Liquid carbon dioxide recovery from gas mixtures with methane

Claim 2

The process of recovering liquid CO 2 with a molar purity of not less than 99.5% from a moisture-free by-product gas mixture of at least 90% by volume CO 2 , at least 2% by volume methane and a fractional percentage of methanol, which comprises: compressing said gas mixture to a pressure in the range of about 225 to 275 psia, chilling the compressed gas mixture containing said methanol by heat exchange with liquid of the reboiler portion of a fractionation zone to condense a major portion of said methanol, separating the condensed methanol from the chilled compressed gas mixture, adsorbing trace contaminants and residual methanol from said chilled compressed gas mixture, further cooling the resulting substantially pure gas mixture of CO 2 and methane by heat exchange with a refrigerant at a predetermined low temperature to effect partial liquefaction of said pure gas mixture, discharging the partially liquefied gas mixture into the reflux portion of said fractionation zone, cooling vapor of the top of said fractionation zone by heat exchange with said refrigerant at said predetermined low temperature to provide reflux liquid for said reflux portion, withdrawing from the top of said fractionation zone a vapor stream containing substantially all of said methane in said by-product gas mixture and not more than 20% of the CO 2 in said by-product gas mixture, and withdrawing liquid CO 2 with a molar purity of not less than 99.5% from the bottom of said fractionation zone.

Claim 3

The process of claim 1 wherein the liquid CO 2 withdrawn from the bottom of the fractionation zone is subcooled by heat exchange with the same refrigerant at the same predetermined low temperature used to provide reflux liquid.

Claim 4

The process of claim 1 wherein the predetermined low temperature of the refrigerant is in the range of about -25° F. to -40° F.

Claim 5

The process of recovering liquid CO 2 with a molar purity of not less than 99.5% from a moisture-containing by-product gas mixture of at least 90% by volume CO 2 and at least 2% by volume methane, which comprises: compressing said gas mixture to a pressure in the range of about 225 to 275 psia, injecting methanol into said gas mixture, chilling the compressed gas mixture containing said methanol by heat exchange with liquid of the reboiler portion of a fractionation zone to condense substantially all the moisture as an aqueous methanol condensate, separating said condensate from the chilled compressed gas mixture, adsorbing trace contaminants as well as residual methanol and moisture from said chilled compressed gas mixture, further cooling the resulting substantially pure gas mixture of CO 2 and methane by heat exchange with a refrigerant at a predetermined low temperature to effect partial liquefaction of said pure gas mixture, discharging the partially liquefied gas mixture into the reflux portion of said fractionation zone, cooling vapor of the top of said fractionation zone by heat exchange with said refrigerant at said predetermined low temperature to provide reflux liquid for said reflux portion, withdrawing from the top of said fractionation zone a vapor stream containing substantially all of said methane in said by-product gas mixture and not more than 20% of the CO 2 in said by-product gas mixture, and withdrawing liquid CO 2 with a molar purity of not less than 99.5% from the bottom of said fractionation zone.

Claim 6

The process of recovering liquid CO 2 with a molar purity of not less than 99.5% from a moisture-containing by-product gas mixture of at least 90% by volume CO 2 and at least 2% by volume methane, which comprises: compressing said gas mixture to a pressure in the range of about 225 to 275 psia, injecting methanol into said gas mixture, chilling the compressed gas mixture containing said methanol by heat exchange with liquid of the reboiler portion of a fractionation zone to condense substantially all the moisture as an aqueous methanol condensate, separating said condensate from the chilled compressed gas mixture, adsorbing trace contaminants as well as residual methanol and moisture from said chilled compressed gas mixture, further cooling the resulting substantially pure gas mixture of CO 2 and methane by heat exchange with a refrigerant at a predetermined low temperature to effect partial liquefaction of said pure gas mixture, discharging the partially liquefied gas mixture into the reflux portion of said fractionation zone, cooling vapor of the top of said fractionation zone by heat exchange with said refrigerant at said predetermined low temperature to provide reflux liquid for said reflux portion, withdrawing from the top of said fractionation zone a vapor stream containing substantially all of said methane in said by-product gas mixture and not more than 20% of the CO 2 in said by-product gas mixture, and withdrawing liquid CO 2 with a molar purity of not less than 99.5% from the bottom of said fractionation zone.

Claim 7

The process of claim 4 wherein the liquid CO 2 withdrawn from the bottom of the fractionation zone is subcooled by heat exchange with the same refrigerant at the same predetermined low temperature used to provide reflux liquid.

Claim 8

The process of claim 4 wherein the predetermined low temperature of the refrigerant is in the range of about -25° F. to -40° F.

