Equipment Layout

The manner is which an exchanger is piped up influences its performance. Horizontal units should have inlet and outlet nozzles on the top and bottom of the shell or channel. Nozzles should not be on the horizontal centerline of the unit. In general, fluids should enter the bottom of the exchanger and exit at the top, except when condensation occurs. Units are almost always designed to be counterflow and the piping must reflect this. When concurrent flow has been specified, it is equally important that equipment be piped to suit. For multipass units, the shellside fluid can be admitted at either end of the shell without affecting the thermal performance. However, for some cases better distribution or mechanical reliability can be achieved with the inlet nozzle at a specific location. 

By anticipating potential problems, the designer can avoid high maintenance or cleaning expenses and costly shutdowns. To anticipate maintenance problems, the designer needs to be familiar with the plant location, process flowsheet, and anticipated plant operation. Some of the questions that must be considered Include  

---

Potassium Carbonate Process. The potassium carbonate process is similar to the sodium carbonate process. However, as potassium bicarbonate [298-14-6] is more soluble than the corresponding sodium salt, this process permits a more efficient absorption than the other. The equipment layout is the same and the operation technique is similar. 

Design equipment layout to accommodate emergency needs—response, ingress, egress... 

Vapor Cloud Explosion (VCE) Explosive oxidation of a vapor cloud in a non-confined space (not in vessels, buildings, etc.). The flame speed may accelerate to high velocities and produce significant blast overpressure. Vapor cloud explosions in plant areas with dense equipment layouts may show acceleration in flame speed and intensification of blast. 

Even, limited PSAs use and contain much information. This information may come as memos and process reports and flow sheets, equipment layout, system descriptions, toxic inventory, hazardous chemical reactions, test, maintenance and operating descriptions. From this, data and analyses are prepared regarding release quantities, doses, equipment reliability, probability of exposure, and the risk to workers, public, and environment. An executive summary analysis is detailed, and recommendations made for risk reduction. Thus the information will be text, calculations of envelope fracture stresses, temperatures, fire propagation, air dispersion, doses, and failure probabilities - primarily in tabular form. 

It is extremely poor economic practice to fit the equipment layout too closely into a building. A slightly larger building than appears necessary will cost little more than one that is overcrowded, yet the extra cost will be small in comparison to the penalties that will result if, to iron out the kinks, the building must be expanded. 

The most conuiion cause of fire accidents in process plants is equipment failure. Tliis is primarily a result of poor equipment maintenance or poor equipment layout and design. Maintenance perfonned according to a detailed and well structured schedule will significantly reduce tlie occurrence of fire accidents. Tlie second largest cause of fire accidents is ignorance of tlie properties of a specific chemical or chemical process. Proper training of employees will increase tlieir knowledge of tlie properties of a specific chemical and chemical process and can prevent many of tliese chemical fire accidents. 

The equipment layout must be devised to ensure proper circulation of acid, not only from drum to drum, but also from the headers. This may require additional pumps, the use of a manifold, or the moving of hoses from one leg to another. 

Equipment layout is also crucial, with consideration given to ... 

The table of stream flows and other data can be placed above or below the equipment layout. Normal practice is to place it below. The components should be listed down the left-hand side of the table, as in Figure 4.2. For a long table it is good practice to repeat the list at the right-hand side, so the components can be traced across from either side. 

To assess the potential hazard of a new plant, the index can be calculated after the Piping and Instrumentation and equipment layout diagrams have been prepared. In earlier versions of the guide the index was then used to determine what preventative and protection measures were needed, see Dow (1973). In the current version the preventative and protection measures, that have been incorporated in the plant design to reduce the hazard-are taken into account when assessing the potential loss in the form of loss control credit factors. 

In the discussion of process and equipment design given in the previous chapters no reference was made to the plant site. A suitable site must be found for a new project, and the site and equipment layout planned. Provision must be made for the ancillary buildings and services needed for plant operation and for the environmentally acceptable disposal of effluent. These subjects are discussed briefly in this chapter. 

Surface runoff should be considered coincident with equipment layout. If surface runoff from one area goes directly to another area the feature of separation has be lost. 

Equipment layout, 19 494-495 Equipment leaks, emissions from,... 

Theoretical analysis and motion simulation work has resulted 1n a basic understanding of fluid motion Inside process equipment. In turn, the specific affects In two and three phase separators, treaters, glycol dehydrators and other process equipment has been analyzed. This research has lead to the establishment of process equipment sizing criteria for all types of vessel motion transmitted from the marine vessel, also the designs of baffling and other Internals to dampen and control the fluid motion have been established together with the optimization of equipment layout on marine vessels. 

Based on this gradation, the most critical process equipment (Category 1) needs to be placed as near as possible to the center of gravity, resulting In the Idealized equipment layout shown 1n Figure 6. 

Pressurized Vertical-Vessel Coalescer. Pressurized influent is pumped into a vertical vessel maintained at a gauge pressure of about 30 psi (200 kPa], The vessel is fitted with coalescer cartridges. The equipment layout is compact, requiring little floor space. The main disadvantage is that for specified duty conditions, it needs a continuously operating SO-hp [40-kW pump. Any breakdown of the pump set would result in complete unit shutdown. The operating... 

The nitric acid plant is relatively small and should not occupy more than 1 hectare. Even this small area should leave plenty of room for expansion. Figure 5.5 shows the equipment layout for the nitric acid plant. The plant layout includes space for a parallel production train should the market expand sufficiently in thefuturesuch that a second plant is required. 

In order to minimize dialkylation of the amino group, 5-BrASA was added to a large excess of the R-amine. This necessitated the engineering of a simple countercurrent toluene extraction system for recycle of the excess R-amine. This first reaction step was studied at a variety of temperatures, concentrations, excesses of R-amine and extraction conditions. The process was monitored by HPLC. In summary, the following outlines the optimum process to the sodium salt of R-aminoketone (X)—Scheme 7. The plant equipment layout is shown in Figure 1. 

---