SYSTEM AND METHOD FOR SOLVENT REGENERATION

Abstract

A system for regeneration of acidic gas solvent, the system comprising; a regeneration cell having a solvent chamber arranged to receive a solvent flow, and an internal chamber arranged to receive a steam flow; said regeneration cell including a gas permeable membrane separating the solvent chamber and internal chamber; wherein the regeneration cell is arranged to vent acidic gas stripped from the solvent by the steam.

Claims

1. A system for regeneration of acidic gas solvent, the system comprising; a regeneration cell having a solvent chamber arranged to receive a solvent flow, and an internal chamber arranged to receive a steam flow; the regeneration cell including a gas permeable membrane separating the solvent chamber and internal chamber; wherein the regeneration cell is arranged to vent acidic gas stripped from the solvent by the steam.

2. The system according to claim 1, further including a re-boiler in communication with an outlet from the solvent chamber, the re-boiler arranged to heat the stripped solvent so as to remove water, and direct the consequential steam flow to the internal chamber.

3. The system according to claim 1, further including a bulk removal regeneration cell, the bulk removal regeneration cell having a bulk removal solvent chamber arranged to receive a solvent flow, and a bulk removal internal chamber; the bulk removal regeneration cell including a gas permeable membrane separating the bulk removal solvent chamber and bulk removal internal chamber; wherein the bulk removal regeneration cell is arranged to vent acidic gas diffused from the solvent, and direct the solvent to the solvent chamber of the regeneration cell.

4. The system according to claim 1, wherein the solvent chamber is concentrically arranged around the internal chamber.

5. A method for regenerating acidic gas solvent, the method comprising the steps of: receiving a solvent flow in a solvent chamber; receiving a steam flow in an internal chamber; separating the internal chamber from the solvent chamber with a gas permeable membrane; stripping the acidic gas from the solvent; diffusing the acidic gas into the internal chamber; and venting the acidic gas from the internal chamber.

6. The method according to claim 5, further including the steps of: re-boiling the stripped solvent so as to remove water; and directing the consequential steam flow to the internal chamber.

7. The method according to claim 5, further including the steps, prior to the solvent receiving step of: receiving the solvent flow in a bulk removal solvent chamber; separating the bulk removal solvent chamber from a bulk removal internal chamber with a gas permeable membrane; removing the acidic gas from the solvent; diffusing the acidic gas through the gas permeable membrane; venting the acidic gas from the bulk removal internal chamber; and directing the solvent to the solvent chamber of the regeneration cell.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0015] It will be convenient to further describe the present invention with respect to the accompanying drawings that illustrate possible arrangements of the invention. Other arrangements of the invention are possible and consequently, the particularity of the accompanying drawings is not to be understood as superseding the generality of the preceding description of the invention.

[0016] FIG. 1 is a schematic view of the regeneration system according to one embodiment of the present invention;

[0017] FIGS. 2A and 2B are schematic views of a membrane contactor cell according to a further embodiment of the present invention;

[0018] FIG. 3 is a schematic view of the regeneration system according to a further embodiment of the present invention;

[0019] FIG. 4 is a schematic view of a regeneration system according to a still further embodiment of the present invention and;

[0020] FIG. 5 is a cross sectional view of a regeneration cell according to the embodiment of FIG. 4.

DETAILED DESCRIPTION

[0021] FIG. 1 shows a regeneration system 5 according to one embodiment of the present invention. Here the system 5 comprises a hydrocarbon removal step 10 followed by the regeneration step 15. A high pressure flash drum 25 receives a feed of solvent laden with an acidic gas, such as an alkanolamine laden with CO.sub.2, and subsequently vents the hydrocarbon 45 through a valve 40. Levels 55 are controlled by a controller 50 within the flash drum 25 with the lean amine flow passing through a lean rich heat exchanger and subsequently introduced into a membrane contactor cell 62. The membrane contactor cell 62 receives a flow 85 of steam into a central core (not shown) which strips the CO.sub.2 and other acid gases which are vented 70. The stripped amine then flows into a reboiler 80, via a valve 75, for re-boiling. The amine is subsequently delivered 90 back to the lean rich heat exchanger 35. Steam from the reboiler 80 is vented into the membrane contactor cell 62 as previously mentioned. Importantly the steam vented by the reboiler is used to heat up the solvent in the membrane contactor to approximately 105° C., which is lower than the conventional column temperature (approx. 131° C.). Consequently, this represents an energy saving as well as saving infrastructure costs.

[0022] The process is better demonstrated in FIGS. 2A and 2B which show a two-step action of introducing 85 steam 110 into an internal chamber 92. In this embodiment the internal chamber 92 is separated from the solvent chamber 100 by a gas permeable membrane 95. Said membrane may be hydrophobic, and include materials such like polysulfone, PTFE, PVDF, PP, PEEK, surface coated membranes or other such suitable material.

