Problems with installing double-flange level gauges on liquefied hydrocarbon spheres
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There is a 3,000-cubic-meter liquefied hydrocarbon spherical tank cluster on site; no rotating ladders or maintenance platforms are installed on the tanks, instead a combined platform is provided at the top of the tank cluster. If double flanges are used, the capillary tube must be at least 20 meters long. I checked the specifications of major transmitter manufacturers, and none offer tubes of such length; even in the case of custom orders, it’s difficult to obtain accurate specifications. Dear experienced sea travelers, how should this situation be handled? What will be the measurement results if a single-flange level transmitter is installed at the lower end of the connecting pipe, with the negative pressure chamber connected to the vapor phase at the upper end of the connecting pipe? Is it similar in effect to a double flange design? If the effects are similar, it should cost less to implement than a double flange design, right? Due to the limited investment by the owner, a setup of one servo and one differential pressure sensor is the only way to achieve remote measurement of liquid level with two sensors; therefore, it is not advisable to recommend radar and servo combinations. There’s nothing to do.
Reply to 1# hwindforce: If you have a servo, you generally rely on the servo level gauge for monitoring. However, if you use a single-flange transmitter, then you need to run a pressure guide tube from the top of the spherical tank to the single-flange negative-pressure type transmitter. This approach is cheaper in terms of cost, but you need to take into account issues such as blockages and interruptions in flow that can occur with the negative-pressure type transmitter.