CO2 recovery device and method for cleaning filtration membrane device of CO2 recovery device

Abstract

A filtration membrane device which uses a filter to collect solid contents remaining in a branched lean solution cleans the filter by using a low-concentration CO.sub.2 absorption liquid circulating within the system as cleaning water (containing the absorption liquid); rough cleaning, which returns the low-concentration CO.sub.2 absorption liquid used for cleaning to a lean solution supply line, is performed; the filter is finish-cleaned by cleaning water from outside the system which does not include the CO.sub.2 absorption liquid; the CO.sub.2 absorption liquid which is adhered to the solid contents is washed and removed; finish-cleaning water which includes the CO.sub.2 absorption liquid is returned to the lean solution supply line the moisture content within the system is maintained at a prescribed value by adjusting the water balance in an absorption tower and the concentration of the CO.sub.2 absorption liquid which circulates within the system is kept at a prescribed concentration.

Claims

1. A CO.sub.2 recovery system comprising: an absorption tower which brings an exhaust gas containing CO.sub.2 into contact with a CO.sub.2 absorption liquid to remove CO.sub.2; an absorption liquid regeneration tower which regenerates a rich solution, which has absorbed CO.sub.2, through heat exchange; a rich solution supply line through which the rich solution is extracted from the absorption tower and is introduced into the absorption liquid regeneration tower; a lean solution supply line through which a lean solution from which CO.sub.2 regenerated in the absorption liquid regeneration tower has been emitted is extracted from the absorption liquid regeneration tower, and is introduced into the absorption tower, and the lean solution is reused as the CO.sub.2 absorption liquid in the absorption tower; and a filtration membrane device which is interposed in a lean-solution branch line branched from the lean solution supply line, a rich solution branch line branched from the rich solution supply line, or both the solution branch lines, and collects solid contents remaining in a branched solution using a filter, and returns filtrate, which has passed through the filter, to the lean solution supply line, the rich solution supply line or both the solution supply lines; wherein the filtration membrane device in which the filter has been used to collect the solid contents is configured to rough-clean the filter by using cleaning water containing CO.sub.2 absorption liquid circulating within a system; return rough-cleaning water to the lean solution supply line, the rich solution supply line or both the solution supply lines; finish-clean the filter by using cleaning water which does not include the CO.sub.2 absorption liquid and which is from outside the system to wash out and remove the CO.sub.2 absorption liquid which is adhered to the collected solid contents; return finish-cleaning water which includes the CO.sub.2 absorption liquid to the lean solution supply line, the rich solution supply line or both the solution supply lines; maintain a moisture content in the system at a prescribed value by adjusting a water balance in the absorption tower; and keep a concentration of the CO.sub.2 absorption liquid which circulates within the system at a prescribed concentration.

2. The CO.sub.2 recovery system according to claim 1, wherein the absorption tower is configured to adjust the water balance therein by controlling the temperature of cleaning water in a cleaning section.

3. The CO.sub.2 recovery system according to claim 1, wherein the absorption tower is configured to adjust the water balance therein by controlling the temperature of cooling water in a cooling tower which cools the exhaust gas containing CO.sub.2 before being introduced into the absorption tower.

4. The CO.sub.2 recovery system according to claim 1, wherein the absorption liquid regeneration tower includes: a separation drum which condenses steam in emission gas containing CO.sub.2 gas that has entrained the steam discharged from a top of the absorption liquid regeneration tower, and separates condensed water, wherein the absorption tower includes: a CO.sub.2 recovery section which brings the exhaust gas containing CO.sub.2 into contact with the CO.sub.2 absorption liquid to absorb CO.sub.2 in the exhaust gas; at least one or more cleaning sections which are disposed on a downstream side of the CO.sub.2 recovery section with respect to an exhaust gas flow, cool CO.sub.2-removed exhaust gas from which CO.sub.2 has been removed, and recover an entrained CO.sub.2 absorption liquid using the cleaning water; and a condensed water receiving section which is disposed on a bottom side of each of the cleaning sections, and recovers condensed water within the cleaning section, and wherein the system is configured to supply any one or both of the condensed water recovered in the condensed water receiving section of the absorption tower and the condensed water separated in the separation drum as the cleaning water containing the CO.sub.2 absorption liquid circulating within the system for the rough cleaning.

5. The CO.sub.2 recovery system according to claim 1, wherein the filtration membrane device is configured to remove the solid contents collected by the filter by performing reverse washing using gas or a cleaning liquid supplied from the outside of the system.

6. The CO.sub.2 recovery system according to claim 1, wherein at least two systems of the filters are provided in parallel in the lean solution branch line, the rich solution branch line or the both the solution branch lines, and alternately collect the solid contents in the branched solution.

