Let’s work on a few questions related to restructuring together
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1. The test results for the initial boiling point of the reformation feed show 75°C; how should the operations be adjusted to meet the process specification requirement of an initial boiling point greater than 80°C? 2. The hydrogen sulfide content in the reforming cycle hydrogen is 8 ppm, and the hydrogen chloride content is 0.5 ppm. Based on these analysis results, how should you adjust the operations? 3 How should a leak in the pre-hydrogenation heat exchanger be handled?
1. Under constant column pressure, control the bottom and top temperatures of the pre-hydrogenation fractionation tower in order to separate components with a initial boiling point of less than 80 degrees. 2. When the bed temperature drops below 480 degrees, identify the source of sulfur; increase the chlorine injection amount accordingly. 3. There is a leak in the pre-hydrogenation heat exchanger; use oil stored in the tank area instead of refined naphtha. Stop operations for repairs on the pre-hydrogenation unit while ensuring normal operation of the reforming unit.
For question two, I’d like to add that it’s necessary to check whether the water-chlorine balance is appropriate If there is too much water, the system should enhance dehydration; chlorine injection should remain unchanged
1. Adjust the bottom temperature of the stripping distillation column to an appropriate level. 2. Increase desulfurization in the pre-hydrogenation section, and appropriately lower the temperature and increase chlorine injection in the reforming section. 3. The pre-hydrogenation section must definitely be shut down for maintenance.