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During the operation, the accuracy of the instrument was found to be insufficient, and the load could not reach the design capability. After replacing the dilution steam valve, desuperheating water valve and fuel gas valve, the production was normal. Due to the change of raw materials in the quench zone reconstruction, the capacity of the quenching zone was insufficient. In this transformation, a new water cooling tower was added in parallel. Quench oil tower: The upper section was changed to a packed tower, and the dilution steam tower was changed. One set of dilution steam generation system was added, two quench oil dilution steam generators were added, and one boiler feed pump was added.
The compression zone is rebuilt to increase one methane gas compressor, and the low-pressure methane originally returned to the compressor is pressurized by the compressor and sent to the human fuel gas system. Increase methane refrigeration compressors, three machines do not move. After accounting, the refrigeration capacity of ethylene is insufficient. In the separation zone, the top of the demethanizer tower is replaced with a packing, the top cooler tube bundle of the deethanizer tower is replaced with a high-efficiency heat exchange tube, the opening ratio of the distillation column of the ethylene distillation tower is increased, and the feed line position is moved upwards. The depropanizer tower and the debutanizer tower were replaced with large towers, and the depropanizer condenser and the propylene rectifier condenser were added.
The original design of the hydrogenation reform of gasoline was light because of the cracking raw materials, and the gasoline production was low. As the raw material becomes heavier, the output of naphtha increases, it is uneconomical to perform only one stage of hydrogenation, and the amount of processing is insufficient. Therefore, in 1997, a new 80kt/a gasoline hydrogenation unit was built. The process used full fraction hydrogenation and post-separation processes.
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