Chemical Engineering Resources forum

A friend on another forum notified me that, Steve Hall , a member of this community passed away yesterday. His son placed his obituary on LinkedIn. He will be missed. Rest in peace, Steve.

A friend on another forum notified me that, Steve Hall , a member of this community passed away yesterday. His son placed his obituary on LinkedIn. He will be missed. Rest in peace, Steve.

​"When using HYSYS to calculate column internals for either a structured or random packed column, the calculated pressure drop is extremely low and falls below the lower limit. In this scenario, does it significantly impact the separation efficiency? Additionally, what is the appropriate percentage of column diameter to select when operating at the minimum vapor/liquid load

​"When using HYSYS to calculate column internals for either a structured or random packed column, the calculated pressure drop is extremely low and falls below the lower limit. In this scenario, does it significantly impact the separation efficiency? Additionally, what is the appropriate percentage of column diameter to select when operating at the minimum vapor/liquid load

Hello I would appreciate clarification on what “process temperature maintenance” means when specifying electric heat tracing. Consider a water-saturated gas entering a pipe at 35°C, with a water dew point of 35°C at the inlet pressure. If the specified heat-tracing maintenance temperature is 35°C: Does this refer to the pipe outer-wall temperature or the actual bulk fluid temperature? Does maintaining the pipe wall at 35°C ensure that the fluid remains at this temperature? As the gas flows, it may cool due to ambient heat losses and the Joule–Thomson effect as pressure decreases. Can heat tracing prevent water condensation under these conditions, considering that the dew point also changes with pressure? Would additional tracing duty or a temperature margin above the dew point be required? Is tracing for temperature maintenance primarily intended to keep stagnant fluid warm when flow stops, or is it also designed to maintain fluid temperature during continuous flow? What triggers the tracing to operate? Is it typically controlled by a sensor on the pipe wall beneath the insulation? How does this differ for self-regulating tracing?

Hello I would appreciate clarification on what “process temperature maintenance” means when specifying electric heat tracing. Consider a water-saturated gas entering a pipe at 35°C, with a water dew point of 35°C at the inlet pressure. If the specified heat-tracing maintenance temperature is 35°C: Does this refer to the pipe outer-wall temperature or the actual bulk fluid temperature? Does maintaining the pipe wall at 35°C ensure that the fluid remains at this temperature? As the gas flows, it may cool due to ambient heat losses and the Joule–Thomson effect as pressure decreases. Can heat tracing prevent water condensation under these conditions, considering that the dew point also changes with pressure? Would additional tracing duty or a temperature margin above the dew point be required? Is tracing for temperature maintenance primarily intended to keep stagnant fluid warm when flow stops, or is it also designed to maintain fluid temperature during continuous flow? What triggers the tracing to operate? Is it typically controlled by a sensor on the pipe wall beneath the insulation? How does this differ for self-regulating tracing?

​This is a natural gas molecular sieve dehydration process, and the red arrow points to a natural gas pre-cooling unit. Could you please specify what exact equipment this is? I haven't used this type of equipment before.

​This is a natural gas molecular sieve dehydration process, and the red arrow points to a natural gas pre-cooling unit. Could you please specify what exact equipment this is? I haven't used this type of equipment before.

For natural gas purification, the professional textbook is Gas Purification; is there a similar authoritative or specialized book available for natural gas liquefaction

For natural gas purification, the professional textbook is Gas Purification; is there a similar authoritative or specialized book available for natural gas liquefaction

In HYSYS, for horizontal vessel sizing, why do the calculated vapor space height and allowable velocity not match? For example, I set a maximum allowable velocity, and it gives a vapor space height and diameter. When I use that diameter to recheck the vapor velocity, the result is higher than the maximum allowable velocity I set. What is the reason? Is there a problem with my parameter input

In HYSYS, for horizontal vessel sizing, why do the calculated vapor space height and allowable velocity not match? For example, I set a maximum allowable velocity, and it gives a vapor space height and diameter. When I use that diameter to recheck the vapor velocity, the result is higher than the maximum allowable velocity I set. What is the reason? Is there a problem with my parameter input