7. The CO.sub.2 recovery system according to claim 1, wherein the CO.sub.2 absorption liquid is an amine-based absorption liquid.

8. A method for cleaning a filtration membrane device of a CO.sub.2 recovery system, comprising: bringing an exhaust gas containing CO.sub.2 into contact with a CO.sub.2 absorption liquid to remove CO.sub.2 in an absorption tower; regenerating a rich solution, which has absorbed CO.sub.2, through heat exchange in an absorption liquid regeneration tower; introducing the rich solution extracted from the absorption tower into the absorption liquid regeneration tower through a rich solution supply line; extracting a lean solution from which CO.sub.2 regenerated in the absorption liquid regeneration tower has been emitted from the absorption liquid regeneration tower to be introduced into the absorption tower through a lean solution supply line, and reusing the lean solution as the CO.sub.2 absorption liquid in the absorption tower; and collecting solid contents remaining in a branched solution in a lean solution branch line, a rich solution branch line, or both the branch lines using a filter, and returning filtrate, which has passed through the filter, to the lean solution supply line, the rich solution supply line or both the solution supply lines, wherein, the filter is rough-cleaned by cleaning water containing the CO.sub.2 absorption liquid circulating within the system; rough-cleaning water is returned to the lean solution supply line, the rich solution supply line or both the solution supply lines; the filter is finish-cleaned by cleaning water which does not include the CO.sub.2 absorption liquid and which is from outside the system to wash out and remove the CO.sub.2 absorption liquid which is adhered to the collected solid contents; finish-cleaning water which includes the CO.sub.2 absorption liquid is returned to the lean solution supply line, the rich solution supply line or both the solution supply lines; a moisture content in the system is maintained at a prescribed value by adjusting a water balance in the absorption tower; and a concentration of the CO.sub.2 absorption liquid which circulates within the system is kept at a prescribed concentration.

9. The method for cleaning the filtration membrane device of the CO.sub.2 recovery system according to claim 8, wherein any one or both of condensed water recovered in a condensed water receiving section of the absorption tower and condensed water separated in a separation drum are used as the cleaning water containing the CO.sub.2 absorption liquid circulating within the system for the rough cleaning.

10. The method for cleaning the filtration membrane device of the CO.sub.2 recovery system according to claim 8, wherein the CO.sub.2 absorption liquid is an amine-based absorption liquid.

11. The method for cleaning the filtration membrane device of the CO.sub.2 recovery system according to claim 8, wherein the water balance in the absorption tower is adjusted by controlling the temperature of cleaning water in a cleaning section.

12. The method for cleaning the filtration membrane device of the CO.sub.2 recovery system according to claim 8, wherein the water balance in the absorption tower is adjusted by controlling the temperature of cooling water in a cooling tower which cools the exhaust gas containing CO.sub.2 before being introduced into the absorption tower.

13. The method for cleaning the filtration membrane device of the CO.sub.2 recovery system according to claim 8, wherein the solid contents collected by the filter are removed by performing reverse washing using gas or a cleaning liquid supplied from the outside of the system.

Description

BRIEF DESCRIPTION OF DRAWINGS

(1) FIG. 1 is a schematic view of a CO.sub.2 recovery device related to Embodiment 1.

(2) FIG. 2-1 is a schematic view of the operation process of the filtration membrane device related to the present embodiment.

(3) FIG. 2-2 is a schematic view of the operation process of the filtration membrane device related to the present embodiment.

(4) FIG. 2-3 is a schematic view of the operation process of the filtration membrane device related to the present embodiment.

(5) FIG. 2-4 is a schematic view of the operation process of the filtration membrane device related to the present embodiment.

(6) FIG. 2-5 is a schematic view of the operation process of the filtration membrane device related to the present embodiment.

(7) FIG. 3 is a view illustrating the comparison between the amounts of loss of CO.sub.2 absorption liquid which adheres to solid contents in cleaning of filters and is discharged to the outside of a system, in the related art when a CO.sub.2 absorption liquid is used, and the present embodiment when finish cleaning is performed afterward.

(8) FIG. 4 is a flowchart illustrating steps of forming a coating layer on a filter and cleaning the filter.

(9) FIG. 5 is a schematic view of a CO.sub.2 recovery device related to Embodiment 2.

(10) FIG. 6 is a schematic view of a CO.sub.2 recovery device related to Embodiment 3.

DESCRIPTION OF EMBODIMENTS

(11) Preferred embodiments of the invention will be described below in detail with reference to the accompanying drawings. In addition, the invention is not limited by the embodiments and includes those configured by combining respective embodiments when there are a plurality of embodiments.

