Process flow description The raw natural gas enters the inlet separator to filter out mechanical impurities and separate the free water, then enters the compressor after precision filtration by the dust filter, and is cooled to 40 ~ 45 ℃ by the cooler of the compressor itself, and then separates some water and heavy hydrocarbons (in case of excessive heavy components), and then enters the dehydration unit for deep dehydration. The dry feed gas from the dehydration skid enters the condensation separation skid, then it enters the refrigeration unit after precooling to ~ 10 ℃ through the heat exchanger. Next after cooling the feed gas to - 35 ℃ and cooling again through throttling, it enters the low-temperature separator for gas-liquid separation after The separated gas phase and liquid phase enter the deethanizer respectively, the tower top gas returns to the heat exchanger for reheating and output outside the boundary, and the tower bottom liquid enters the depropane and debutane tower for separation again. LPG at the top of the tower and stable light hydrocarbon at the bottom of the tower enter the storage tank respectively for loading and export. Scope of process flow Process flow scope of the unit: 1 compressor skid, 1 integrated skid (including raw material filtration and separation unit, pressure regulating and metering unit, dehydration unit and condensation separation unit), 1 refrigeration unit skid, 2 LPG Storage skids, 2 stable light hydrocarbon skids, two sets of truck crane pipes, 1 set of instrument air system, 1 set of instrument control system and separation tower skid，excluding circulating water system, flare and release system, power generation system, power supply and distribution and other public systems. Product and utility consumption Products and output When operating under the design basis conditions specified in Chapter 1, the output of LPG, stable light hydrocarbon and dry gas of the unit is as follows. Table LPG output of natural gas recovery unit Feed gas flow into the unit Calculated value of mixed hydrocarbon production remarks By masst/d Liquid volumem3/d Design flow: 5.0×104Nm3/d 12 24 Depending on intake air composition Molar content of LPG component: C3 + C4 ≥ 95%, C5 + ≤ 3% Table stable light hydrocarbon output of natural gas recovery unit Feed gas flow into the unit Calculated value of mixed hydrocarbon production remarks By mass t/dLiquid volume m3/dDesign flow: 5.0×104Nm3/d46.4Depending on intake air composition 40Saturated steam pressure ≤ 74kpa at ℃     Table dry gas output of natural gas recovery unit Feed gas flow into skid Calculated value of dry gas production remarks pressure MPaflow 104Nm3/dDesign flow: 5.0×104Nm3/d1.24.36