Method to condense and recover carbon dioxide (CO2) from CO2 containing gas streams

Abstract

A method to condense and recover CO.sub.2 from CO.sub.2 containing streams. A first step involve providing at more than one heat exchanger, with each heat exchanger having a first flow path for passage of a first fluid and a second flow path for passage of a second fluid. A second step involves passing a stream of very cold natural gas sequentially along the second flow path of each heat exchanger until it is heated for distribution and concurrently passing a CO.sub.2 containing stream sequentially along the first flow path of each heat exchanger, allowing the water vapor portion of the CO.sub.2 containing stream to condense and precipitate on the condensing heat exchangers. A third step involves passing a water vapor free CO.sub.2 containing stream to a cryogenic heat exchanger to condense, precipitate and recover CO.sub.2. This processes results in the recovery of CO.sub.2 and water vapor from CO.sub.2 containing streams using condensing heat exchangers, chiller, compressor, expander and power generator to recover the low value thermal heat available in CO.sub.2 containing waste streams.

Claims

1. A method to cool and condense a CO2 containing gas stream to recover CO2, comprising the steps of: providing more than one heat exchanger, the more than one heat exchanger comprising at least one water condensing heat exchanger and at least one CO2 condensing heat exchanger, each heat exchanger having a first flow path for passage of a first fluid and a second flow path for passage of a second fluid; passing an uncompressed CO2 containing gas stream along the first flow path of the water condensing heat exchanger to cool and condense water vapor in the CO2 containing gas stream, and through a separator to separate condensed water from the CO2 containing gas stream; cooling coolant water in a chiller that is powered by heat in the CO2 containing gas stream; compressing the CO2 containing gas stream exiting the separator and then cryogenically cooling the CO2 containing gas stream in the at least one CO2 condensing heat exchanger, the at least one CO2 condensing heat exchanger condensing at least a portion of the CO2 in the CO2 containing gas stream, and separating the condensed CO2 from the cooled CO2 containing gas stream in a CO2 separator; passing the cooled CO2 containing gas stream from the CO2 separator along the second flow path of at least one heat exchanger to cool the CO2 containing gas stream in the first flow path; passing the cooled coolant water from the chiller along the second flow path of at least one heat exchanger to cool the CO2 containing gas stream in the first flow path; generating a natural gas stream at a temperature and pressure suitable for distribution in a distribution natural gas line from a Liquid Natural Gas (LNG) stream by: firstly, pressurizing the LNG stream in a liquid pump; secondly, heating the pressurized LNG stream in stages by passing the pressurized LNG stream through the second flow path of the at least one CO2 condensing heat exchanger and at least one additional heat exchanger to generate the natural gas stream; and thirdly, passing the natural gas stream through a gas expander to depressurize and cool the natural gas stream to a pressure and temperature suitable for distribution, the natural gas stream being expanded by the gas expander without being consumed, the gas expander being capable of generating power from expanding natural gas before discharging the natural gas stream into the distribution natural gas line for downstream consumption.

2. The method of claim 1, wherein the CO2 containing gas stream is a stream of diverted flue gas.

3. The method of claim 1, further comprising the step of passing the cooled water from the chiller through the second flow path of at least one heat exchanger to cool the CO2 containing gas stream.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) These and other features will become more apparent from the following description in which reference is made to the appended drawings, the drawings are for the purpose of illustration only and are not intended to in any way limit the scope of the invention to the particular embodiment or embodiments shown, wherein:

(2) FIG. 1 is a schematic diagram of an apparatus used to condense and recover CO.sub.2 from in CO.sub.2 containing gas streams.

(3) FIG. 2 is a schematic diagram of an alternative apparatus used to condense and recover CO.sub.2.

(4) FIG. 3 is a schematic diagram of a further alternative apparatus used to condense and recover CO.sub.2.

(5) FIG. 4 is a schematic diagram of a further alternative apparatus used to condense and recover CO.sub.2.

(6) FIG. 5 is a schematic diagram of a further alternative apparatus used to condense and recover CO.sub.2.

(7) FIG. 6 is a schematic diagram of a further alternative apparatus used to condense and recover CO.sub.2.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

(8) The preferred method to recover and condense carbon dioxide embodiment will now be described with reference to FIGS. 1 through 6.

(9) In this process cryogenic energy is supplied by a pressurized stream of LNG to condense and recover carbon dioxide. The CO.sub.2 containing gas stream is cooled down in a counter current flow though various exchangers to remove the water vapor before condensing and recovering the CO.sub.2.