Claim 9

In the process for removing CO 2 from a feed gas containing at least 50% by volume methane and at least 5% by volume CO 2 comprising: compressing said gas; injecting methanol into said gas to dehydrate said gas by chilling said gas to condense all the moisture therein as aqueous methanol and by separating said aqueous methanol from the chilled dehydrated gas; scrubbing said chilled dehydrated gas at a pressure of about 200 to 600 psia with cold recycled methanol supplied at a temperature of about -40° F. to -70° F. and containing not more than about 2% on a molar basis of absorbed CO 2 ; recovering the scrubbed gas containing not more than about 2.5% by volume CO 2 as high BTU fuel gas product; chilling the methanol with absorbed CO 2 withdrawn from said scrubbing by heat exchange with a refrigerant at a predetermined low temperature; and passing the chilled methanol through a pressure-reduction flashing separation of CO 2 -rich gas from said methanol and at least two heat flashing separations of CO 2 -rich gas from said methanol which is then recycled to said scrubbing; the improvement which comprises: compressing all of the flashed CO 2 -rich gas containing at least 90% by volume CO 2 , at least 2% by volume methane and a fractional percentage of methanol to a pressure in the range of about 225 to 275 pisa, chilling the compressed CO 2 -rich gas containing said methanol by heat exchange with liquid of the reboiler portion of a fractiontion zone to condense a major portion of said methanol, separating the condensed methanol from the chilled compressed CO 2 -rich gas, adsorbing trace contaminants and residual methanol from said chilled compressed CO 2 -rich gas, further cooling the resulting substantially pure gas mixture of CO 2 and methane by heat exchange with said refrigerant at said predetermined low temperature to effect partial liquefaction of said pure gas mixture, discharging the partially liquefied gas mixture into the reflux portion of said fractionation zone, cooling vapor of the top of said fractionation zone by heat exchange with said refrigerant at said predetermined low temperature to provide reflux liquid for said reflux portion, withdrawing from the top of said fractionation zone a vapor stream containing substantially all of said methane in said flashed CO 2 -rich gas and not more than 20% of the CO 2 in said flashed CO 2 -rich gas, and recycling said vapor stream for compression with said feed gas; and withdrawing liquid CO 2 with a molar purity of not less than 99.5% from the bottom of said fractionation zone.

Claim 10

In the process for removing CO 2 from a feed gas containing at least 50% by volume methane and at least 5% by volume CO 2 comprising: compressing said gas; injecting methanol into said gas to dehydrate said gas by chilling said gas to condense all the moisture therein as aqueous methanol and by separating said aqueous methanol from the chilled dehydrated gas; scrubbing said chilled dehydrated gas at a pressure of about 200 to 600 psia with cold recycled methanol supplied at a temperature of about -40° F. to -70° F. and containing not more than about 2% on a molar basis of absorbed CO 2 ; recovering the scrubbed gas containing not more than about 2.5% by volume CO 2 as high BTU fuel gas product; chilling the methanol with absorbed CO 2 withdrawn from said scrubbing by heat exchange with a refrigerant at a predetermined low temperature; and passing the chilled methanol through a pressure-reduction flashing separation of CO 2 -rich gas from said methanol and at least two heat flashing separations of CO 2 -rich gas from said methanol which is then recycled to said scrubbing; the improvement which comprises: compressing all of the flashed CO 2 -rich gas containing at least 90% by volume CO 2 , at least 2% by volume methane and a fractional percentage of methanol to a pressure in the range of about 225 to 275 pisa, chilling the compressed CO 2 -rich gas containing said methanol by heat exchange with liquid of the reboiler portion of a fractiontion zone to condense a major portion of said methanol, separating the condensed methanol from the chilled compressed CO 2 -rich gas, adsorbing trace contaminants and residual methanol from said chilled compressed CO 2 -rich gas, further cooling the resulting substantially pure gas mixture of CO 2 and methane by heat exchange with said refrigerant at said predetermined low temperature to effect partial liquefaction of said pure gas mixture, discharging the partially liquefied gas mixture into the reflux portion of said fractionation zone, cooling vapor of the top of said fractionation zone by heat exchange with said refrigerant at said predetermined low temperature to provide reflux liquid for said reflux portion, withdrawing from the top of said fractionation zone a vapor stream containing substantially all of said methane in said flashed CO 2 -rich gas and not more than 20% of the CO 2 in said flashed CO 2 -rich gas, and recycling said vapor stream for compression with said feed gas; and withdrawing liquid CO 2 with a molar purity of not less than 99.5% from the bottom of said fractionation zone.

Claim 11

The improvement of claim 7 wherein the condensed methanol separated from the chilled compressed CO 2 -rich gas is recycled for injection into the compressed feed gas for the dehydration thereof.

Claim 12

The improvement of claim 7 wherein the liquid CO 2 withdrawn from the bottom of the fractionation zone is subcooled by heat exchange with the same refrigerant at the same predetermined low temperature used to provide reflux liquid.

Claim 13

The improvement of claim 7 wherein the predetermined low temperature of the refrigerant is in the range of about -25° F. to -40° F.

Claim 14

The improvement of claim 7 wherein prior to passing the chilled methanol with absorbed CO 2 through the pressure-reduction flashing separation of CO 2 -rich gas from said chilled methanol, said chilled methanol with absorbed CO 2 is passed through a preliminary partial pressure-reduction flashing separation of CO 2 -rich gas which is recycled for scrubbing with cold methanol.

Claim 15

The improvement of claim 11 wherein the CO 2 -rich gas from the preliminary partial pressure-reduction flashing separation amounts to about 10% by volume of all the gas scrubbed with cold methanol.

Claim 16

The improvement of claim 11 wherein the liquid CO 2 withdrawn from the bottom of the fractionation zone is subcooled by heat exchange with the same refrigerant at the same predetermined low temperature used to provide reflux liquid.

Claim 17

The improvement of claim 13 wherein the predetermined low temperature of the refrigerant is in the range of about -25° F. to -40° F.