The design pressure of the shell side of the heat exchanger has been increased. Should the design pressure of the connected pipelines be increased?
Thread Content
This post was last posted by a man in black with a sword on 2026-7-11 21:12 Editing a project, a heat exchanger, the shell side operating pressure is only 0.47mpag, and the tube side operating pressure is 2.5mpag. It seems to be based on the 2/3, 10/13 regulations of some heat exchangers, that is, the design pressure of the shell side is not lower than 2/3 or 10/13 of the tube side, etc. In the past, a large design institute used 0.8, so the design pressure of the shell side is 2.0mpag. There is a requirement that the design pressure of the pipeline cannot be lower than the design pressure of the connected equipment. The design pressure of the pipelines before and after the shell side of the heat exchanger should not be considered as 2.0mpag. But I looked at their pipeline table and the design pressure of the pipeline is only 1.0mpag. It does not matter about 2.0mpag. Guys, can you tell me what the situation is now? Is the above approach correct? Or am I understanding it wrong? Chemical Industry Discussion
When the design pressure on the shell side of the heat exchanger increases, the design pressure of the connected pipelines does not necessarily have to increase simultaneously. It needs to be recalculated and determined based on the actual maximum possible pressure that the pipelines bear (including fault conditions).