Embodiment 1

(12) FIG. 1 is a schematic view of the CO.sub.2 recovery device related to Embodiment 1. As illustrated in FIG. 1, a CO.sub.2 recovery device 10A related to the present embodiment includes an absorption tower 1004 which brings exhaust gas 1001A containing CO.sub.2 into contact with a CO.sub.2 absorption liquid 1005 to remove CO.sub.2; an absorption liquid regeneration tower 1006 which regenerates a rich solution 1005A, which has absorbed CO.sub.2, through heat exchange; a rich solution supply line L.sub.12 through which the rich solution 1005A is extracted from the absorption tower 1004 and is introduced into the absorption liquid regeneration tower 1006 side; a lean solution supply line L.sub.13 through which a lean solution 1005B into which CO.sub.2 regenerated in the absorption liquid regeneration tower 1006 has been emitted is extracted from the absorption liquid regeneration tower 1006, and is introduced into the absorption tower 1004, and the lean solution 1005B is reused as the CO.sub.2 absorption liquid in the absorption tower 1004; and a filtration membrane device 13 which is interposed in a lean solution branch line L.sub.21 branched from the lean solution supply line L.sub.13, collects solid contents 11 remaining in the branched lean solution 1005B-1 using the filter 12, and returns filtrate 1005B-2, which has passed through the filter 12, to the lean solution supply line L.sub.13. With respect to the filtration membrane device 13 when the filter 12 has been used to collect the solid contents 11, the filter 12 is cleaned using a low-concentration CO.sub.2 absorption liquid as cleaning water (containing the absorption liquid) 16A, the low-concentration CO.sub.2 absorption liquid circulating within a system; rough cleaning, which returns the low-concentration CO.sub.2 absorption liquid used for cleaning to the lean solution supply line L.sub.13, is performed; the filter 12 is finish-cleaned by cleaning water 21 which does not include the CO.sub.2 absorption liquid and which is from outside the system; the CO.sub.2 absorption liquid which is adhered to the collected solid contents 11 is washed and removed; finish-cleaning water which includes the CO.sub.2 absorption liquid is returned to the lean solution supply line L.sub.13; the moisture content within the system is maintained at a prescribed value by adjusting the water balance within the absorption tower 1004; and the concentration of the CO.sub.2 absorption liquid which circulates within the system is kept at a prescribed concentration.

(13) In the present embodiment, the absorption liquid regeneration tower 1006 includes a separation drum 1026 which condenses steam in emission gas 1007 containing CO.sub.2 gas that has entrained the steam discharged from the top of the absorption liquid regeneration tower as condensed water 1028, and separates the condensed water 1028. Additionally, the absorption tower 1004 includes a CO.sub.2 recovery section 1010 which brings the exhaust gas containing CO.sub.2 into contact with the CO.sub.2 absorption liquid to absorb CO.sub.2 in the exhaust gas 1001A containing CO.sub.2; a first cleaning section 1013-1 which is disposed on an upper stage side of the CO.sub.2 recovery section 1010, cools CO.sub.2-removed exhaust gas 1001B from which CO.sub.2 has been removed, and recovers an entrained CO.sub.2 absorption liquid using cleaning water 1013a; and a condensed water receiving section 1015a which is disposed on a lower side of the first cleaning section 1013-1, and recovers condensed water 1014 generated within the first cleaning section 1013-1. As the cleaning water 1013a used in the first cleaning section 1013-1, a portion of the condensed water 1028 separated by the separation drum 1026 is supplied by a condensed water supply line L.sub.24.

(14) Also, in the present embodiment, a portion of the condensed water 1014 which includes the CO.sub.2 absorption liquid 1005 recovered in the condensed water receiving section 1015a is used as cleaning water 16A which cleans the filter 12 so as to be supplied to the filtration membrane device 13 via a cleaning water supply line L.sub.15.

(15) In a CO.sub.2 recovery method using the CO.sub.2 recovery device 10A, in the absorption tower 1004, the CO.sub.2-containing exhaust gas 1001A comes into countercurrent contact with the CO.sub.2 absorption liquid 1005 supplied from nozzles 1011 that are liquid dispersers, in the CO.sub.2 recovery section 1010 provided on a lower part side of the absorption tower 1004, and CO.sub.2 in the CO.sub.2-containing exhaust gas 1001A is absorbed by the CO.sub.2 absorption liquid 1005 according to, for example, a chemical reaction (RNH.sub.2+H.sub.2O+CO.sub.2.fwdarw.RNH.sub.3HCO.sub.3).

