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Heat isobutane alkylation

Seasonal chances in gasoline sales and heating oil sales compel some modifications to be made in conversion level. Therefore, the conversion pattern of a given catalytic cracking unit can vary from season to season. In summer operations, for instance, higher yields of motor gasoline are desired, both from direct production of 5/430° FVT catalytic naphtha and also from conversion of butylenes and isobutane to alkylate. [Pg.15]

At the heart of the UOP HF alkylation unit is a vertical reactor-heat exchanger, shown in Fig. 14. The isobutane-alkene mixture enters the shell of the reactor through several nozzles, and HF enters at the bottom of the reactor. The reaction heat is removed by cooling water, which flows through cooling coils inside the reactor. After phase separation in the settler, the acid is recycled to the reactor. The hydrocarbon phase together with a slipstream of used acid and makeup isobutane is sent to the isostripper , where the alkylate product, n-butane, and isobutane are separated. The isobutane is recycled to the reactor. During normal... [Pg.303]

A, Find the optimum liquid concentration of the propane isobutane mixture in an auto lefrigerated alkylation reactor. The exothermic heat (10 Btu/h) of the alkylation reaction is removed by vaporization of the liquid in the reactor. The vapor is com pressed, condensed, and flashed back into the reactor through a pressure letdown valve. The reactor must operate at 50°F, and the compressed vapors must be condensed at 110°F. [Pg.115]

In this work, the goal is to design a control function in such a manner that neither the reaction heat nor kinetic nor mass transfer terms are required for stabilizing temperature. The scheme provides an estimated value of the heat generation from energy balance. Alkylation isobutane/propylene using sulfuric... [Pg.35]

High isobutane recycle purity is not required on HF alkylation units as is required on many H2SO4 units because relatively high normal butane concentrations in the reaction zone do not appreciably affect the quality of the alkylate. Isobutane purities below 60% are usually avoided, however, since this purity definitely gives lower-quality alkylate and the cost of recycling the normal butane is considerable in heat requirements as well as fractionation equipment requirements. [Pg.191]

Table 9.3 Kinetic parameters and heat of reaction for isobutane/1 -butene alkylation. Table 9.3 Kinetic parameters and heat of reaction for isobutane/1 -butene alkylation.
Model structure is shown in Figure 5. Process variables, unit constants (such as heat transfer coefficients), and feed streams are described on input or as selected by the optimization routine. Then, heat and material balances are performed using an assumed alkylate yield and isobutane consunq>tion. These results form a set of reaction conditions irtiich are used in correlations to calculate reactor performance. The heat and material balance calculations are repeated if reactor performance differs significantly from that used in the previous calculation. Operating incentives are then conqmted and may be used in the optimization routine to select new values of the optimization variables. [Pg.264]

Extraction. Solvent extraction processes are usually fairly expensive because of the cost in recovering the solvent, such as by heating or chilling, and usually with some loss of solvent. In SARP we have a unique and quite favorable situation. The solvent is a recycle stream of isobutane from the alkylation section, which, after it is used to extract DIPS, is returned along with the DIPS to alkylation, where the isobutane is processed as usual in alkylation. [Pg.296]

A portion of this chilled Isobutane liquid flows upward to chill the downflowing acid, remove the heat of fusion and convey the alkylate back to the alkylation reactor. The remainder conveys the acid crystals plus ester concentrate mixture to the centrifugal... [Pg.307]

Alkylation reactions were conducted in a 20-mL monel vessel. Measured amounts of the reactants were condensed into the vessel by cooling it to liquid nitrogen temperature. Thereafter, the vessel was heated to a temperature above the critical point of isobutane and was allowed to stand for 16 hr to assure complete mixing of the reactant gases. To carry out the reaction, the vessel was then rapidly heated in a sand bath for a measured time, and the reaction was terminated by depressurizing. [Pg.292]

The alkylation reaction of isobutane with a mixture of C4 linear olefins was carried out in liquid phase at temperatures between 25 and 80°C, and at 30 Kg/cm, in a fixed-bed reactor. The space velocity was WHSV = 1 ft referred to the olefins. The isobutane is premixed with the olefins. The molar ratio used in this study was 15. The C4 olefins fraction contains 38% 1-butene, 22% trans-butene, 14% cis-2-butene and 26 % isobutene. In order to analyze the products coming out of the reactor, a ten-loop valve was used to collect the sample to be analyzed after the mn. Products are analyzed by GC, using a 100 m squalane column. Prior to the reaction, catalysts were pretreated in-situ, heating up to 250 C in an air stream. [Pg.408]

In each compartment, the pressure is regulated so that some of the dispersed hydrocarbons vaporize. Light hydrocarbons and especially isobutane vaporize this vaporization removes most but not all of the following heats of reaction plus energy provided by agitation. Ackerman et al. have reported that there is a temperature increase from the first to the last compartment simultaneously, the quality of the alkylate decreases.The vaporization, with high certainty, occurs mainly in those droplets positioned at or near the top surface of the dispersion, where the pressure is lowest. Hence, many of the droplets that pass over the vertical plate from one compartment to the next have experienced vaporization (and have reduced concentrations of isobutane). [Pg.61]

In an analogous manner, isopropyl chloride was converted to propane in 90% yield whenitwas heated at 40° with isopentane and aluminum chloride. Heating the isopentane with aluminum chloride and hydrogen chloride caused it to undergo autodestructive alkylation, yielding higher-boiling isoparafiins and isobutane but no propane less catalyst complex was formed than when isopropyl chloride was used. [Pg.45]


See other pages where Heat isobutane alkylation is mentioned: [Pg.413]    [Pg.168]    [Pg.198]    [Pg.225]    [Pg.290]    [Pg.985]    [Pg.302]    [Pg.303]    [Pg.309]    [Pg.40]    [Pg.511]    [Pg.248]    [Pg.213]    [Pg.248]    [Pg.190]    [Pg.39]    [Pg.88]    [Pg.44]    [Pg.278]    [Pg.285]    [Pg.225]    [Pg.302]    [Pg.303]    [Pg.309]    [Pg.262]    [Pg.275]    [Pg.320]    [Pg.2134]    [Pg.2561]    [Pg.2564]    [Pg.121]    [Pg.178]    [Pg.140]    [Pg.2120]    [Pg.181]    [Pg.45]   
See also in sourсe #XX -- [ Pg.279 ]




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Isobutane

Isobutane alkylation

Isobutanes

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