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Gas outlet nozzles

A typical horizontal three-phase separator with flooded weir is shown in Figure 3.4. The inlet nozzle (Nl) and the gas outlet nozzles (N2) are placed as close as possible to the vessel tangent line. The distance of tiie nozzle center line and the tan line is dictated by tiie mechanical limitations of the vessel however, distances in Table 3.7 can be used for initial design. [Pg.219]

As the gas outlet nozzle is not required to be designed for a two-phase flow, a higher momentum can be used for the design. Normally, the following value is used ... [Pg.233]

As liquid flows out of the exit nozzle, it will swirl and create a vortex. Vortexing would carry the gas out with the liquid. Therefore, all liquid outlet nozzles should be equipped with a vortex breaker. Figure 12-0 shows several vortex breaker designs. Additional designs can be found in the Pressure Vessel Handbook. Most designs depend on baffles around or above the outlet to prevent swirling. [Pg.346]

In order to handle higher loads, the liquid baffle is placed at the top to collect liquid and cause it to drop back down through the gas body. If the baffle is omitted, the liquid will run dowm the oudet pipe and be sw ept into the outlet nozzle by the outgoing gas as shown in Figure 4-50B. Figure 4-50 and 4-51 show several alternate entrance and exit details. The unit with a tangential entry is 30%-60% more efficient than one with only a turned-down 90° elbow in the center. [Pg.264]

A venturi nozzle is located in the clean-gas outlet from each bag, which is used for cleaning. A jet of high-velocity air is directed through the venturi nozzle and into the bag, which induces clean gas to pass through the fabric to the dirty side. The high-velocity jet is released in a short pulse, usually about 100 milliseconds, from a compressed... [Pg.778]

Gas-Liquid separation chamber Baffle Outlet nozzle... [Pg.236]

Gas and liquid flow up along the membrane, then turn to the inlet of a narrow channel at the top of the chamber. This flow pattern enhances continuous replacement of electrolyte over the whole membrane surface. It is especially effective in eliminating gas stagnation at the top zone of the electrolysis area. The DAM-type system ensures that the fine-bubble flow is constant through its narrow channel and that smooth gas separation occurs at the outlet of the channel. Gas and liquid flow separately through an upper duct, an outlet nozzle and an outlet hose, then to a... [Pg.253]

Figure 7.21 Combined multifunctional impinging stream gas-liquid reactor. 1-tower 2-screen foam-remover 3-gas outlet tube 4-liquid outlet tube 5-gas conduit 6-eddy pressure nozzle 7-... Figure 7.21 Combined multifunctional impinging stream gas-liquid reactor. 1-tower 2-screen foam-remover 3-gas outlet tube 4-liquid outlet tube 5-gas conduit 6-eddy pressure nozzle 7-...
Figures 16.38 and 16.39 demonstrate that the form of the particle size distributions is once again almost constant during the process time, and consequently the pneumatic recycled dust is not used for seed production. Dust is deposited on the particles because the nozzle position is close to the dust recycle tube (uniform wetted dust), and this leads to an enlarged particle growth. The measured time-dependent gas outlet temperature and the measured time-dependent conversion corresponds with simulations (Fig 16.40). The bed mass growth is linear at constant liquid injection rates (Fig. 16.41). The change in particle size distribution value and of the Sauter diameter is, again, declining. Figures 16.38 and 16.39 demonstrate that the form of the particle size distributions is once again almost constant during the process time, and consequently the pneumatic recycled dust is not used for seed production. Dust is deposited on the particles because the nozzle position is close to the dust recycle tube (uniform wetted dust), and this leads to an enlarged particle growth. The measured time-dependent gas outlet temperature and the measured time-dependent conversion corresponds with simulations (Fig 16.40). The bed mass growth is linear at constant liquid injection rates (Fig. 16.41). The change in particle size distribution value and of the Sauter diameter is, again, declining.
The stainless steel reaction vessel was a horizontal tank 6 inches in diameter and 24 inches long (Figure 4). The humid gas was introduced to the vessel in a direction normal to the sodium pocket, thereby causing impingement on the sodium surface. A second inlet gas tap was provided into the side of the vessel for nonturbulent reaction studies. An outlet nozzle was located at each end of the reaction vessel in order to minimize gas channeling. Initial vessel temperature was controlled by voltage variation to externally woimd resistance heating wires. [Pg.72]

Concentrated HgS04is placed in an iron reaction vessel, which has one gas and two addition nozzles on top and one outlet nozzle... [Pg.220]

The HCIHX for the HTTP is a vertical helically-coiled counter flow type heat exchanger in which the primary helium gas flows on the shell side and the secondary in the tube side as shown in Fig.2. The major specification is shown in Table 1. The primary helium gas of the maximum 950°C enters the HCIHX through the inner tube In the primary concentric hot gas duct. It is deflected under a hot header and discharged around the heat transfer tubes to transfer primary heat to the secondary cooling system. It flows to the primary circulator via an upper outlet nozzle and returns between the inner and outer shell in order to cool the outer shell. [Pg.166]

Helium flowed through the inlet nozzle into the turbine section. Behind the compressor outlet helium flowed through the outlet diffiisor into the outlet nozzle and from there into the hot gas duct. Inside the turbomachinery only the inlet and outlet nozzles, the diffusors and the blading channel were exposed to high temperatures. All other sections of the machine (blade feet, rotor and housing) were cooled by means of the cooling gas system or the sealing gas system (see Fig. 8). [Pg.192]

Gas inlet and outlet nozzles of the equipment are designed to reduce pressure drop and to improve gas distribution. [Pg.21]

Orientation of aU nozzles for incoming and outgoing gas/liquid, e.g. gas inlet and outlet nozzles on HGF, heat exchanger (air preheater) ... [Pg.80]

Orientation of gas inlet and outlet nozzles shall suit existing plant ducts if possible. [Pg.170]

Refractory-/acid-resistant lining in gas inlet and oudet boxes shall be carried out by vendor to suit drain nozzles on the gas outlet boxes for draining out any (acidic) condensate. [Pg.171]

Size and orientations of gas inlet and outlet nozzles—(better if they suit gas ducts at site) internal lining of refractory/AR bricks in the enclosure for gases. Purchaser to make civil foundations suitable for the maximum weight and the overall dimensions (length, breadth, and height). Location of foundation bolts and any other supports shall be as per drawing given by vendor. [Pg.175]

Centrifugal separators cannot be sized with the F factor approach used with other types of separators because the maximum allowable velocity is a weaker function of gas density than the square root dependence in the F factor correlation. Maximum velocities for centrifugal separators depend upon the design and are different for each of the several manufacturer units. Pressure drop varies from 1 to 10 velocity heads depending upon the manufacturer. Velocity head should be based on inlet (outlet) nozzle velocity. [Pg.159]


See other pages where Gas outlet nozzles is mentioned: [Pg.194]    [Pg.194]    [Pg.686]    [Pg.233]    [Pg.233]    [Pg.194]    [Pg.194]    [Pg.686]    [Pg.233]    [Pg.233]    [Pg.1603]    [Pg.247]    [Pg.506]    [Pg.49]    [Pg.263]    [Pg.76]    [Pg.1425]    [Pg.355]    [Pg.1917]    [Pg.55]    [Pg.124]    [Pg.1907]    [Pg.506]    [Pg.1607]    [Pg.191]    [Pg.365]    [Pg.64]    [Pg.336]    [Pg.158]    [Pg.158]    [Pg.159]   
See also in sourсe #XX -- [ Pg.2 , Pg.219 ]




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