Parallel cycle

This result requires some explanation. An argument was given by Denton [6], who pointed out that the expansion of the mixed gas (I + ip) from to may be considered as a combination of unit flow through the turbine from T3 to T4, and an expansion of a flow of (/(from T2 to 7), through a reversed compressor (Fig. 4.2). The cycle [1,2,3,5,6,1] of Fig. 4.2a is equivalent to two parallel cycles as indicated in Fig. 4.2b a cycle [1,2,3,4,1] with unit circulation plus another cycle passing through the state points [1,2,2,1] with a circulation tp. The second cycle has the same efficiency as the first (but vanishingly small work output) so that the combined cooled cycle has the same efficiency as each of the two... 

Rueping has recently reported an interesting alknylation reaction of a-imino esters employing both phosphoric acid Ip and AgOAc as orthogonal cocatalysts [35]. As seen in the catalytic cycle in Scheme 5.21, generation of chiral iminium ion pair I nucleophilic and alkynyl-silver species II proceeds simultaneously. Subsequent nucelophilic addition completes both parallel cycles [36]. 

Introducing parallel operations to the steps which limit the batch cycle time. 

Whether parallel operations, larger or smaller items of equipment, and intermediate storage should be used can only be judged on the basis of economic tradeoffs. However, this is still not the complete picture as far as the batch process tradeoffs are concerned. So far the batch size has not been varied. Batch size can be varied as a function of cycle time. Overall, the variables are... 

Dehydrogenation of /i-Butane. Dehydrogenation of / -butane [106-97-8] via the Houdry process is carried out under partial vacuum, 35—75 kPa (5—11 psi), at about 535—650°C with a fixed-bed catalyst. The catalyst consists of aluminum oxide and chromium oxide as the principal components. The reaction is endothermic and the cycle life of the catalyst is about 10 minutes because of coke buildup. Several parallel reactors are needed in the plant to allow for continuous operation with catalyst regeneration. Thermodynamics limits the conversion to about 30—40% and the ultimate yield is 60—65 wt % (233). 

Consider the scheme of Example 23.4 having an automatic parallel switching. If we assume the closing sequence cycle to be 30 seconds, the recommended value of discharge resistance for each 20 kVAr capacitor bank having a capacitance of 120 fiF can be determined as follows ... 

If the work assumption is made, i.e., if it is assumed that the external work done by surface and body forces on a finite region in the reference configuration of a body undergoing homogeneous closed cycles of deformation is nonnegative, then an inequality may be deduced paralleling (5.37) by arguments essentially the same as those of Section 5.2.4. 

A semi-batch reactor has the same disadvantages as the batch reactor. However, it has the advantages of good temperature control and the capability of minimizing unwanted side reactions by maintaining a low concentration of one of the reactants. Semi-batch reactors are also of value when parallel reactions of different orders occur, where it may be more profitable to use semi-batch rather than batch operations. In many applications semi-batch reactors involve a substantial increase in the volume of reaction mixture during a processing cycle (i.e., emulsion polymerization). 

Fixed-bed adsorbers may be operated in either intermittent or semicon-tinuous mode. A typical removal system is a semicontinuously operated dnal-bed system one bed is in adsorption mode while the other is being re generated (Fig. 13.23). " The adsorption performance of the bed can he monitored by analyzing the outlet gas. Once organic vapors are detected in the gas stream, the incoming gas stream is routed to the parallel adsorber, and the exhausted bed is regenerated. The adsorption and desorption cycles can also be fixed. 

Calculation of the specific work and the arbitrary overall efficiency may now be made parallel to the method used for the a/s cycle. The maximum and minimum temperatures are specified, together with compressor and turbine efficiencies. A compressor pressure ratio (r) is selected, and with the pressure loss coefficients specified, the corresponding turbine pressure ratio is obtained. With the compressor exit temperature T2 known and Tt, specified, the temperature change in combustion is also known, and the fuel-air ratio / may then be obtained. Approximate mean values of specific heats are then obtained from Fig. 3.12. Either they may be employed directly, or n and n may be obtained and used. 

A modification of the HAT cycle has been proposed by Nakhamkin [11], which is known as the cascaded humid air turbine (CHAT). The higher pressure ratios required in humidified cycles led Nakhamkin to propose reheating between the HP and LP turbines. Splitting the expansion in this way is paralleled by splitting the compression, and enables the HP shaft to be non-generating, as indicated in Fig. 6.15. This implies that the capital cost of the plant can be reduced, but the cycle is still complex. 

Macchi et al. [9] made an extensive study of water injection cycles in their two classic papers and their results are worth a detailed study. Some of their calculations (for ISTIG, RWI and HAT) are reproduced in Figs. 6.18-6.20, all for surface intercooling (parallel calculations for evaporative intercooling are given in the original papers). 

Harmonics or multiples of 2, 3, 4, etc., of this frequency will exist and be dominant for two-cycle gas engines, and one half multiples will be dominant for four-cycle engines. If several single-acting cylinders are operating on the same system in parallel, the magnitude of the pulses will depend upon the combination of cylinders and crank throws, and this magnitude is additive for the simultaneous waves in phase. 

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