Reactors fractionating synthesis

Using two-stage series reactor system, gasoline fraction of hydrocarbons was also synthesized. [41] As a methanol conversion catalyst, MFI-type metallosihcate such as H-Fe-sdicate and H-Ga-sdicate were optimum for gasohn fraction synthesis. 

A stream at 220 atm and 100 °C containing 27.2% NH3, 54.5% H2, and 18.2% NH3 is currently being recycled to an ammonia synthesis reactor. You want to feed it through a hollow-fiber module with a fiber volume fraction of 0.5 to recover 90% of the ammonia. The module s membranes are 240 pm in diameter, have a permeability P of 4.0 10 cm /sec, and a selective layer thickness I equal to 35 pm. How long should gas spend in this module ... 

The catalytic hydrogenation of fatty oils, the desulfurization of liquid petroleum fractions by catalytic hydrogenation, Fischer-Tropsch-type synthesis in slurry reactors, and the manufacture of calcium bisulfite acid are familiar examples of this type of process, for which the term gas-liquid-particle process will be used in the following. 

C30 oil, homopolymer of 1-decene, Ethyl Corp., Inc.) served as the start-up solvent for the experiments. The catalyst (ca. 5-8 g) was added to start-up solvent (ca. 300 g) in the CSTR. The reactor temperature was then raised to 270°C at a rate of l°C/min. The catalyst was activated using CO at a space velocity of 3.0 sl/h/g Fe at 270°C and 175 psig for 24 h. FTS was then started by adding synthesis gas mixture (H2 CO ratio of 0.7) to the reactor at a space velocity of either 3.1 or 5.0 sl/h/g Fe. The conversions of CO and H2 were obtained by gas chromatography (GC) analysis (HP Quad Series Micro-GC equipped with thermal conductivity detectors) of the product gas mixture. The reaction products were collected in three traps maintained at different temperatures—a hot trap (200°C), a warm trap (100°C), and a cold trap (0°C). The products were separated into different fractions (rewax, wax, oil, and aqueous) for quantification by GC analysis. However, the oil and the wax (liquid at room temperature) fractions were mixed prior to GC analysis. 

The Oxo process uses synthesis gas with a H2 to C(0 ratios of 1 1 to 2 1, Hydro for mylation in the Oxo reactor takes place at moderate temperatures, 212-400°F, but very high pressures, 3000-5000 psi. The effluent from the reactor is cleaned up to remove light gas by-products to recover the catalyst for recycling and to recycle any unreacted olefin. Ac this point, the balance between the aldehyde isomers can be adjusted by fractionating out the... 

Obviously, equation 8 suggests that the ideal synthesis gas reactor should operate at a CH4 02 mole ratio of 2 1 (29.6% CH4 in air) if total conversion of the reactants occurs. At high enough temperatures, this mixture is completely converted to H2 and CO at thermodynamic equilibrium. Below about 1270 K, the equilibrium mole fraction of carbon becomes significant. Hence, a reactor must be maintained above 1270 K to avoid carbon formation. 

Pibouleau et al. (1988) provided a more flexible representation for the synthesis problem by replacing the single reactor unit by a cascade of CSTRs. They also introduced parameters for defining the recovery rates of intermediate components into the distillate, the split fractions of top and bottom components that are recycled toward the reactor sequence, as well as parameters for the split fractions of the reactor outlet streams. A benzene chlorination process was studied as an example problem for this synthesis approach. In this example, the number of CSTRs in the cascade was treated as a parameter that ranged from one up to a maximum of four reactors. By repeatedly solving the synthesis problem, an optimum number of CSTRs was determined. 

If the feed is suddenly stopped, it behaves as an adiabatic batch reactor with an accumulation corresponding to the non-converted fraction, thus the maximum temperature of the synthesis reaction is... 

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