(16) Then, the CO.sub.2-removed exhaust gas 1001B after CO.sub.2 has been removed comes into gas-liquid contact with the cleaning water 1013a which includes the CO.sub.2 absorption liquid 1005 supplied from the nozzles 1011 in the first cleaning section 1013-1, and the CO.sub.2 absorption liquid 1005 entrained in the CO.sub.2-removed exhaust gas 1001B is recovered. Additionally, the condensed water 1014 which includes the CO.sub.2 absorption liquid 1005 recovered in the condensed water receiving section 1015a is supplied via the first liquid circulation line L.sub.14, and is reused as the cleaning water for the first cleaning section 1013-1.

(17) The rich solution 1005A with high CO.sub.2 concentration into which CO.sub.2 has been absorbed is supplied to the absorption liquid regeneration tower 1006 side via the rich solution supply line L.sub.12 by a rich solvent pump P.sub.1, is introduced into the tower from the vicinity of a tower top 1006a of the absorption liquid regeneration tower 1006, and causes an endothermic reaction with steam indirectly heated with saturated water vapor 1021 in a reboiler 1020 when flowing downward within the tower, and most of the CO.sub.2 is emitted and regenerated. In addition, the saturated water vapor 1021 is discharged as condensed water 1020 from the reboiler 1020.

(18) Additionally, the CO.sub.2 gas 1007 that has entrained the steam discharged from the rich solution 1005A inside the tower is led out from the tower top 1006a of the absorption liquid regeneration tower 1006. Then, with respect to the CO.sub.2 gas 1007 that has entrained the steam, the steam is condensed by a cooling section 1025, water is separated as the condensed water 1028 by the separation drum 1026, and only the CO.sub.2 gas 1027 is discharged and recovered to the outside of the system. The condensed water 1028 separated by the separation drum 1026 is supplied to an upper part of the absorption liquid regeneration tower 1006, an upper part of the absorption tower 1004, and the like, and adjusts water balance within the closed system.

(19) The lean solution 1005B with low CO.sub.2 concentration regenerated in the absorption liquid regeneration tower 1006 is subjected to heat exchange with the rich solution 1005A by a heat exchanger 1016 and is cooled, is then raised in pressure by a lean solvent pump P.sub.2, and is further cooled by the lean solvent cooler. Thereafter, the lean solution is supplied again to the absorption tower 1004 and is circulated and reused as a CO.sub.2 absorption liquid.

(20) In the present embodiment, when such CO.sub.2 recovery is performed and when there is an improvement in the concentration of the solid contents 11 in the lean solution 1005B, the lean solution 1005B-1 is introduced into the filtration membrane device 13, and the solid contents 11 remaining in the lean solution 1005B-1 are collected by the filter 12, so that the lean solution 1005B-2 from which the solid contents 11 have been removed can be supplied to the lean solution supply line L.sub.13.

(21) Accordingly, the concentration of the solid contents in the CO.sub.2 absorption liquid which circulates through the absorption tower 1004 and the absorption liquid regeneration tower 1006 can be reduced.

(22) Next, the removal operation of the solid contents 11 in the filtering device 13 and the cleaning operation of the filter 12 will be described.

(23) FIGS. 2-1 to 2-5 are schematic views of an operation process of the filtration membrane device related to the present embodiment.

(24) In a normal CO.sub.2 recovery operation, as illustrated in FIG. 2-1, when circulation is made through the absorption tower 1004 and the absorption liquid regeneration tower 1006, the CO.sub.2 absorption liquid 1005 (lean solution 1005B) is circulated and reused within the closed system by closing valves V.sub.11 and V.sub.12 and releasing a valve V.sub.13.

(25) In contrast, in the operation of removing the solid contents 11, as illustrated in FIG. 2-2, the valves V.sub.11 and V.sub.12 are opened while the lean solution 1005B-1 is filtered by the filtration membrane device 13. Accordingly, the lean solution 1005B-1 which has been partly extracted from the lean solution supply line L.sub.13 is supplied into a filtration membrane device body 17 via the lean solution branch line L.sub.21 through which the lean solution 1005B-1 is supplied to the filtration membrane device 13 side, and the solid contents 11 remaining in the lean solution 1005B-1 are collected by the filter 12. Then, the lean solution 1005B-2 from which the solid contents 11 have been removed is supplied to the lean solution supply line L.sub.13 via the lean solution branch line L.sub.21.

(26) Next, after the separation of the solid contents 11 is completed, as illustrated in FIG. 2-3, a valve V.sub.16 of the cleaning water supply line L.sub.15 is released, and the low-concentration CO.sub.2 absorption liquid circulating within the system is supplied into the filter device body 17 as the cleaning water 16A. By virtue of the supply of the cleaning water 16A, the CO.sub.2 absorption liquid adhering to the filter 12 is recovered in the cleaning water 16A, and rough cleaning of the filter 12 is performed.

