INDUSTRIAL A N D ENGINEERING CHEMISTRY
1184
Vol. 44, No. 5
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350 0 3 N
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0.5 1.0 1.5 20 STEAM INTRODUCED, POUNC PER POUND OF DRY, ASH.FREE COAL
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9. Effect of V a r i a b l e s on Y i e l d and O u t p u t R a t e
LEGEND
of S y n t h e s i s - G a s
0.75 15. 0 2 per lb. dry, ash-free coal 1.00 Ib. 0;. per Ib. dry, ash-free coal
Computed from run 62, Sewiokley coal, size 90.8% through ZOO-mesh; assumed: exit-gas temperature 1800' F., no heat losses
operating results were shown t o depend on three independent process variables: oxygen to coal ratio, steam to coal ratio, and steam temperature. An analysis of their effects on theoretically calculated operating results revealed that the magnitudes of these variables may be so selected and combined t h a t the optimum results probably would be obtained under a given set of conditions. Thus, less reactive high rank and low grade fuels may also be gasified effectively, with much reduction in oxygen requirement, by a suitable choice and combination of the operating variables, especially if the contact time and rates of tho reactions are increased by certain modifications in the generator design to suit the available fuel. Furthermore, it appears that, by plotting the actual and/or calculated theoretical operating results versus the three essential process variables in the manner s h o r n , it should be possible t o predict the probable operating results under a given set of operating conditions. The conclusions outlined here are based on results obtained in a relatively small number of comparable runs. They should not be considered definite, but rather tentative and preliminary, indicative of highly probable trends t h a t need to be confirmed by additional experimental data. Nevertheless, the results of prcliininary tests obtained in the laboratory scale gasifier served as a useful guide to operating conditions for inuch larger pilot plant gasifiers. I n these, the suitability of t h e coal for synthesis-gas production on commercial basis n as, then, finally determined.
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(6) Katz, Sidney, IND. EXG.CHEM.,43, to he printed. (7) Sands, A. E., Wainwright, 11. W., and Egleson, G. C., U. S. Bur. Mines, R e p t . Inuest. 4699, 6-7, 50-51 (1950). (8) Sands, A. E., Wainwright, H. W.. and Schmidt, L. D., IND. ENG.CHEM.,40, 607 (1948). (9) Schmidt, L. D., McGee, J. P., and Slone, M. C., Chem. Eng. Progress, 44, 737 (1948). (10) Sebastian, J. J. S., Edehurn, P. W., Bonar, F., Bonifield, L. W., and Schmidt, L. D., U. S. Bur. Mines, Rept. Invest. 4742 (January 1951). (11) Strimbeck, G. R., Holden, J. H., Rockenbach, L. P., Cordiner, J. B., Jr.. and Schmidt, L. D., Ibid., 4733 (November 1950). (12) Wagman, D. D., Rossini, F. D., et al., Natl. Bur. Standards, Resecmh P a p e r 1634 (1945). RECEIVED for review January 18, 1952. ACCEPTED February 27. 1952. Presented as part of the Symposium on Gasification of Solid Fuels before the Divisions of Gas and F u e l Chemistry and Physical and Inorganic Chemistry a t the Diamond Jubilee Meeting of the AMEKICAN CHEMICAL SOCIETY, New York, N. Y .
ACKNOWLEDGMENT
Thanks are due L. D. Schmidt for his frequent suggestions and helpful assistance in evaluating the results and T. E. Corrigan for ready assistance in establishing the thermodynamic procedure for calculating the operating results under assumed conditions. LITERATURE CITED
(1) Alhright, C. W., Holden, J. H., Simons, H. P., and Schmidt,
L. D., Chem. Eng., 56,108 (June 1949). (2) Am. Soc. Testing Materials, Classification of Coals by Grade, D 389-37. (3) Barker, R. R., Sebastian, John J. S., Schmidt, L. D., and Simons, H. P., IND.EN^. CHmf., 43,1204 (1951). (4) Ratchelder, H. R., and Sternberg, J. C., Ibid., 42,877 (1950). (5) Edmister, W. C., Perry, €I., Corey, R. C., and Elliott, M. A., Paper No. 51-A-20, Am. Soc. Mech. Engrs. Annual Meeting (1951).
Correction In t h e February staff-industry collaborative repoit, "Ammonia at 1000 Atmospheres," b y Will H. Shearon, Jr., and H. L. Thompson [IKD. ENG.CHEM.,44, 254 (1952) on page 261, first column, third paragraph, the size of t h e two carbon steel converters (1E) should be 25.75 inches inside diameter b y 16.67 feet high, with shells 10.375 inches thick. In F. W. Mohlman's introduction t o t h e Symposium o n ENG.CHEM.,44, 467 (1952)], Liquid Industrial Wastes [IND. the third line should read, ',has cost $9 t o $12 billion t o date, of which $4.5 billion were allocated t o municipal needs a n d $4.5 t o $7.5 billion t o industrial wastes."
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