Badger evaporator

Figure 5 illustrates a typical distillation train in a styrene plant. Benzene and toluene by-products are recovered in the overhead of the benzene—toluene column. The bottoms from the benzene—toluene column are distilled in the ethylbenzene recycle column, where the separation of ethylbenzene and styrene is effected. The ethylbenzene, containing up to 3% styrene, is taken overhead and recycled to the dehydrogenation section. The bottoms, which contain styrene, by-products heavier than styrene, polymers, inhibitor, and up to 1000 ppm ethylbenzene, are pumped to the styrene finishing column. The overhead product from this column is purified styrene. The bottoms are further processed in a residue-finishing system to recover additional styrene from the residue, which consists of heavy by-products, polymers, and inhibitor. The residue is used as fuel. The residue-finishing system can be a flash evaporator or a small distillation column. This distillation sequence is used in the Fina-Badger process and the Dow process. 

Heat Transfer from Various Metal Surfaces In an early work, Pridgeon and Badger [Jnd. Eng. Chem., 16, 474 (1924)] pubhshed test results on copper and iron tubes in a horizontal-tube evaporator that indicated an extreme effect of surface cleanliness on heat-transfer coefficients. However, the high degree of cleanhness needed for high coefficients was difficult to achieve, and the tube layout and... 

U.S. customary). Fragen and Badger [Ind. Eng Chem., 28, 534 (1936)] correlated overall coefficients on sugar and sulfite hquor in the same evaporator for viscosities to 0.242 Pa-s (242 cP) and found a relationship that included the viscosity raised only to the 0.25 power. 

Badger, W.L. Ind. Eng. Chem. 22 (1930) 700. The evaporation of caustic soda to high concentrations by means of diphenyl vapour. 

Badger, W. L. Heat Transfer and Evaporation (Chemical Catalog Co., 1926). 

Brooks, C. H. and Badger, W. L. Trans. Am. Inst. Chem. Eng. 33 (1937) 392. Heat transfer coefficients in the boiling section of a long-tube, natural circulation evaporator. 

T he late W. L. Badger s 40 years experience with commercial evaporators in the chemical industry has provided the basis for the economic production of fresh water from sea water. Five years ago, those familiar with sea water evaporation practice could predict minimum possible water costs no lower than about 1.60 per 1000 gallons. In 1955, the Office of Saline Water, U. S. Department of the Interior, commissioned W. L. Badger and Associates to study the minimum cost of making fresh water from sea water by using evaporator techniques of the chemical industry. Because previous estimates of water cost had been several times above the Office of Saline Water s goal, several optimistic assumptions served as a basis for this study ... 

Little work has been published on the effect of viscosity on heat transfer in the long-tube vertical evaporator. Cessna, Leintz, and Badger [Trans. Am. Inst. Chem. Eng., 36, 759 (1940)] found that the overall coefficient in the nonboiling zone varied inversely as the 0.7 power of viscosity (with sugar solutions). Coulson and Mehta [Trans. Inst. Chem. Eng., 31, 208 (1953)] found the exponent to be -0.44, and Stroebe, Baker, and Badger (loc. cit.) arrived at an exponent of -0.3 for the effect of viscosity on the film coefficient in the txriling zone. 

A series of articles, "Studies in Evaporator Design, by W. L. Badger, has also been published in 1920 and 1921 in Chemical and Metallurgical Engineering, Badger gives experimental data with special reference to the horizontal-tube evaporator. 

Figures 19 and 20 shows also a similar type of evaporator as constructed by Mantius and Badger, but in both cases the liquor is recirculated from the vapor body to the liquor chest, and is only discharged when it has reached the correct density.

---