(27) After this rough cleaning is completed, as illustrated in FIG. 2-4, the valve V.sub.16 of the cleaning water supply line L.sub.15 is closed, a valve V.sub.17 of a cleaning water supply line L.sub.23 is released, and the cleaning water 21 which does not include the CO.sub.2 absorption liquid is supplied into the filtration membrane device body 17. Finish cleaning which cleans and removes the CO.sub.2 absorption liquid adhering to the filter 12 and the solid contents 11 is performed by the cleaning water 21 which does not include the CO.sub.2 absorption liquid supplied from the outside.

(28) By performing this finish cleaning, the CO.sub.2 absorption liquid adhering to the filter 12 and the solid contents 11 which could not be removed in the rough cleaning can be cleaned and removed.

(29) The finish-cleaning water 21a which includes the CO.sub.2 absorption liquid which has performed this finish cleaning is supplied to the lean solution supply line L.sub.13 via a return line L.sub.22, and is introduced into the absorption tower 1004.

(30) Since the water from the outside is introduced as a result of introducing the finish-cleaning water 21a into the absorption tower 1004, the amount of water within the closed system increases. Hence, in the present embodiment, the operation of adjusting the water balance within the absorption tower 1004 to keep the moisture content within the system at a prescribed value, and keeping the concentration of the CO.sub.2 absorption liquid circulating within the system at a prescribed concentration is performed.

(31) Next, the adjustment operation of the water balance of the CO.sub.2 absorption liquid will be described referring to FIG. 1.

(32) A first adjustment operation of the water balance of the CO.sub.2 absorption liquid is performed by controlling the temperature of the cleaning water 1013a in the first cleaning section 1013-1. Specifically, the temperature of the cleaning water 1013a in the first cleaning section 1013-1 is adjusted in a heat exchange unit 1013b. Specifically, the amount of entrainment of water into the CO.sub.2-absorption-solution-removed exhaust gas 1001C is increased by maintaining a high heat exchange temperature in the heat exchange unit 1013b when heat exchange of the cleaning water 1013a is performed and by evaporating the moisture in the cleaning water 1013a when passing through the first cleaning section 1013-1. Accordingly, the moisture content discharged to the outside of the system is increased.

(33) In addition, as confirmation of the water balance, the amount of stored water within a water storage part 1004b of the bottom part of the absorption tower 1004 is measured by a level meter 31. Then, as a result of the measurement of the level meter 31, a command is issued from a control unit 32 so that a command (.sub.1) of adjusting the temperature in the heat exchange unit 1013b becomes proper and so that the water balance becomes proper. Here, as in the present embodiment, a worker operates the water balance properly without using the control unit 32.

(34) Hence, in the related art, the cleaning of the filter 12 is performed using the cleaning water 1013a with a low-concentration CO.sub.2 absorption liquid, as the cleaning water 16A. However, since the CO.sub.2 absorption liquid could not be removed to a value equal to or lower than the concentration even at a low concentration, discharged solid contents were discarded to the outside with the CO.sub.2 absorption liquid adhered thereto, and there was loss of the CO.sub.2 absorption liquid.

(35) In contrast, in the present invention, the finish cleaning of the filter 12 is performed using the cleaning water 21 which does not include the CO.sub.2 absorption liquid at all after the rough cleaning is performed using the cleaning water 1013a with the low-concentration CO.sub.2 absorption liquid as the cleaning water 16A. Thus, in the related art, the CO.sub.2 absorption liquid adhering to the solid contents 11 discarded to the outside as discharged solid contents as it is can be recovered. As a result, reduction of the amount of loss of the CO.sub.2 absorption liquid and efficient removal of the solid contents from the lean solution 1005B can be achieved.

(36) FIG. 3 is a view illustrating the comparison between the amounts of loss of CO.sub.2 absorption liquid which adheres to solid contents in cleaning of filters and is discharged to the outside of a system, in the related art when a CO.sub.2 absorption liquid is used, and the present embodiment when the finish cleaning is performed afterward.

(37) In a case where the loss when the low-concentration CO.sub.2 absorption liquid of the related art illustrated on the right side of FIG. 3 is 100, the amount of loss to be discharged to the outside of the system is reduced to by performing both the rough cleaning and the finish cleaning on the filter 12.

