Key issues concerning the long-term operation of catalytic units at 60%~70% load
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Dear colleagues: If the unit operates at a load level of 60%~70% for an extended period of time, what issues must be addressed and given special attention in the case of heavy oil catalytic units? Device description: The CSIC MIP process is implemented in a high-and-low configuration, with two stages of regeneration – one lean and one rich. Two downstream external heat exchangers are installed, and a mixed feed of hydrogenated heavy oil and hydrogenated wax oil is used. The distillation unit features top circulation, rich and lean absorption oil streams, primary intermediate stream, secondary intermediate stream, and slurry circulation. Absorption stability is consistent with the conventional value ； There are three units: the flue gas extractor, the main fan, and the motor; as well as a backup fan and motor unit. There are two CO boilers, SCR denitration systems, and DEV wet desulfurization systems.
There are two main hazards associated with long-term operation at low load: one is the lower processing capacity, and severe coking occurs in some areas； Instead, the processing capacity is low; some pumps operate at low load for extended periods, which can lead to wear of the impeller. If not properly controlled, vacuum issues may arise.
What do you mean by severe coking in some areas?
Hey, how is the MIP running for your team? How user-friendly is the device?
Our unit has not been started yet; the Phase 1 MIP unit is operating well.
Is it the MIP-CGP process? What is the octane rating of gasoline, and by how much is the yield of liquefied gas higher than that of conventional catalytic cracking?
It is the MIP-CGP process, with an octane number of MON: 82 and RON: 92. No cross-comparison has been done; the properties of the raw materials are different. Only qualitative assessment is possible, not quantitative.
The minimum load is generally set at 60% in terms of design considerations; personally, I think it would be better to aim for a higher value – 70% would be ideal. This way, the product is more likely to meet the requirements and is easier to operate. Several issues to consider: 1. Nozzle atomization effect; for low processing volumes, it is necessary to increase the atomized steam. 2 To increase the tube reaction time, it is necessary to follow the principles of catalytic cracking and prevent excessive cracking. Even though it’s a MIP, this factor still needs to be taken into account; it’s necessary to get the research institutions and design firms to cooperate. Of course, if there are experts available or if one is an expert oneself, it’s possible to carry out the calculations oneself. 3 The linear velocity of the cyclone separators in the settler and regenerator, or even those with three cyclones, must be maintained above the minimum linear velocity. If necessary, reduce the pressure in the reaction regenerator system and the distillation system.
When operating at 60%~70% load for extended periods, the pressure drop in the filtration section of the EDV flue gas desulfurization unit is insufficient, resulting in inadequate removal of SO3; this causes blue smoke to emerge from the chimney
If the unit is operating at full capacity and the pressure drop across the filtration module is sufficient, does blue smoke appear from your company’s chimney?