Abstract
Plenty of thermal explosions and runaway reactions of cumene hydroperoxide (CHP) were described from 1981 to 2010 in Taiwan. Therefore, a thermal explosion accident of CHP in oxidation tower in 2010 in Taiwan was investigated because of piping breakage. In general, high concentration of CHP for thermal analysis using the calorimeter is dangerous. Therefore, a simulation method and a kinetic parameter were used to simulate thermal hazard of high concentrations of CHP only by the researcher. This study was applied to evaluate thermal hazard and to analyze storage parameters of 80 and 88 mass% CHP using three calorimeters for the oxidation tower, transportation, and 50-gallon drum. Differential scanning calorimetry (DSC) (a non-isothermal calorimeter), thermal activity monitor III (TAM III) (an isothermal calorimeter), and vent sizing package 2 (VSP2) (an adiabatic calorimeter) were employed to detect the exothermic behavior and runaway reaction model of 80 and 88 mass% CHP. Exothermic onset temperature (T 0), heat of decomposition (ΔH d), maximum temperature (T max), time to maximum rate under isothermal condition (TMRiso) (as an emergency response time), maximum pressure (P max), maximum of self-heating rate ((dT/dt)max), maximum of pressure rise rate ((dP/dt)max), half-life time (t 1/2), reaction order (n), activation energy (E a), frequency factor (A), etc., of 80 and 88 mass% CHP were applied to prevent thermal explosion and runaway reaction accident and to calculate the critical temperature (T c). Experimental results displayed that the n of 80 and 88 mass% CHP was determined to be 0.5 and the E a of 80 and 88 mass% CHP were evaluated to be 132 and 134 kJ mol−1, respectively.
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Abbreviations
- A :
-
Frequency factor, sec−1 M1−n
- C p :
-
Liquid specific heat at constant pressure, kJ kg−1 °C−1
- C 0 :
-
Initial concentration, mol L−1
- E a :
-
activation energy, kJ mol−1
- K :
-
Pre-exponential factor, s−1
- M :
-
Mass of reactant, g
- P max :
-
Maximum pressure during overall reaction, psig
- Q :
-
Calorific capacity, J g−1
- \( \dot{Q} \) :
-
Heat flow, W g−1
- R :
-
Gas constant, 8.314 J mol−1 K−1
- S :
-
Wetted surface area, m2
- SADT:
-
Self-accelerating decomposition temperature, °C
- T :
-
Temperature, °C
- T A :
-
Final adjusted temperature, K
- T A0 :
-
Initial adjusted temperature, K
- T f :
-
Final temperature, °C
- T M :
-
Final measured temperature, K
- T max :
-
Maximum temperature during overall reaction, °C
- T M0 :
-
Initial measured temperature, K
- T NR :
-
Temperature of no return, °C
- T wall :
-
Temperature on the wall, °C
- TMRad :
-
Time to maximum rate under adiabatic system, min, hr
- U :
-
Heat transfer coefficient, kJ min−1 m−2 K−1
- a:
-
Vessel wetted surface area, m2
- k i :
-
Rate at stage i, s−1
- m :
-
Mass of reactor, kg
- n :
-
Order of reaction, dimensionless
- α:
-
Degree of conversion, dimensionless
- β:
-
Heating rate, °C min−1
- λ:
-
Heat conductivity, J ms K−1
- ϕ:
-
Thermal inertia, dimensionless
- △H d :
-
Heat of decomposition, J g−1
- (dT/dt):
-
Self-heating rate, °C min−1
- (dT/dt)A :
-
Actual self-heating rate, °C min−1
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Wu, SH., Wu, JY., Wu, YT. et al. Explosion evaluation and safety storage analyses of cumene hydroperoxide using various calorimeters. J Therm Anal Calorim 111, 669–675 (2013). https://doi.org/10.1007/s10973-012-2570-5
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DOI: https://doi.org/10.1007/s10973-012-2570-5