(38) Additionally, a second adjustment operation of the water balance of the CO.sub.2 absorption liquid is performed by controlling the temperature of the cooling water 1031 in the cooling tower 1030, which cools the CO.sub.2-containing exhaust gas 1001A before being introduced into the absorption tower 1004, using the heat exchange unit 1032. Specifically, the heat exchange temperature in the heat exchange unit 1032 which performs heat exchange of the temperature of the cooling water 1031 in the cooling tower 1030 is made low, moisture is condensed in the cooling tower 1030, and the amount of entrainment of water into the CO.sub.2-containing exhaust gas 1001A is lowered so that the amount of moisture to be introduced into the absorption tower 1004 is lowered.

(39) In addition, as confirmation of the water balance, the amount of stored water within a water storage part 1004b of the bottom part of the absorption tower 1004 is measured by a level meter 31, and a command (.sub.2) of adjusting the temperature in the heat exchange unit 1032 is issued from the control unit 32 so that the water balance becomes proper. In addition, a worker operates the water balance properly without using the control unit 32.

(40) As a result of the adjustment of the water balance, for example, when the concentration of the CO.sub.2 absorption liquid in the CO.sub.2 absorption liquid 1005 is targeted at, for example, 30%, water is supplied as the cleaning water 21 from the outside, so that the CO.sub.2 absorption liquid 1005 in the absorption tower 1004 is prevented from being diluted to 29%, and 30% that is a targeted management value can always be maintained.

(41) Additionally, as the filter 12, it is preferable to use cartridge filters, precoat filters, metal slit filters, wire net filters, and sintered metal filters. However, the invention is not limited to these. For example, arbitrary filters, such as hollow fiber membranes and MF membranes (microfiltration membranes), may be used as long as the solid contents 11 in the CO.sub.2 absorption liquid 1005, can be filtered.

(42) Additionally, any of natural filtration, pressure filtration, filtration under reduced pressure, and centrifugal filtration may be applied as a filtration method.

(43) Additionally, a method for replacing a filter when using a precoat filter as the filter 12 will be described.

(44) FIG. 4 is a flowchart illustrating steps of forming a coating layer on the filter and cleaning the filter.

(45) As illustrated in FIG. 4, when the precoat filter is used as the filter 12, the filter 12 is obtained by forming a coating layer on the filter 12, using the cleaning water 16A as a low-concentration CO.sub.2 absorption liquid in which a filter medium has been dissolved.

(46) That is, when the precoat filter is used as the filter 12, as illustrated in FIG. 4, the method includes a coating layer forming step S11 of forming a coating layer in the surface of the filter 12; a solid contents filtering step S12 of filtering and removing the solid contents 11 in the CO.sub.2 absorption liquid 1005; a rough cleaning step S13 of recovering the CO.sub.2 absorption liquid 1005 adhering to the surface of the filter 12, using the cleaning water 16A, and cleaning the filter 12; and a finish cleaning step S14 of performing finish cleaning of the filter 12, using the cleaning water 21 which does not include CO.sub.2 supplied from the outside.

(47) First, in the coating layer forming step S11, the coating layer is formed by dissolving a filter medium constituting the coating layer of the filter 12 in the cleaning water 16A and making the cleaning water 16A in which the filter medium has been dissolved adhere to the filter 12.

(48) Then, in the solid contents filtering step S12, the branched CO.sub.2 absorption liquid 1005B-1 is supplied to the filtration membrane device 13 via the lean solution branch line L.sub.21, the lean solution 1005B-1 is filtered by the filter 12, and the solid contents 11 remaining in the lean solution 1005B-1 are collected. Then, the lean solution 1005B-2 from which the solid contents 11 have been removed is supplied to the lean solution supply line L.sub.13 (refer to FIG. 2-2).

(49) Then, in the filter rough cleaning step S13, the cleaning water 16A is supplied to the filtration membrane device 13, the CO.sub.2 absorption liquid 1005 adhering to the filter 12 is recovered in the cleaning water 16A, and the rough cleaning of the filter 12 is performed (refer to FIG. 2-3).

(50) Then, in the finish cleaning step S14, the cleaning water 21 which does not include the CO.sub.2 absorption liquid is supplied from the outside to the filtration membrane device 13, the CO.sub.2 absorption liquid 1005 adhering to the filter 12 is collected in the cleaning water 21, the filter 12 is cleaned, and the CO.sub.2 absorption liquid adhering to the solid contents 11 collected in the filter is recovered (refer to FIG. 2-4). Accordingly, reduction of the amount of loss of the absorption liquid adhering to the discharged solid contents and efficient removal of the solid contents from the CO.sub.2 absorption liquid can be achieved.

(51) After this series of cleaning of the filter 12 is completed, the coating layer to which the solid contents 11 and the solid contents 11 adhere are discarded (S15).

