The process shown in Figure 1 is a steam-cracking process for ethylene production from an ethane-propane mixture. The process can be divided into three main parts: cracking and quenching; compression and drying; and separation.
Cracking and quenching. Initially, an ethane-propane mixture is fed to furnaces in which, under high-severity conditions, it is cracked, forming ethylene, propylene and other byproducts. The furnace outlet stream is subsequently fed to a water-based quench, to prevent further reactions and formation of undesirable byproducts.
From a decanter downstream from the quench tower, heavies, condensed dilution steam, tar and coke are removed. Cracked gas from the quench is then directed to compression and separation.
Compression and drying. The compression of the cracked gas is performed across five stages. After the third stage of compression, carbon dioxide and sulfur are removed from the cracked gas by caustic soda and water washes in a caustic scrubber. The compressed cracked gas is cooled and subsequently dried by molecular sieves that remove most of the water.
Separation. The dried cracked gas is fed to a cold box for the removal of hydrogen and light hydrocarbons, while minimizing ethylene losses.
At this point, condensates from the chilling train are fed to a series of separation columns. In the first column (demethanizer), methane is obtained from the top and further used in the cold box, while the bottom stream is fed to a second column (deethanizer).
The top of the deethanizer, composed primarily of ethylene and ethane, is fed to an acetylene converter and then fractionated in the C2-splitter. In this column, lights are removed from the overheads and recycled to the compression system, while polymer-grade (PG) ethylene is drawn from the column as a side stream. Ethane, from C2-splitter bottoms, is recycled to the cracking furnaces.
The deethanizer bottom stream is fed to a depropanizer, which distills C3 components in the overheads. This overhead stream is catalytically hydrotreated for methyl acetylene and propadiene removal, and then fed to the C3-splitter. In this column, lights are removed from the overheads and recycled to the compressors, while polymer-grade (PG) propylene is drawn from the column as a side stream. Propane from C3-splitter bottoms is recycled to the cracking furnaces. A C4+ stream is obtained from the depropanizer bottoms.
An economic evaluation of the process was conducted based on data from the first quarter of 2015, considering a facility with a nominal capacity of 1,700,000 ton/yr of ethylene constructed on the U.S. Gulf Coast.
Estimated capital expenses (total fixed investment, working capital and initial expenses) to construct the plant are about $2.37 billion, while the operating expenses are estimated at about $360 per ton of ethylene produced.
With a global nominal capacity of about 155 million ton/yr, ethylene is among the major petrochemicals produced worldwide. The major part of ethylene production is consumed in the manufacture of polyethylene, but ethylene is also applied in the production of ethylene oxide, ethylene dichloride and ethylbenzene (Figure 2).
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