Pipe supports intermediate

The cost for piping covers labor, valves, fittings, pipe, supports, and othc rdtems involved in the complete erection of all piping used directly in the process. This includes raw-material, intermediate-product, finished-product, steam, water, air, sewer, and other process piping. Since process-plant piping can run as high as 80 percent of purchased-equipment cost or 20 percent of tied-capital investment, it is understandable that accuracy of the entire estimate can be seriously affected by the improper application of estimation techniques to this one component. 

Snuffing steam, which is used to suppress a fire in the header box in the convection or radiant sections, is supplied through local and remote manifolds. The remote manifold shoulcontrol stations are located along the pipe rack adjacent to die furnace. This particular fiimat uses manually controlled valves for each burner. The burner supply headers—fuel gas, fire steam, and fuel oil—are run... 

Minimum size of pipe is, sometimes dictated by structural considerations, i.e., l/i-inch Schedule 40 steel pipe is considered the smallest size to span a 15 to 20 pipe rack without intermediate support. 

Inorganic membranes employed in reaction/transport studies were either in tubular form (a single membrane tube incorporating an inner tube side and an outer shell side in double pipe configuration or as multichannel monolith) or plate-shaped disks as shown in Figure 7.1 (Shinji et al. 1982, Zaspalis et al. 1990, Cussler 1988). For increased mechanical resistance the thin porous (usually mesoporous) membrane layers are usually supported on top of macroporous supports (pores 1-lS /im), very often via an intermediate porous layer, with pore size 100-1500 nm, (Keizer and Burggraaf 1988). 

Anchor design is particularly important with high pressures and large pipe sizes because of the high thrusts that develop at end anchors. End anchors are so called because they occur at terminal points and at changes in direction of the pipe. At these points, the pressure acting on the inside area of the pipe would tend, if unrestrained by anchors, to pull an expansion joint apart. End anchors must absorb this pressure reaction as well as the forces required to activate the expansion joint and to overcome friction in supports and guides. Intermediate anchors, on the other hand, are subject to only the latter forces. 

Corrugated-pipe designs shown in Fig. 9-8b behave structurally as an intermediate between a bellow s joint and straight pipe They are also intermediate in price and require tie-rod support to keep the corrugations from straightening out under creep conditions. Such expansion designs are limited to short-expansion, straight-line requirements. 

The construction of the HTTR started in March 1991, with first criticality in 1997 to be followed after commissioning testing. At present the HTITI reactor building and its containment vessel have been constructed and its main components, such as a reactor pressure vessel, an intermediate heat exchanger, hot gas pipings and core support structures, have been installed in the containment vessel. Fuel fabrication has been started as well. 

The CEFR block is shown in Fig. 14.3 (Xu, 2008). It is mainly composed of a reactor cover, a sodium pool, and internal structures. The reactor cover is an approximately 2-m-thick steel-concrete structure that acts as the reactor upper shielding and provides support for the plug, main pumps, intermediate heat exchangers (IHXs), residual heat removal heat exchangers, and the circuits and pipes of various auxiliary systems. The driving mechanisms of control and safety, the fuel manipulator, and various measurement instruments are all fixed on the small plugs of the plug system. 

The primary circuit of the CEFR is composed of two main pumps, four intermediate heat exchangers, reactor core support diagrid plenum, pipes, and cold and hot sodium pools. In the cold pool, the two primary loops are separated from each other, but in hot pool they are linked up. In normal operation the average sodium temperature in the cold pool is 360°C and in the hot pool it is 516°C. Figure 2 shows the CEFR primary pipe. 

---