Gas-absorption process

Claim 2

In a process wherein a liquid phase is withdrawn from a first liquid-gas contacting zone for effecting preferential absorption of a selected component of a feed-gas mixture in a liquid absorbent and is passed downwardly through second and third liquid-gas contacting zones, the liquid-phase input to the second zone comprising said liquid containing absorbent in solution said gaseous component and at least one less-soluble, diluent gas, said liquid-phase input being contacted in the second zone with a warmer, upflowing gas phase derived from the third zone, said gas phase comprising vapor of said liquid absorbent and a lesser amount of gas desorbed from said liquid absorbent; the method of recovering said component as a gas, comprising: (a) establishing a peak concentration of said component in a section of the second zone by (1) maintaining the temperature of the liquid-phase input to the second zone at a sufficiently lower value than the temperature of said upflowing third-zone-derived gas-phase input to the second zone to effect, in said section, condensation of a major fraction of the absorbent-vapor upflow into said section; and (2) maintaining below said section stripping factors of less than one for said component and for gases less soluble than said component while maintaining above said section stripping factors of more than one for said component and less than one for less-soluble gases; and (b) withdrawing gas rich in said component from said section.

Claim 3

The process of claim 1 wherein said liquid-phase input to the second zone is at a temperature in the range of from approximately -200° F. to 500° F.

Claim 4

The process of claim 1 wherein the first, second, and third zones, respectively comprise upper, intermediate, and lower zones of a single liquid-gas contacting column.

Claim 5

The process of claim 3 wherein the upper, intermediate, and lower zones of said column are maintained at approximately the same superatmospheric pressure.

Claim 6

The process of claim 1 wherein said liquid absorbent is selected from the group consisting of fluorocarbons, hydrocarbons, and water.

Claim 7

A process for recovering a selected component from a feed-gas mixture containing the same, said process comprising: (a) providing a liquid-gas contacting column defining an upper zone, an intermediate zone, and a lower zone; (b) passing a stream of a liquid absorbent for said component downwardly through the zones of said column, said zones being maintained at approximately the same superatmospheric pressure and at least part of said lower zone being maintained at the boiling point for said absorbent at the pressure prevailing in said column; (c) in said upper zone, countercurrently contacting said liquid absorbent with said feed gas mixture; (d) in said intermediate zone, countercurrently contacting the resulting gas-enriched liquid absorbent with desorbed gases and absorbent vapor derived from said lower zone; (e) in said lower zone, countercurrently contacting the liquid absorbent from the intermediate zone with absorbent vapor and desorbed gases obtained by boiling the liquid absorbent downflow through said lower zone; (f) maintaining the temperatures and flow rates of the countercurrent liquid- and gas-phase inputs to said intermediate zone at values effecting, in a section of said intermediate zone, condensation of a major fraction of the absorbent-vapor upflow into said section, while maintaining below said section stripping factors of less than one for said components and for gases less suitable than said component and above said section stripping factors of more than one for said component and less than one for gases less soluble than said component, thus concentrating said component as in said section, and (g) withdrawing gas enriched in said component from said section.

Claim 8

A process for recovering a selected component from a feed-gas mixture containing the same, said process comprising: (a) providing a liquid-gas contacting column defining an upper zone, an intermediate zone, and a lower zone; (b) passing a stream of a liquid absorbent for said component downwardly through the zones of said column, said zones being maintained at approximately the same superatmospheric pressure and at least part of said lower zone being maintained at the boiling point for said absorbent at the pressure prevailing in said column; (c) in said upper zone, countercurrently contacting said liquid absorbent with said feed gas mixture; (d) in said intermediate zone, countercurrently contacting the resulting gas-enriched liquid absorbent with desorbed gases and absorbent vapor derived from said lower zone; (e) in said lower zone, countercurrently contacting the liquid absorbent from the intermediate zone with absorbent vapor and desorbed gases obtained by boiling the liquid absorbent downflow through said lower zone; (f) maintaining the temperatures and flow rates of the countercurrent liquid- and gas-phase inputs to said intermediate zone at values effecting, in a section of said intermediate zone, condensation of a major fraction of the absorbent-vapor upflow into said section, while maintaining below said section stripping factors of less than one for said components and for gases less suitable than said component and above said section stripping factors of more than one for said component and less than one for gases less soluble than said component, thus concentrating said component as in said section, and (g) withdrawing gas enriched in said component from said section.

Claim 9

The process of claim 6 wherein said liquid absorbent is selected from the group consisting of fluorocarbons, hydrocarbons, and water.

Claim 10

The process of claim 6 wherein said upper zone of said column is maintained at a temperature in the range of from approximately -200° F. to 500° F.

Claim 11

The process of claim 6 wherein heat is removed from a region of said column disposed between said lower zone and said section by condensing a part of the absorbent-vapor upflow in said region and transferring the heat of condensation to a heat sink outside said column.

Claim 12

The process of claim 6 wherein the gas withdrawn from said section is derived from an inverted cuplike gas-collector mounted in said section.