Process piping plan

Valve Pits - Process Piping Plan - Sections and Details Process Water Pipe Tunnel - Support Details and Piping... 

It can be concluded that selection of proper material or lining for seawater application is important and depends on the criticality of the system, availability of standby system/equipment and availability of isolation devices for maintenance. For process piping in seawater application the success of proper lining or coating material depends on the suitability for in-situ/field application and the proper corrosion monitoring plan. 

Figure 12 shows the plan and elevation views of a process unit piping (9). A dmm is supported off the piperack. Heat exchangers are located far enough back from the support columns so that they are accessible and their shell covers can be removed. Pumps are located underneath the piperack, but sufficient room is provided for maintenance equipment to access the motors and to remove the pump if necessary. The motor is always oriented away from the process equipment and located on that side of the piperack. Instmment valve drops are shown supported from the columns. The instmment trays themselves mn on the outside of the support columns. Flat turns are only made from the outside position of the piperack. Nozzle-to-nozzle pipe mns are made whenever possible. Larger lines are located on the outside of the piperack. Connections to nozzles above the rack are made from the top... 

Environmental factors should also be incorporated into a company s technical or research and development program. Since the planning horizons for new projects may now extend to 5 to 10 years, R D programs can be designed for ecific projects. These may include new process modifications or end-of-pipe control technologies. 

In transporting this water through insulated pipes to the process equipment, it is good practice to allow a 2°F temperature rise when planning heat transfer calculations. 

To ensure that the water flows through the whole of the system as smoothly as possible and with the minimum of turbulence, it is vital that the layout of pipework should be planned before fabrication starts. It should not be the result of haphazard improvisation to avoid more and more obstacles as construction proceeds. Pipe runs should be minimised or run as directly as possible with every effort made to avoid features that might act as turbulence raisers. For this reason the number of flow controllers, process probes, bends, branches, valves, flanges, intrusive fittings, or mechanical deformation or damage to the pipework, should be kept to a minimum. 

Hazard and Operability Analysis (Hazop) (Kletz, 1992) is one of the most used safety analysis methods in the process industry. It is one of the simplest approaches to hazard identification. Hazop involves a vessel to vessel and a pipe to pipe review of a plant. For each vessel and pipe the possible disturbances and their potential consequences are identified. Hazop is based on guide words such as no, more, less, reverse, other than, which should be asked for every pipe and vessel (Table 1). The intention of the quide words is to stimulate the imagination, and the method relies very much on the expertise of the persons performing the analysis. The idea behind the questions is that any disturbance in a chemical plant can be described in terms of physical state variables. Hazop can be used in different stages of process design but in restricted mode. A complete Hazop study requires final process plannings with flow sheets and PID s. 

Proper planning is a delicate process because public health measures are rarely noticed or appreciated (like buried utility pipes, they are often hidden functions) except when they fail—then they are very visible. Consumers are particularly upset by unsafe (contaminated) environmental media (water, air, and/or soil) because they are often viewed as entitlements—and indeed, it is reasonable for consumers to expect a high-quality, safe environment. Public health failures during response to contamination threats often take the form of too much or too little action. The results of too little action, including no response at all, can have disastrous consequences potentially resulting in public injuries or fatalities. On the other hand, a disproportionate response... 

All piping components furnished by the vendor that are shown in Figure D-2 and Figure D-3, Plans 52-54, are considered subject to the process fluid. 

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