Catalyzed pre-lift dry gas volume

In my opinion, it depends on the processing capacity of the device’s dry gas absorption and reabsorption system, the properties of the raw materials, as well as the load on the compressor.

From multiple perspectives, optimize the operating conditions to determine whether to use pre-lift dry gas, as well as the control amount for the pre-lift dry gas.

Has it been put into use there yet? What is the ratio to steam?

Can using pre-heated dry gas yield significant results? In what ways can this be evident?

https://bbs.hcbbs.com/forum.php?mod=viewthread&tid=633898 When you recommended those materials for fellow sailors to learn*, don’t forget about them yourself.

What our company is currently using normally is pre-heated dry gas, in an amount of around 8,000 Nm3. This may need to be adjusted based on the feed rate, feed temperature, and the properties of the crude oil. I’m not quite sure about the details either; it’s a workshop, but it’s not a specific position.

There is a certain gap between theory and practice

What was said on the second floor is correct. I set the pre-lift medium flow at 7,000 NM3/h; it is used primarily to reduce steam consumption. By increasing the pre-lift dry gas flow to 1,000 NM3/h, the amount of steam required for pre-lifting is reduced accordingly. However, the steam flow cannot be completely stopped – 500 NM3/h must remain. The amount to be used is determined primarily by the reaction conditions, the pressure compressor, absorption stability, and system gas operations. For example, increasing the pre-raised dry gas by 1000 NM3 will raise the reaction pressure; it is then necessary to check whether there is enough head difference between the two vessels. Increasing the speed of the pressure compressor can help address this issue, but there is a limit to how much the speed can be increased – once that limit is reached, it determines one of the conditions for the maximum amount of pre-raised dry gas that can be used ； Looking at the absorption and stabilization process again, if the operating conditions remain unchanged, increasing the pre-heated dry gas flow rate by 1000 NM/h is equivalent to creating a backflow effect; this leads to an increase in the amount of rich gas at the inlet of the absorption tower, a decrease in the amount of lean gas at the outlet, and an increase in the amount of dry gas at the outlet of the reabsorption tower. However, the amount of dry gas after desulfurization remains largely unchanged. If the speed of the compressor is increased, all these values will increase even further, and the linear velocity within the absorption tower will rise as well. In such cases, the absorption efficiency deteriorates, resulting in the dry gas not meeting the required C3 standards. To improve the absorption efficiency, factors such as the equipment and the system also play a role in determining how much pre-heated dry gas should be used ； Furthermore, it is determined by issues such as quality problems that arise from the increased load on the desulfurization system, as well as the need to achieve a balance in the amount of dry gas produced by the unit ； A proper value can be achieved through reasonable combination and adjustment of these factors; each case needs to be analyzed on its own. I think there is room to use it appropriately from the perspective of reducing energy consumption, but going beyond that limit is pointless and may even have the opposite effect. The above are purely personal opinions.