·MDEA Decarbonization Process Description:
The feed gas is filtered through a separator and enters the bottom of the absorption tower, where it contacts lean MDEA solution sprayed from the top in a countercurrent flow. CO₂ and H₂S are selectively absorbed. The rich solution is depressurized in a flash tank to remove hydrocarbons, preheated in a lean rich solution heat exchanger, and then enters the top of the regeneration tower. Under steam stripping in the reboiler, CO₂ and H₂S are desorbed. The regenerated lean solution is exchanged, cooled, and pumped back to the absorption tower for circulation. The acid gas from the top of the tower can be sent to sulfur recovery or CO₂ liquefaction units.
·Molecular Sieve Dehydration Process Description:
After decarbonization, the raw gas enters adsorption Tower A, where water is selectively adsorbed by the molecular sieve bed. The outlet dry gas has a water dew point ≤ -60°C and is sent downstream. After adsorption saturation, Tower B switches to the regeneration process: dry gas or nitrogen is heated in a heater and used for reverse purging of the molecular sieve bed. The desorbed water is condensed and separated in a cooler. Subsequently, cold dry gas is used for forward cooling of the bed to 40°C, completing regeneration for standby. The dual towers automatically switch via programmed valves, with a cycle time of 8–12 hours.
·Low-Temperature + Temperature Swing Adsorption (TSA) Process Description:
After molecular sieve dehydration, the raw gas enters a plate-fin heat exchanger for precooling, causing partial condensation of C₅+ heavy hydrocarbons. It is then deeply cooled by a turbo-expander or mixed refrigerant, and oil phase (recovering LPG/NGL) is separated in a low-temperature separator. Residual heavy hydrocarbons in the gas phase enter the TSA molecular sieve adsorption tower, where heavy hydrocarbons are selectively adsorbed. The outlet gas, with heavy hydrocarbon content ≤ 20 mg/Nm³, is sent to the liquefaction unit. After adsorption saturation, heated purified gas is used for reverse purging regeneration. The desorbed heavy hydrocarbons are cooled and recovered, and the regeneration gas is used as fuel gas.
·Cryogenic Distillation for Nitrogen Removal:
After dehydrocarbonization, the raw gas exchanges heat with top nitrogen and bottom methane in the precooling section to lower its temperature and partially remove heavy hydrocarbons. It then enters the main cooler, where it is deeply cooled to -162°C by a DMR mixed refrigerant and enters the middle of the nitrogen removal tower. The top nitrogen is fully refluxed in the condenser, while the bottom methane is vaporized in the reboiler and rises, completing distillation separation. The bottom methane is reheated to ambient temperature and exported as product gas. The top pure nitrogen gas is used as fuel gas after recovering cold energy in the expander, achieving self-balance of cold energy.
·Manufacturing, Installation, and Commissioning Period:
Modularized for factory assembly and on-site installation, ensuring efficient product delivery. The total project duration from contract signing to successful commissioning is 7 months.
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From initial design to final commissioning, every deadline was met with precision—working with this team made our LNG expansion project a complete success.
Their ability to source and deliver high-quality turbines and compression units ahead of schedule kept our entire plant overhaul on track and under budget.
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