate, which is mainly paraffins, is freed from traces of ethylene glycol by distillation. Other solvents that could be used for this purpose are liquid sulfur dioxide and sulfolane (tetramethylene sulfone). 

Products from catalytic cracking units are also more stable due to a lower olefin content in the liquid products. This reflects a higher hydrogen transfer activity, which leads to more saturated hydrocarbons than in thermally cracked products from delayed coking units, for example. 

The liquid products of catalytic cracking (obtained in accordance with the described principles) have been omitted from consideration thus far, except in the case of the alkyl aromatics. To the refiner, the liquid obtained is of prime importance, both as gasoline and heavier intermediate oils. 

The process has three basic variations-the Type II unit, the Type III unit, and the Type IV unit with the degree of desulfurization, and process severity, increasing from Type I to Type IV. Thus, liquid products from Types III and IV units can be used directly as catalytic cracker feedstocks and perform similarly to virgin gas oil fractions, whereas liquid products from the Type II unit usually need to be vacuum-flashed to provide a feedstock suitable for a catalytic cracker. 

Liquid Products from Thermal and Catalytic Cracking Run Designation ... 

Lee et al. [13] have described the cnmnlative amount distributions of liquid product by catalytic degradation of waste HDPE at different reaction temperatures and at a reactant amonnt of 200 g, as shown in Fignre 5.8. These distributions were clearly dependent on reaction temperature. Thus the slope from the cumulative amount of liquid product versus the initial reaction time was defined as the initial rate of degradation, which is shown as a fnnction of reaction temperatnre in Fignre 5.9. The initial rate of degradation of waste HDPE was exponentially increased with increase of reaction temperature and moreover at... 

Figure 5.14 Cumulative amount distributions of liquid products for catalytic degradation of waste HOPE and PS mixture using spent FCC catalyst at 400°C. (A initial degradation region B final degradation region). (Reproduced with permission from Elsevier)...

Figure 18.5 C-NP gram of liquid products from thermal and catalytic (SA1) degradation of PP/PVC (8/2) mixture (10 g) at 380°C. (Reproduced with permission from the American Chemical Society)...

Elliott, D.C., Wang, H., French, R., Deutch, S., lisa, K., 2014. Hydrocarbon liquid production from biomass via hot-vapor filtered fast pyrolysis and catalytic hydroprocessing of the biooil. Energy Fuels 28, 5909—5917. 

Liquid Fuels. Liquid fuels can be obtained as by-products of low temperature carbonization by pyrolysis, solvent refining, or extraction and gasification followed by catalytic conversion of either the coal or the products from the coal. A continuing iaterest ia Hquid fuels has produced activity ia each of these areas (44—46). However, because cmde oil prices have historically remained below the price at which synthetic fuels can be produced, commercialization awaits an economic reversal. 

Cost. The catalytically active component(s) in many supported catalysts are expensive metals. By using a catalyst in which the active component is but a very small fraction of the weight of the total catalyst, lower costs can be achieved. As an example, hydrogenation of an aromatic nucleus requires the use of rhenium, rhodium, or mthenium. This can be accomplished with as fittie as 0.5 wt % of the metal finely dispersed on alumina or activated carbon. Furthermore, it is almost always easier to recover the metal from a spent supported catalyst bed than to attempt to separate a finely divided metal from a liquid product stream. If recovery is efficient, the actual cost of the catalyst is the time value of the cost of the metal less processing expenses, assuming a nondeclining market value for the metal. Precious metals used in catalytic processes are often leased. 

The process consists of a reactor section, continuous catalyst regeneration unit (CCR), and product recovery section. Stacked radial-flow reactors are used to minimize pressure drop and to facilitate catalyst recirculation to and from the CCR. The reactor feed consists solely of LPG plus the recycle of unconverted feed components no hydrogen is recycled. The liquid product contains about 92 wt% benzene, toluene, and xylenes (BTX) (Figure 6-7), with a balance of Cg aromatics and a low nonaromatic content. Therefore, the product could be used directly for the recovery of benzene by fractional distillation (without the extraction step needed in catalytic reforming). 

The catalytic degradation of polypropylene was carried out over ferrierite catalyst using a thermogravimetric analyzer as well as a fixed bed batch reactor. The activation of reaction was lowered by adding ferrierite catalyst, which was similar with that from ZSM-5. Ferrierite produced less gaseous products than HZSM-5, where the yields of i-butene and olefin over ferrierite were higher than that over HZSM-5. In the case of liquid product, main product over ferrierite is C5 hydrocarbon, while products were distributed over mainly C7-C9 over HZSM-5. Ferrierite showed excellent catalytic stability for polypropylene degradation. 

Fig. 5. Cumulative liquid product 3deld from thermal and catalytic degradation of LDPE at different temperature...

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