Flash separator

rich glycol at reduced pressure generates flash gas that can be used as a fuel gas to the regenerator reboiler or as a stripping gas or for both. Excess flash gas is normally vented to the flare system. The flash separator pressure is maintained through a back-pressure control valve on the gas outlet line from the separator. The liquid flow is maintained through a level-control valve. 

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The calculation of single-stage equilibrium separations in multicomponent systems is implemented by a series of FORTRAN IV subroutines described in Chapter 7. These treat bubble and dewpoint calculations, isothermal and adiabatic equilibrium flash vaporizations, and liquid-liquid equilibrium "flash" separations. The treatment of multistage separation operations, which involves many additional considerations, is not considered in this monograph. 

For a binary, let s denote as V the fractional molar split of the feed into overhead product and as L the fractional split into bottom product. Calculate compositions of the flash separation of feed into vapor v and liquid 1 to give v/1 = V/L. The resulting vapor can be regarded as being composed of a portion d of the overhead product composition and a portion r of the flash liquid composition. 

Low-temperature exchange (LTX) units use the high flowing temperature of the well stream to melt the hydrates after they are formed. Since they operate at low temperatures, they also stabilize the condensate and recover more of the intermediate hydrocarbon components than would be recovered in a straight multistage flash separation process. 

Example 8-19 Continuous Steam Flash Separation Process Separation of Non-Volatile Component from Oi anics... 

Batch with Constant Reflux Ratio, 48 Batch with Variable Reflux Rate Rectification, 50 Example 8-14 Batch Distillation, Constant Reflux Following the Procedure of Block, 51 Example 8-15 Vapor Boil-up Rate for Fixed Trays, 53 Example 8-16 Binary Batch Differential Distillation, 54 Example 8-17 Multicomponent Batch Distillation, 55 Steam Distillation, 57 Example 8-18 Multicomponent Steam Flash, 59 Example 8-18 Continuous Steam Flash Separation Process — Separation of Non-Volatile Component from Organics, 61 Example 8-20 Open Steam Stripping of Heavy Absorber Rich Oil of Light Hydrocarbon Content, 62 Distillation with Heat Balance,... 

Rich amine from the bottom of the HjS contactor goes to a flash separator to remove dissolved hydrocarbons from the amine solution. The rich amine is pumped from the separator to the amine regenerator,... 

One can interpret this physically as follows suppose that the trajectory of the harmonic oscillator be represented by a point on a rotating wheel. The eye observes a circle (the path of the point) if the wheel rotates rapidly this corresponds to continuous illumination. On the other hand, if one illuminates the rotating wheel with stroboscopic flashes separated by a period 2n, a given mark on the wheel appears as a fixed point. Thus, under continuous illumination one sees ... 

Distillation usually is the most economical method of separating liquids, superior to extraction, adsorption, crystallization, or others. Exceptions to this rule include Flash separation when flash separation is sufficient and Settling (decanting or coalescing) when the mixture has LL immiscibility without addition of extraction solvent. 

To demonstrate the effectiveness of this approach, consider the optimization of the ammonia process given in Fig. 2. This process is a single-loop design with a three-stage adiabatic flash separation. Further details of the process can be found in Lang and Biegler (1987). 

The module FLASH simulates the reformer flash separator by using a modified Chao-Seader method. The necessary constants for the Chao-Seader correlation have been developed for the lumped components. The output from this module determines the liquid yield and the composition of recycle gas. 

A series of flash separations in which the gas is removed at each stage simulates a differential vaporization process. 

This residue is further heated and introduced into a vacuum column operated at an absolute pressure of about 50 millimeters of mercury, a vacuum maintained by the use of steam ejectors. A flash separation is made to produce heavy gas oil and nondistillable pitch. 

In the process (Figure 9-22), fresh vacuum residuum, microcatalyst, and hydrogen are fed to the hydroconversion reactor. Effluent is sent to a flash separation zone to recover hydrogen, gases, and liquid products, including naphtha, distillate, and gas oil. The liquid bottoms from the flash step is then fed to a vacuum distillation tower to obtain a 565°C (1050°F ) product oil and a 565°C + (1050°F+) bottoms fraction that contains unconverted feed, microcatalyst, and essentially all of the feed metals. 

One of the most successful petrochemical applications is illustrated in Figure 8.14 treatment of resin-degassing vent gas in a polyolefin plant [28]. In these plants, olefin monomer, catalyst, solvents, and other coreactants are fed at high pressure into a polymerization reactor. The polymer product (resin) is removed from the reactor and separated from excess monomer in a flash-separation step. The recovered monomer is recycled to the reactor. Residual monomer is removed from the resin powder by... 

Devolatilization of concentrated solution may start with an above atmospheric flash separation. This way the solvent and unreacted monomer can be easily and directly recycled. However, downstream all devolatilization equipment is operated under reduced... 

Flash Flash , FlashS Separator, 3-Phase Separator... 

The checkers isolated the product by standard flash separation chromatography on Bakerflex flash-grade silica. Unreacted 2-(diphenylphosphino)benzoic acid was obtained as the first band, and the product was obtained cleanly as the second band. An unidentified phosphorus compound was detected in the column wash by PNMR. 

Suggest a solution order for the set of equations in Table P5.14 representing the flash separator in Fig. P5.14. The selection of the first seven of the eight design variables to be calculated (feed stream variables and the equilibrium pressure) is standard for flash separations. The last design variable is usually selected as either... 

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