I’m seeking help from experts: how can I reduce pressure fluctuations in the system when starting up hydrogen production for the first time and switching to cyclic feeding mode for gas generation?

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This post was last edited by tt12345ss on 2016-5-13 at 16:35.
Prerequisites:
1) Once vulcanization is complete, the hydrogenation reactor is removed and pressure is maintained; the desulfurization reactor then continues with the N2 circulation for temperature increase. The process flow is as follows: K3001A (compressor) —— F3001 (preheating furnace) —— R3001 (hydrogenation reactor) —— R3002 (desulfurization reactor) —— E3005 (start-up cooler) —— D3002 (for start-up purposes) —— K3001A.
2) Once conversion and medium-voltage reduction are complete, the process flow is as follows: K3001B (compressor) —— F3002 (conversion furnace) —— R3002 (medium-voltage reaction reactor) —— E3002 (cooling) —— D3004 (liquid separation); after that, three-stage cooling and liquid separation take place —— K3001B.
3) The overall cycle of the plant is as follows: K3001A (compressor) —— F3001 (preheating furnace) —— R3001 (hydrogenation reactor) —— R3002 (desulfurization reactor) —— F3002 (conversion furnace) —— R3002 (medium-voltage reaction reactor) —— E3002 (cooling) —— D3004 (liquid separation); after that, three-stage cooling and liquid separation take place —— K3001A (compressor).
Question A: When cycles 1) and 2) operate simultaneously, i.e., two separate cycles, how can this be changed to an overall cycle in order to minimize pressure fluctuations in the system? B: What impact will reducing the load on Unit B first and then changing the process cycle have on the system, and what effect will it have on the conversion catalyst? C: What impact will changing the process loop first and then reducing the load on Unit B have on the system, and what effect will it have on the conversion catalyst? D: Please ask an expert to provide a more specific plan for making the changes! !