[0023] The CO.sub.2 laden solvent is introduced 60 into the solvent chamber 100 but prevented from entering the internal chamber 92 by the gas permeable membrane 95. The steam 110 interacts through the membrane 95 with the solvent stripping the CO.sub.2 105 from the solvent and venting the CO.sub.2 70 from an outlet in gas communication with the internal chamber 92. The flow of steam from the inlet 85 to the outlet 70 drives against the flow of solvent from the inlet 60 to the outlet 65. This tends to concentrate the CO.sub.2 gas 105 about the gas outlet 70 aiding in the stripping process. Thus, the CO.sub.2 flows out of the cell 62 as the steam is condensed, with the stripped solvent flowing out 65 of the cell 62 towards the reboiler.

TABLE-US-00001 TABLE 1 Liquid Liquid Initial Final Inlet Outlet Vessel- CO.sub.2 CO.sub.2 Temper- Temper- volume/ Loading, Loading, ature, ature, flow, mol/mol mol/mol ° C. ° C. minutes Membrane 0.43 0.001 94.5 105 24.54 Regeneration System Conventional 0.30 0.01 114 131 47.90 Using Column Regeneration Module 2.5 cm ID, 50 cm length, membrane area 0.31 m.sup.2 MBC liquid flow rate is 0.60 L/hr

[0024] As can be seen, the system according one embodiment of the present invention provides a final CO.sub.2 loading in the regenerated solvent of 0.001 mol/mol as compared to a conventional system using column regeneration having a final CO.sub.2 loading of 0.01 mol/mol.

[0025] Further, the vessel-volume/flow for this embodiment is 24.54 as compared to 47.90 for the conventional system. The reduction in vessel-volume/flow consequently suggests to a reduction in the required infrastructure and therefore a significant reduction in capital expenditure for the invention as compared to the systems of the prior art.

[0026] FIG. 3 shows a further embodiment with the regeneration system 115 having a similar front end hydrocarbon removal system. The variation in this embodiment is having a two-stage regeneration system. The first stage 122 includes a membrane contactor cell 120 that acts like a bulk removal chamber of the prior art. Again, the solvent 118 enters the bulk removal regeneration cell 120 into the corresponding bulk removal solvent chamber. The bulk removal internal chamber includes a gas permeable membrane for separating the bulk removal internal chamber from the bulk removal solvent chamber. This allows for the diffusion of CO.sub.2 into the bulk removal internal chamber and consequent venting 125. In this first stage 122 no steam is used and hence a low temperature low pressure environment in the membrane contactor cell 120 efficiently removes a portion of the CO.sub.2 before delivering to the second stage 124. It will be noted that, whilst the steam flow is in a direction counter to the solvent flow, for the bulk removal regeneration cell the flow of CO.sub.2 is in the same direction as the solvent flow.

[0027] The second stage acts in a similar manner to that of the embodiment of FIG. 1 whereby the solvent having a reduced CO.sub.2 concentration enters the solvent chamber of a membrane contactor cell 135. Steam is introduced 150 into the internal chamber stripping the remaining CO.sub.2 from the solvent and venting 140 the CO.sub.2. The stripped solvent is then delivered 145 to a reboiler 155 which, as with the previous embodiment, directs steam back to the second stage cell 135 and regenerates the stripped solvent 160 back to the lean rich heat exchanger.

TABLE-US-00002 TABLE 2 Initial Final CO.sub.2 CO.sub.2 Liquid Inlet Liquid Outlet Vessel- Loading, Loading, Temperature, Temperature, volume/ mol/mol mol/mol ° C. ° C. flow Membrane 0.42 0.01 111 106 24.54 Regeneration System one stage 1.sup.st Stage 0.43 0.10 114 99 11.78 2.sup.nd Stage 0.10 0.01 99 105 Conventional 0.30 0.01 114 131 47.90 Using Column Regeneration MBC 1.sup.st Stage MBC 2.sup.nd Stage Module 1.5 cm ID, 50 cm length, Module 3.4 cm ID, 50 cm length, membrane area 0.22 m.sup.2 membrane area 0.56 m.sup.2 MBC liquid flow rate is 2.70 L/hr MBC liquid flow rate is 2.70 L/hr CO.sub.2 flux is 0.0223 kmol/(m.sup.2 .Math. hr) CO.sub.2 flux is 0.0022 kmol/(m.sup.2 .Math. hr) Vessel-volume/flow is 1.96 Vessel-volume/flow is 9.82

[0028] FIG. 4 shows a schematic view of a further embodiment of the present invention. Again the front end hydrocarbon removal system is the same. However, the cell for the regeneration side has been replaced by a cell having a heat element in place of the membrane isolated internal chamber. The arrangement is similar whereby CO.sub.2 latent solvent is introduced 175 into the new cell 170.

[0029] FIG. 5 shows an application of the embodiment shown in FIG. 4 with a cell 170 having a housing 210 with a central core 215 defining an internal chamber 225 and a solvent chamber having hollow fibre membranes 220. Steam enters 237 at inlet 235 the housing and travels along the internal core 215 exiting 247 from outlet 245 at the far end of the housing 210 to heat the solvent. The solvent enters 265 into the solvent chamber 220 and exits 260 at the opposed end of the housing 210. The solvent chamber 220 includes a gas permeable membrane whereby the carbon dioxide permeates into the tube side of the permeable membrane which then exits 255.