Converter temperature control
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In coal water slurry gasification, the excessive temperature in the shift converter leads to high inlet temperatures that cannot be controlled; moreover, the steam-to-water ratio in the gasification process is also high – it is designed to be 1.4, but the actual value reaches 1.45. All the bypass lines for the inlet and outlet heat exchangers are also open. It’s unclear whether this is a design issue or something else; the cause cannot be determined. . . .
Are there inlet and outlet isolation valves on the heat exchange tubes and the shell side? If so, the temperature of the water-gas at the inlet of the shift converter can be reduced by closing the valve for the hot process gas. It would be helpful to include a flow diagram to facilitate a better analysis of the reasons.
Has there been any change in the composition of the feed gas? Such as oxygen content
There should be a waste boiler in the middle; is the design of this waste boiler unreasonable (with too small a size), resulting in low steam production? Is it causing less heat of reaction to be transferred out? Or, as mentioned above, the main line of the heater for the imported raw gas should generally be equipped with a valve; it is possible to try reducing the flow rate slightly, but the pressure difference across the entire system should remain the key factor to consider
Do you mean to turn down the main line of the heat exchanger so that more gas flows through the secondary line? We tried this method; when I turned off the main flow, the inlet temperature increased. My analysis is that the volume of gas passing through the heat exchanger was too low, which resulted in a higher temperature on the exit side of the heat exchanger. What you suggested doesn’t work. . .
That makes sense; I think there are some issues with the design of that waste boiler
Or could it be that I turned it down too much? ? ? ?
It’s still a problem with the heat exchanger; the bypass line of the heat exchanger is too small.
How many sections are there in a converter? How is the temperature drop between segments? How many years has it been in use? Has the hotspot moved down to the end already? If it is a CoMo catalyst, with a high bed temperature and large steam volume, has this created a vicious cycle? Has the desulfurization activity of the catalyst in the upper section decreased significantly, causing the reaction to shift downward? A comprehensive analysis is recommended.
A new catalyst or? Is the vulcanization complete? It seems that the temperature rises excessively as soon as air gets in