(52) In this solid contents discarding step S15, the cleaning water 21 is first drained, and air is supplied from the same direction as normal cleaning to perform drying. Thereafter, compressed air 18 is supplied into the filtration membrane device body 17 from a reverse direction, the filter medium is blown away, and the coating layer is removed as waste 19 (refer to FIG. 2-5).

(53) The removed filter medium is discarded to the outside as the waste 19. However, since the CO.sub.2 absorption liquid adhering to the filter medium and the solid contents collected by this filter medium are removed, the waste loss of the CO.sub.2 absorption liquid is almost eliminated in the filter cleaning operation.

(54) Then, similar to the above-described one, a coating layer is newly formed again on the filter 12, using the cleaning water 16A in which the filter medium has been dissolved.

(55) If the amount of exhaust gas is, for example, 1,000,000 Nm.sup.3/H, and the general amount of dust and soot is 5.0 mg/Nm.sup.3, it is necessary to remove the dust and soot, which has not been removed in the cooling tower 1030 or a desulfurization device (not illustrated), in the absorption tower 1004. In this case, the amount of dust and soot to be removed in the absorption tower 1004 becomes as large as 1,000,000 (Nm.sup.3/H)5.0 (mg/Nm.sup.3)=5.0 kg/H. Additionally, generally, since the amount of collection of the dust and soot per one filter is about 100 g to 200 g, replacement of about 50 filters/H is required.

(56) In contrast, when the filter 12 is cleaned and the coating layer is formed, the water circulating within the system is used. Accordingly, even if the amount of dust and soot removed in the absorption tower 1004 becomes large, a relatively large amount of the solid contents in the lean solution can be continuously processed in a short time.

(57) Additionally, in the cleaning of the filter 12, the cleaning water 16A which includes the low-concentration CO.sub.2 absorption liquid within the system is used, and the finish cleaning is performed using the cleaning water 21 which does not include the CO.sub.2 absorption liquid from the outside of the system after the rough cleaning is performed. Thus, reduction of the amount of loss of the CO.sub.2 absorption liquid adhering to the discharged solid contents and efficient removal of the solid contents from the CO.sub.2 absorption liquid can be achieved.

(58) Also, a proper CO.sub.2 recovery operation is performed by adjusting the water balance in the system according to the amount of the cleaning water introduced from the outside and always maintaining the proper concentration of the CO.sub.2 absorption liquid.

(59) In this way, according to the CO.sub.2 recovery device 10A related to the present embodiment, in a step of cleaning the filter 12 which has filtered the solid contents 11 remaining in the CO.sub.2 absorption liquid 1005, such as amine, a decrease in the concentration of the CO.sub.2 absorption liquid 1005 can be prevented, and the loss of the CO.sub.2 absorption liquid 1005 can be markedly reduced.

(60) Accordingly, it is also possible to apply the CO.sub.2 recovery device invention to coal fired boilers, and even if the CO.sub.2 recovery device is enlarged, and the amount of dust and soot removed in the absorption tower 1004 becomes as large as, for example, 5.0 kg/H, a relatively large amount of the solid contents in the lean solution can be continuously processed in a short time.

(61) In the present embodiment, one filtration membrane device 13 provided with the filter 12 is provided to remove the solid contents. However, at least two systems of filtration membrane devices may be provided in parallel in the lean solution branch line L.sub.21, the solid contents in the CO.sub.2 absorption liquid may be alternately collected, cleaning is performed by the cleaning liquid 21 which does not include the CO.sub.2 absorption liquid supplied from the outside of the system, and thereafter, the water balance may be adjusted.

(62) Accordingly, since the solid contents in the lean solution can be removed by the filter 12 in the other system even when the filter 12 is cleaned by one system of the filtration membrane device 13, separation of the solid contents and regeneration of the filter 12 can be continuously and alternately performed.

(63) As a result, continuous operation of a reduction of the amount of loss of the CO.sub.2 absorption liquid adhering to the discharged solid contents, and the efficient removal of the solid contents from the CO.sub.2 absorption liquid can be achieved.

(64) In the present embodiment, a case where the lean solution 1005B is used as a solution to be supplied to the filtration membrane device 13 has been described. However, the invention is not limited to this, and the rich solution 1005A may be used. Additionally, the filter 12 may be cleaned using a solution in which both the rich solution 1005A and the lean solution 1005B are mixed together.

Embodiment 2

(65) A CO.sub.2 recovery device related to Embodiment 2 according to the invention will be described with reference to FIG. 5.

