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15 The overhead gas product from the CO7/Light Ends 16 Splitter 472. The carbon dioxide is distilled as an over head product in stream 482 subsequently compressed and condensed to combine with the carbon dioxide product from the COZ/Light Ends Separator Tower 495 in stream 450 as the total liquid carbon dioxide product in stream 487. The methanol bottoms product stripped of carbon dioxide and other hydrocarbons becomes the “lean” methanol. Itiscooled at 120° F. and 'recycled to the system. The CO2-Methanol Splitter 472 ‘Methanol make-up is0.38 l6-MOLE/HR The above iscomputer calculated. sorber 496. This “lean” methanol in stream 481 has been chilled to a temperature of 0° to —-40° F. The “lean” The advantage of the art disclosed by the ?rst em bodiment process over the Ryan/Holmes separation system discussed in the “Background” also applies for COMP MOL/H MOL/H MOL/H MOL/H MOL/H MOL/H MOL/H TEMP-F PRES-PSIA 102 — 2.3 368 350 18 8 188 0 48 358 350 354 350 630 4,861,360 Separator Tower 495 containing methane, lighter com ponents, carbon dioxide, and ethane in stream 444 is mixed with liquid in stream 451 withdrawn at the bot tom chimney tray 496 of Methanol Absorber 455. The mixture isrefrigerated to a temperature of ~40“ to 0° F. This partially condenses the carbon dioxide which is absorbed or dissolved into the liquid methanol stream. The refrigeration removes the heat of solution or ab sorption and effectively reduces the “lean” methanol 10 is operated at pressures of 300 to 400 psia with top rate. The mixture is fed to the bottom of the Methanol Absorber 496 where the gas and liquid separate. The gas ?ows upward, countercurrent to the downcoming “lean” methanol fed at the top of the Methanol Ab temperatures of — 15° to 25° F. and corresponding bot toms temperatures 300° to 400° F. Typical operating conditions, product distributions, and?owratesareillustratedinTableIII. I TABLEIII E.O.R. CO2 RECOVERY SYSTEM ALT-l 83% co2 VOL = 83.13 l-TOW l-TOW NGL NGL NGL COMB COMB FEED OVHD FEED OVHD BTMS FEED FEED STREAM NO 401 417 492 424 437 428 430 27.00 27.00 790.00 790.00 7570.00 5887.50 290.00 275.46 240.00 19.91 32.00 0.02 78.00 0.00 24.00 0.00 24.00 0.00 25.00 0.00 0.00 0.00 0.00 27.00 27.00 0.00 0.00 0.00 790.00 790.00 1682.50 1671.30 11.20 7558.80 7558.80 14.54 14.14 0.40 289.60 289.60 220.09 6.59 213.50 26.50 26.50 N2 C1 CO2 C2 C3 IC4 NC4 1C5 NC5 NC6 MEOH 0.00 0.00 TOTAL 9100.00 6999.89 31.98 0.00 78.00 0.00 24.00 0.00 24.00 0.00 25.00 0.00 31.98 78.00 24.00 24.00 25.00 0.02 0.02 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 2100.11 1692.03 408.08 8691.92 8691.92 3-TOW 3-TOW LEAN ABS ABS CO2 MEOH TOT OVHD BTMS MEOH OVHD BTMS OVHD BTMS CO2 STREAM NO 444 450 481 456 460 482 476 487 COMP MOL/H MOL/H MOL/H MOL/H MOL/H MOL/H MOL/H MOL/H N2 C1 CO2 C2 C3 IC4 0.00 N01- 0.00 1C5 0.00 NC5 0.00 NC6 0.00 MEOH 0.00 0.00 TOTAL TEMP-F PRES-PSIA 1000.00 0.28 999.72 0.05 999.67‘ 0.05 2025.01 6666.91 1010.00 864.86 2170.15 1159.00 1011.15 7825.91 — 1 44 — 10 --10 - 10 15 346 44 615 623 610 610 610 375 381 623 27.00 0.00 0.00 27.00 0.00 0.00 0.00 0.00 774.28 15.72 0.00 755.46 18.82 18.82 0.00 34.54 1116.50 6442.30 10.00 0.93 1125.57 1114.20 11.37 7556.50 105.48 184.12 1.75 24.75 0.02 0.00 80.06 25.42 25.31 0.00 1.13 0.62 0.62 0.11 209.43 0.00 25.37 0.00 0.02 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 000 0.00 0.00 0.00 0.00 0.00 000 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 methanol rate is based on a molal ratio of carbon diox~ idetomethanolofbetweentwoandthreetoone.The 55 thisalternateembodimentinthatnosolidformationof carbon dioxide is more soluble in methanol than meth ane or the lighter components. Consequently, the car bon dioxide isdissolved or absorbed inthe “lean” meth anol, The separated liquid leaves the bottom of the Methanol Absorber 496 as a liquid at temperatures of 60 ther at this level of temperature and above, all of the 10° to 20° F. above the inlet “lean” methanol. Hydrogen sul?de is also very soluble in methanol and if any is present itwill be dissolved in the methanol. The “rich” methanol in stream 460 is partially cross-exchanged withthe“lean”methanolinstream478torecoverthe65 cryogenic energy and warm the “rich” methanol. The warmed “rich” methanol from the Methanol Absorber 496 in stream 499 isfed to the COy/Methanol materials of construction for the distillation and absorp tion system may be carbon steel, which reduces the plant cost, Also, the methanol is a polar molecule used to absorb the carbon dioxide and hydrogen sul?de from theethane-methane-and-lightercomponents.Themeth anol serves to invert the relative volatility of carbon dioxide to ethane and maintain itwell above one. Based on this fact, the methanol not only prevents the poten carbon dioxide will take place in the distillation and absorptionseparationsystemsdescribedhereinbecause the minimum temperature required is —40° E. which is well above the freezing point of carbon dioxide. FurPDF Image | CARBON DIOXIDE ABSORPTION METHANOL PROCESS
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