Regarding the reflux issue in the regenerator tower
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The amount of amine solution processed by the regeneration tower is only 1.2 t/h, and the amount of carbon dioxide regenerated is only 40 kg/h – this is a very small quantity. I would like to ask the experts the following questions: 1. What load is appropriate for the lean solution after amine regeneration? I have set it at 0.2 mol CO2/mol MEA; is this suitable? 2. I do not plan to use reflux in my regeneration tower; the steam from the reboiler and the carbon dioxide used for stripping are both removed from the top of the tower, while the rich solution enters at the top as well. The temperature of the rich solution inlet is set at 85 degrees. I intend to increase the height of the tower so that the rich solution can be used directly as reflux. After all the gases are removed, they go into a gas-liquid separator, and the liquid phase from this separator is used as make-up fluid, which is then fed into the heat exchanger between the lean and rich solutions. Is this approach acceptable? 3. If the plan is feasible, what appropriate temperature and pressure should be set for the vapor at the bottom of the tower? What would be the approximate amount of stripping vapor required? I have currently set the pressure at the bottom of the tower at 120 KPa and the temperature at 120 degrees – is that acceptable? Please, big brother, reply back. I’m begging you
1. The set value of the load needs to take into account the saturation of the amine solution and the removal efficiency, typically ranging from 0.1 to 0.3 mol CO2/mol MEA. 0.2 mol CO2/mol MEA is a relatively common load value in practical applications, but it still needs to be determined based on specific circumstances. 2. The plan is feasible, but attention must be paid to controlling the liquid level inside the tower to avoid the formation of liquid bubbles and dry sections. At the same time, the design of the gas-liquid separator must also be reasonable to ensure effective liquid phase recovery. 3. The settings for the steam temperature and pressure at the bottom of the tower need to be adjusted based on factors such as the liquid level inside the tower and the capacity of the condenser. Generally, a bottom pressure of between 100–180 kPa and a temperature of around 110–135°C are considered appropriate. The amount of stripping steam required needs to be calculated based on factors such as the amine solution concentration and the processing volume; it is generally recommended to keep this ratio within the range of 1:1.5 to 2. I hope the answer can help you solve the problem. .
Expert, I’m using a packed tower – is the liquid level that needs to be controlled the level in the bottom tank of the tower? Does a packed tower not require attention to dry plates? I am using 30% wt MEA as the absorbent, and I plan to reduce the loading from 0.4 to 0.2. How many kilograms of steam are required for a feed volume of 1 ton of rich liquid? Is a tower height of 7m appropriate? Thank you, expert:handshake