(66) FIG. 5 is a schematic view of the CO.sub.2 recovery device related to Embodiment 2 of the invention. In the drawing, the same components as the CO.sub.2 recovery device 10A of Embodiment 1 of the invention illustrated in FIG. 1 will be designated by the same reference numerals, and duplicate description will be omitted.

(67) In Embodiment 1, the cleaning liquid 1013a in the absorption tower 1004 is used as the cleaning water which includes the low-concentration CO.sub.2 absorption liquid. However, the condensed water 1028 separated by the separation drum 1026 is used as cleaning water 16B in the present embodiment.

(68) That is, the CO.sub.2 recovery device 10B related to the present embodiment, as illustrated in FIG. 5, has the cleaning water supply line L.sub.15 branching from the condensed water supply line L.sub.24 through which the condensed water 1028 separated by the separation drum 1026 is supplied to the lean solution branch line L.sub.21.

(69) Since the condensed water 1028 which includes the low-concentration CO.sub.2 absorption liquid can be supplied to the lean solution branch line L.sub.21 by providing the cleaning water supply line L.sub.15 branching from the condensed water supply line L.sub.24, the condensed water 1028 can be used as the cleaning water 16B.

Embodiment 3

(70) A CO.sub.2 recovery device related to Embodiment 3 according to the invention will be described with reference to FIG. 6.

(71) FIG. 6 is a schematic view of the CO.sub.2 recovery device related to Embodiment 3 of the invention. In the drawing, the same components as the CO.sub.2 recovery device 10A of Embodiment 1 of the invention illustrated in FIG. 1 will be designated by the same reference numerals, and duplicate description will be omitted.

(72) As illustrated in FIG. 6, in a CO.sub.2 recovery device 10C related to the present embodiment, a second cleaning section 1013-2 is provided between the first cleaning section 1013-1 in Embodiment 1 and the CO.sub.2 recovery section 1010.

(73) The first cleaning section 1013-1 performs cleaning of the CO.sub.2-absorption-solution-removed exhaust gas 1001C to be emitted, using the condensed water 1028 which includes the low-concentration CO.sub.2 absorption liquid separated by the separation drum 1026, similar to Embodiment 1.

(74) The second cleaning section 1013-2 supplies a portion of the condensed water 1014 from the first cleaning section 1013-1 via the supply line L.sub.18 to the circulation line L19, circulates this condensed water as cleaning water 1013c using a pump P.sub.7, and cleans and removes the CO.sub.2 absorption liquid remaining in the CO.sub.2-removed exhaust gas 1001B which has recovered CO.sub.2 using CO.sub.2 recovery section 1010.

(75) Here, in the present embodiment, the amount of entrainment of water into the CO.sub.2-absorption-solution-removed exhaust gas 1001C is increased by maintaining a high heat exchange temperature in the heat exchange unit 1013d interposed in the circulation line L.sub.19 when heat exchange of the cleaning water 1013c is performed and by evaporating the moisture in the cleaning water 1003c when passing through the second cleaning section 1013-2. Accordingly, the moisture content discharged to the outside of the system is increased.

(76) In the present embodiment, the cleaning water 16A is supplied from the circulation line L.sub.19 via the cleaning water supply line L.sub.15 to the filtration membrane device 13.

(77) In order to prevent the cleaning performance of the finish cleaning of the first cleaning section 1013-1 on the upper stage side from degrading, the cleaning water 1013a in the first cleaning section 1013-1 on the upper part side of the absorption tower is not used as the cleaning water of the filter 12 of the filtration membrane device 13 unlike Embodiment 1.

REFERENCE SIGNS LIST

(78) 10A TO 10C: CO.sub.2 RECOVERY DEVICE 11: SOLID CONTENT 12: FILTER 13: FILTRATION MEMBRANE DEVICE 16A, 16B: CLEANING WATER (CONTAINING ABSORPTION SOLUTION) 21: CLEANING WATER WHICH DOES NOT INCLUDE CO.sub.2 ABSORPTION LIQUID (NO ABSORPTION LIQUID) 17: FILTRATION MEMBRANE DEVICE BODY 1001A: CO.sub.2-CONTAINING EXHAUST GAS 1001B: CO.sub.2-REMOVED EXHAUST GAS 1001C: CO.sub.2-ABSORPTION-SOLUTION-REMOVED EXHAUST GAS 1004: ABSORPTION TOWER 1005: CO.sub.2 ABSORPTION LIQUID 1005A: RICH SOLUTION 1005B: LEAN SOLUTION 1006: ABSORPTION LIQUID REGENERATION TOWER 1010: CO.sub.2 RECOVERY SECTION 1030: COOLING TOWER 1031: COOLING WATER