(10) The present practice releases the CO.sub.2 containing flue gas streams into the atmosphere without recovering its low value heat, its water vapor and the CO.sub.2. The proposed invention routes the CO.sub.2 containing flue gases through duct 1 into heat exchanger section 50. A pressurized natural gas stream flows through line 10 into heating coil 70. The pressurized natural gas stream is heated by the warm flue gas and exits through line 11. The pressure control valve 57 is pre-set to meet the gas pressure requirement of line 12. The now cooler CO.sub.2 containing flue gas stream enters heat exchanger section 51 where it exchanges heat with a lean CO.sub.2 flue gas stream that enters through line 5 into heating coil 71. The lean CO.sub.2 flue gas stream is heated by the warmer flue gas stream before exiting the exchanger through line 6 into the atmosphere. The CO.sub.2 containing flue gas stream is now approaching its dew point and it enters heat exchanger section 52 through duct 2 and into coil 72. Atmospheric air enters section 52 though a once through duct 13 to further cool the CO.sub.2 containing flue gas. The CO.sub.2 containing flue gas has reached its dew point and now begins to condense its vapor in heat exchanger section 53. The condensed water exits the heat exchanger through line 14. A cold lean CO.sub.2 flue gas stream enters the heat exchanger through line 4 into heating coil 73 and exits through line 5. This cold stream further reduces the temperature of the CO.sub.2 containing flue gas to remove more water. The CO.sub.2 containing flue gas is now near zero and now enters heat exchanger section 54 to remove the remaining water. The condensed water exits through line 15. A pressurized natural gas stream provides additional cooling entering the heat exchanger section 54 through line 9 into heating coil 74 and exits through line 10. The CO.sub.2 containing flue gas stream is now free of water and enters heat exchanger section 55 through duct 3. A liquid natural gas stream 7 is pressurized by pump 56 to a pre-set pressure and then enters heat exchanger 55 through line 8 into heating coil 75. The CO.sub.2 in stream 3 is condensed, liquefied and exits though line 16. The LNG having given up its cool energy is vaporized in coil 75 and exits through line 9.

(11) The process cools and recovers the CO.sub.2 in the flue gas stream using condensing heat exchangers and the cryogenic temperatures of LNG. There are various process variations that can enhance the recovery of the low value waste heat present in the CO.sub.2 containing flue gas. Moreover, the process efficiency will increase proportionally to the CO.sub.2 concentration of the flue gas. A variation of FIG. 2 follows the process as in FIG. 1 with the addition of a separator 218 after heat exchanger 54 to remove any moisture in the stream prior to compressing the CO.sub.2 containing flue through compressor 257. Line 204 conducts the gas stream from the separator 218 to the compressor 257. Compressing the CO.sub.2 containing flue gas before cooling it with LNG reduces the cryogenic load in heat exchanger 55. Line 205 conducts the output from the compressor 257 to the heat exchanger 55. In FIG. 3, the added improvement to the process over FIG. 2 has the addition of a gas expander 358 and power generator 359. These components take advantage of the thermal energy gained in section 50 by the compressed natural gas from the CO.sub.2 containing flue gas to generate electricity. In FIG. 4 there is another improvement on the process over FIG. 3 where an absorption chiller 460 replaces the atmospheric air heat exchanger to further recover the low waste heat available to generate chilled water for use in cooling the CO.sub.2 containing flue gas. A different variation of FIG. 4 over FIG. 3 has a pressure control valve 57, known as a JT-valve, in lieu of a gas expander. Another variation of FIG. 4 over FIG. 3 is the removal of the CO.sub.2 containing flue gas compressor. In FIG. 5 the variation of FIG. 4 is the addition of CO.sub.2 containing flue gas compressor 257. The complete and maximized recovery process arrangement is shown in FIG. 6 where chiller 460, compressor 257, expander 358, and power generator 359 maximize the recovery of low value waste heat, water vapor recovery and CO.sub.2 recovery.

(12) Referring to FIGS. 4-6, the gas stream in line 412 enters section 452 through coil 472 to extract heat from the flue gas stream and then enters chiller 460 through line 413. The chilled stream in line 414 enters section 453 through coil 473 to further cool the flue gas stream and return to the chiller through line 415. A condenser 459 provides cooling for chiller 460 by exchanging the cool in stream 5 with the heat in stream 417. The condensed stream 416 returns to the chiller 460 and the heated flue gas stream 404 enters section 51. Similar to line 15, condensed water exits through line 418.

(13) In this patent document, the word “comprising” is used in its non-limiting sense to mean that items following the word are included, but items not specifically mentioned are not excluded. A reference to an element by the indefinite article “a” does not exclude the possibility that more than one of the element is present, unless the context clearly requires that there be one and only one of the elements.

(14) It will be apparent to one skilled in the art that modifications may be made to the illustrated embodiment without departing from the spirit and scope of the invention as hereinafter defined in the Claims.