The function of the flash tank
Thread Content
We use a 7-column low-temperature methanol washing process. The thermal regeneration tower is divided into two sections; the first section is the flashing section, with a controlled pressure of 1.0 MPa. But in practice, we control it at 0.25MPA. Because I think there’s no advantage to having such high pressure. Lower pressure increases the H2S concentration in the Claus gas, while also reducing the heat consumption of the thermal regeneration tower. What do everyone think?
Is your process Linde’s process? In the Lind process, the pressure in the regeneration tower is always around 0.25 MPa; it’s not as high as you mentioned. I’m hearing about the second stage of the regeneration tower for the first time; could I take a look at your process diagram? ?
Our set value for Luchi is 0.2 MPa; such a high set value corresponds to the pressure in the medium-pressure flash evaporation system.
Today, I’m analyzing why the acid gas removal tower contains 18% hydrogen – what could be the reason? Please ask an expert to help analyze it, thank you!
The original poster is referring to Luchi’s process, which is different from Linde’s. Let me share my opinion. Let me start by talking about the design principles. The design is determined based on the flash temperature; the goal is that at this temperature and pressure, almost all of what flashes off is carbon dioxide, with very little hydrogen sulfide – in fact, as little as possible. This is a reasonable approach. If you reduce the pressure, it’s inevitable that the concentration of hydrogen sulfide will increase. But this results in a lot of hydrogen sulfide being circulated. It will increase the load on the stripping tower; has there been any change in the temperature of the stripping tower? If possible, you can analyze the flash vapor. For reference only.