The filling factor problem for horizontal containers

This issue has already been discussed; check the relevant links.

Sometimes, the process data sheet will specify the elevation of the liquid level, and this can be used to calculate the filling coefficient; generally speaking, however, this consideration is minimal

Some items were found in the relevant section; it’s not clear whether they are what the original poster was looking for. Please refer to Article 36: The design storage capacity of pressure vessels used to store liquefied gases shall comply with the following regulations: 1. For fixed pressure vessels that contain liquefied gases (including liquefied petroleum gas), the design storage capacity shall be calculated using the following formula: W = φVρt. Here, W represents the storage capacity, and t represents time. φ is the filling coefficient, which is generally set at 0.9; for vessels whose volume has been determined experimentally, this value can be higher than 0.9, but it must not exceed 0.95； 　　V — Volume of the pressure vessel, m3 ； 　　ρt —— density of the saturated liquid at the design temperature. 　　2. The maximum allowable filling volume of a mobile pressure vessel with a liquefied gas as the medium shall be calculated using the following formula: W = φvV Where: W – the maximum allowable filling volume of the vessel, in tons; φv – the filling volume per unit volume, determined based on 8% of gas space remaining in the vessel at 50°C and the density of the medium at that temperature, in t/m3; V – the actual volume of the vessel, in m3. 　　The design pressure, corrosion margin, and filling volume per unit volume for the common media in mobile pressure vessel tanks are selected according to Table 3–3. 　　Table 3-3 Design pressure, corrosion margin, and filling volume per unit volume for common media Design Pressure Corrosion Margin Filling Volume per Unit Volume MPa mm t/m3 Liquid ammonia 2.16 2 0.52 Liquid chlorine 1.62 4 1.20 Liquid sulfur dioxide 0.98 4 1.20 Propylene 2.16 1 0.43 Propane 1.77 1 0.42 Saturation vapor pressure at 50°C Greater than 1.62 Ata 2.16 1 0.42 Other cases 1.77 1 0.42 n-Butane 0.79 1 0.51 Isobutane 0.79 1 0.49 Butene, isobutene 0.79 1 0.50 Butadiene 0.79 1 0.55

Generally, this needs to be taken into consideration; the same is true for vessels at atmospheric pressure