Solid content of slurry

The solid content of the slurry should be controlled at no more than 6 grams per liter.

It seems to be no more than 7g/l

Our initial target was 2 grams per liter, but if we try to control this value, we need to remove a much larger amount of slurry, which reduces the yield of the plant. Therefore, our current target is 8 grams per liter

Our control target is 2.0 kg/l, which is beneficial for the pipelines in the slurry system; primarily, we also control the viscosity of the slurry to keep it at or below 50

The control limit is no more than 2 grams per liter! If it is exceeded, it will cause wear and tear on the equipment, and accidents may even occur! If the solid content exceeds the limit, it is necessary to promptly analyze the reasons and find solutions!

It must be below 6; otherwise it will have a significant impact on your slurry pump. Due to coking of your flap valve, the solid content level will not be very good

We control it at 2 grams per liter, but as long as it’s no more than 6, that’s fine

The most commonly used parameter is quality, with the typical unit being ug/g; for us, it is ≯12

It should be kept below 6 g/l; high levels can cause blockages in pipelines and heat exchangers, as well as coking at the bottom of the distillation tower.

The general requirement is no more than 6 g/l. However, in actual production, the lower the solid content, the better. It can reduce blockages or inefficiencies in pipelines and heat exchangers, ensuring stable and continuous production. At the same time, it reduces wear on valves, pipelines, and pump bodies. We generally control the density of the slurry at 1000 g/cm3 and the solid content at 2 g/l; appropriately removing excess oil from the slurry is beneficial for production.

The control should be no more than 6, but given the poor quality of the raw materials currently available, along with the strategy of using agents to replace oil, the solid content is naturally very high; as a result, it’s necessary to increase the amount of material removed

1. I think the root cause of the solid content issue in the slurry is the problem of low centrifugation efficiency and issues with operational adjustments. . . 2. No matter how well a device is designed, it still has an operational threshold value. Once it’s reached, everyone just needs to avoid exceeding this value. 3. The technology for the separation of catalysts and regenerants in catalytic units is based on the principles of chemical engineering as well as the gas-solid two-phase separation techniques used in chemical reactors. 4. The main equipment used for gas-solid separation is the centrifugal separator, whose working principle is centrifugal sedimentation. 5. Each centrifuge has a range of optimal operating gas velocities determined by its designer; if the gas velocity exceeds or falls below this range, the centrifugal motion of the gas and catalyst particles inside the centrifuge will be disrupted. . . As a result, the gas-solid phases cannot be separated effectively; in other words, the gas does not escape easily and the solids do not settle properly. . . 6. When the processing capacity of the unit rises to a level close to the upper limit that the centrifuge can handle, since the inlet area of the centrifuge remains constant, the inlet gas velocity increases as the volume of gas increases. As a result, more solids are carried away by the gas, which is manifested as an increase in the solid content. Once the gas velocity exceeds its limit, the solids will no longer settle under the force of gravity; this can lead to serious consequences, such as the majority or all of the solids being carried into the distillation tower, or into the flue gas pipelines and exhaust systems. . . The consequences are not just the damage to the equipment. . . Everyone knows very well. . . What money can a company still make at this point? Isn’t this creating opportunities for profit for catalyst manufacturers, flue gas treatment equipment manufacturers, centrifuge manufacturers, and those who produce internal components for these devices? Hahaha. . . . :lol

I agree with your view to a large extent, but I have a question: you mentioned that the area of the centrifugal separation inlet is fixed. Can we increase the size of our modification? Because the counter-reactor is fixed. If the inlet area is increased, the pressure drop should decrease, right? Does it affect the operation? Thank you!

If the scale increase is not significant, the inlet area of the cyclone can be expanded while the cyclone itself remains unchanged.