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4,861,360 9 10 TABLE I STREAM COMPONENT 101 132 131 137 138 142 N2 0114 co; 1128 3.60 C2H6 158.00 @118 132.00 1041110 62.00 10514112 26.00 NC6H14 6.40 MEOH 0.00 TOTAL 2000.00 TEMP-F 115 PRES-PSIA 615 0.08 97.92 97.92 0.00 0.20 513.00 513.00 0.00 184.04 10.77 10.77 28.58 1.69 1.91 0.00 0.00 0.00 111.98 46.02 51.84 51.84 0.00 12.62 119.38 0.00 0.00 0.00 0.01 61.99 0.00 0.00 0.00 0.00 26.00 0.00 0.00 0.00 0.00 6.40 0.00 0.00 0.00 0.00 0.00 0.09 0.09 2000.00 1553.98 446.02 673.62 673.62 1825.00 -12 68 -29 100 77 500 503 500 495 545 98.00 97.92 514.00 513.80 1000.00 815.96 STREAM COMPONENT 140 199 196 144 187 169 185 N2 0114 co; 1128 C2H6 C3H8 1041110 IC5H12 Nc61-114 MEOH TOTAL TEMP-F 7 19 215 77 25 115 15 PRES-PSIA 505 450 455 545 360 355 350 0.00‘ 0.08 0.00 0.00 0.80 0.20 0.00 0.00 833.77 183.46 0.58 6.00 1.69 1.56 0.35 0.00 60.14 40.04 5.98 0.00 12.62 2.78 116.60 0.00 0.02 0.03 61.96 0.00 0.00 0.00 26.00 0.00 0.00 0.00 6.40 0.00 1999.91 0.00 0.00 400.00 2908.95 228.15 217.87 406.00 'METHANOLMAKEUPIS1.24MOL/HZR The overall utility requirements are illustrated in Table 11. HORSEPOWER Pumps Air Coolers Compressors Total Steam TABLE II UTILITIES APFFEL METHANOL BHP 51 206 4,226 4,483 DUTY MBTU/HR 31,027 RYAN/HOLMES BHP 124 250 5,570 5,944 DUTY MBTU/HR 32,235 ALTERNATE EMBODIMENT MODE FOR CARRYING OUT THE INVENTION Referring to FIG. 1C, there is shown the feed gas stream 401 feeding to a COz-Splitter 412. Stream 401 is 0.00 0.00 0.00 1.00 0.00 0.00 13.04 1010.19 975.61 0.04 3.21 3.21 80.24 19.94 19.94 0.00 15.40 15.40 0.00 0.05 0.05 0.00 0.00 0.00 0.00 0.00 0.00 0.19 2399.72 0.96 94.51 3448.51 1015.17 STREAM COMPONENT 62 N2 01-14 co; 112s C2H6 C3H8 1c4111o 1051-112 NC6H14 MEOH TEMP-F PRES-PSIA 0.00. 0.00 34.58 0.00 0.00 0.00 0.00 0.00 0.00 2398.76‘ 2433.34 120 555 45 credfromeachoftheseoutgoingstreams456and492. TheexchangeofenergyisaccomplishedinaFeedGas to Methane Gas Exchanger 405 for streams 404 and 456. The exchange of energy is accomplished in a Feed Gas toCog-Splitterbottoms exchanger 403 forstreams402 50 and 492. The cooled feed gas streams 402 and 404 are recombined in a stream 406 and chilled to a temperature of 50° to —30° F. with propane or freon or other suit able refrigeration (not shown in detail) in a Chiller 407 fed by stream 406. The effluent chilled feed stream 408 55 fromChiller407isreducedinpressuretoalevelof350 to 400 psia by a pressure control valve 410 at the outlet ofstream 408. The effluent stream 411 from valve 410 is fed to a Cog-Splitter 412. The pressure in stream 411 is set and controlled by a Pressure Controller 409 which 60 operatesvalve410,COg-Splitter412separatesthecom ponents ofstream 411. The overhead gas from the CO2 Splitter 412 exits in a stream 413 and is chilled to a temperature of 0° to -30" F. by a C02 Splitter Re?ux Condenser 414 with propane or freon refrigeration or split into two streams 402 and 404. The feed gas in streams402and404cross-exchangewithproductmeth 65othersuitablerefrigerant(notshownindetail).The ane in stream 456 for stream 404 and COZ-Splitter bot toms stream 492 for stream 402. The split is distributed on the basis of the cryogenic energy that can be recov ef?uent stream 415 from the Cog-Splitter Re?ux Con densor 414 ?ows to a Re?ux Accumulator 416. Part of the gas in stream 415 is condensed in Accumulator 416,PDF Image | CARBON DIOXIDE ABSORPTION METHANOL PROCESS
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