hollerg
Chemical
- Mar 22, 1999
- 97
I am renovating an existing evaporator to run at a lower pressure, but at a higher level of moisture removal from an organic acid, resulting in both higher bulk temperature, and higher tube wall temperature. I have a minor component that forms from thermal degradation with first order kinetics. I want to ensure I have essentially the same concentration of the minor at the higher temperatures. The minor is not volatile
I know I need to minimize the liquid inventory but once that is minimized how do I factor in the contribution of the tube wall temperature? The degradation doubles for every 10 C rise in T. I think I need a relationship to apportion the relative contribution of the damage the heat exchanger surface temperature causes and the degradation in the bulk @ the flash temperature.
The evaporator uses an external heat exchanger, with a 100 to one circulation to product discharge rate and a 50 to one inventory to product discharge rate. Temperature rise is only one degree C in each pass. Back-pressure suppresses boiling in the tubes to prevent salts from fouling the surface.
I am considering setting up the reaction model to be two parts: 1) A mixed-flow reactor (CSTR) to account for the reaction at bulk T. 2) A second mixed-flow reactor at the temperature of the wall and limiting the volume of the second reactor to the thickness of 1/64th of an inch to represent the reaction. Only @ ~ 6000 Re#, 14 cP fluid.
Thanks in advance for your constructive comments and suggestions.
(I would lower the vacuum level further and operate colder, but precipitation would occur.)
Gary
I know I need to minimize the liquid inventory but once that is minimized how do I factor in the contribution of the tube wall temperature? The degradation doubles for every 10 C rise in T. I think I need a relationship to apportion the relative contribution of the damage the heat exchanger surface temperature causes and the degradation in the bulk @ the flash temperature.
The evaporator uses an external heat exchanger, with a 100 to one circulation to product discharge rate and a 50 to one inventory to product discharge rate. Temperature rise is only one degree C in each pass. Back-pressure suppresses boiling in the tubes to prevent salts from fouling the surface.
I am considering setting up the reaction model to be two parts: 1) A mixed-flow reactor (CSTR) to account for the reaction at bulk T. 2) A second mixed-flow reactor at the temperature of the wall and limiting the volume of the second reactor to the thickness of 1/64th of an inch to represent the reaction. Only @ ~ 6000 Re#, 14 cP fluid.
Thanks in advance for your constructive comments and suggestions.
(I would lower the vacuum level further and operate colder, but precipitation would occur.)
Gary