System and method for recovering gas containing CO2 and H2S

Abstract

The system includes: an absorber which brings an introduction gas into contact with an absorbent that absorbs CO.sub.2 and H.sub.2S; an absorbent regenerator which releases CO.sub.2 or the like to regenerate the absorbent; a second supply line which returns a regenerated absorbent to the absorber from the regenerator; a third supply line which extracts a semi-rich solution from the vicinity of a middle stage of the absorber, and introduces the semi-rich solution to the vicinity of the middle stage of the regenerator; and a semi-rich solution heat exchanger which is interposed at an intersection between the third supply line and the second supply line to perform the heat exchange between the semi-rich solution and the lean solution.

Claims

1. A method for recovering a gas containing CO2 and H2S using an absorber and a regenerator, the method comprising: extracting a semi-rich solution which has absorbed a part of CO2 and H2S contained in an introduction gas from the vicinity of a middle stage of the absorber to be introduced into the vicinity of a middle stage of the regenerator; extracting a rich solution which has absorbed CO2 and H2S contained in the introduction gas from a bottom portion of the absorber to be introduced into the vicinity of a top portion of the regenerator; separating a non-condensable gas including N2, H2 and CO contained in the semi-rich solution in a first flash drum prior to introduction into the vicinity of the middle stage of the regenerator, and separating a non-condensable gas including N2, H2 and CO contained in the rich solution in a second flash drum prior to introduction into the vicinity of the top portion of the regenerator; heat-exchanging the semi-rich solution with a lean solution regenerated by removing CO2 and H2S contained in the semi-rich solution and the rich solution in the regenerator; cooling water vapor accompanied by CO2 and H2S gas released from the regenerator with a condenser to condense the water vapor into water; separating the water and the CO2 and H2S gas in a separation drum; and joining the CO2 and H2S separated in the separation drum and the non-condensable gas separated in the first and second flash drums.

Description

BRIEF DESCRIPTION OF DRAWINGS

(1) FIG. 1 is a schematic diagram of a recovery system of a gas containing CO.sub.2 and H.sub.2S according to a first embodiment.

(2) FIG. 2 is a schematic diagram in which an example of a temperature condition of the recovery system of the gas containing CO.sub.2 and H.sub.2S according to the first example is added.

(3) FIG. 3 is a schematic diagram in which an example of a temperature condition of the recovery system of the gas containing CO.sub.2 and H.sub.2S according to a conventional example is added.

DESCRIPTION OF EMBODIMENTS

(4) The present invention will be described in detail below with reference to the accompanying drawings. The present invention is not to be limited to the examples. In addition, constituent elements in the examples include those that can be easily assumed by a person skilled in the art or those that are substantially identical.

(5) First Example

(6) A recovery system of a gas containing CO.sub.2 and H.sub.2S according to an example of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of a recovery system of a gas containing CO.sub.2 and H.sub.2S according to the first example.

(7) As illustrated in FIG. 1, a recovery system 10 of the gas containing CO.sub.2 and H.sub.2S according to this example includes an absorber 13 which uses a gasified gas containing CO.sub.2 and H.sub.2S obtained from a gasification furnace for gasifying, for example, the coal, the biomass or the like, as an introduction gas 11, and brings the introduction gas 11 into contact with an absorbent 12 which absorbs CO.sub.2 and H.sub.2S to absorb CO.sub.2 and H.sub.2S from the introduction gas 11; an absorbent regenerator (hereinafter, referred to as a “regenerator”) 14 which extracts an absorbent (rich solution) 12A, which has absorbed CO.sub.2 and H.sub.2S from a bottom portion 13c of the absorber 13, introduces the absorbent from a top portion 14a via a first supply line L.sub.1, and releases CO.sub.2 and H.sub.2S by the heat of a reboiler 15 to regenerate the absorbent 12; a second supply line L.sub.2 which discharges a regenerated absorbent (lean solution) 12B from a bottom portion 14c of the regenerator 14 and returns the regenerated absorbent to a top portion 13a of the absorber 13; a third supply line L.sub.3 which extracts an absorbent (semi-rich solution) 12C which has absorbed a part of CO.sub.2 and H.sub.2S from the vicinity of a middle stage 13b of the absorber 13, and introduces the extracted semi-rich solution 12C to the vicinity of a middle stage 14b of the regenerator 14; and a semi-rich solution heat exchanger 17 which is interposed at an intersection between the third supply line L.sub.3 and the second supply line L.sub.2 to perform the heat exchange between the semi-rich solution 12C and the lean solution 12B.

(8) In this system, CO.sub.2 and H.sub.2S are removed in the regenerator 14 and the regenerated absorbent (lean solution) 12B is reused as the absorbent 12.

(9) In a purifying method using the recovery system 10 of the gas containing CO.sub.2 and H.sub.2S, the gasified gas obtained in the gasification furnace for gasifying the coal, the biomass, or the like is sent to a gas cooling device (not illustrated), is cooled here by the cooling water and is introduced into the absorber 13 as the introduction gas 11.

(10) Filling portions 13A, 13B are provided inside the absorber 13 to improve the countercurrent contact efficiency of the introduction gas 11 and the absorbent 12, when passing through the filling portions 13A, 13B. In addition, a plurality of filling portions may be provided, and the countercurrent contact between the introduction gas 11 and the absorbent 12 may be performed, for example, by a spray method, a liquid column method, a tray method or the like other than the filling method.

(11) In the absorber 13, the introduction gas 11, for example, comes into countercurrent-contact with the amine-based absorbent 12, CO.sub.2 and H.sub.2S in the introduction gas 11 are absorbed by the absorbent 12 by a chemical reaction, and purified gas 21 from which CO.sub.2 and H.sub.2S are removed is discharged out of the system. The absorbent 12 which absorbs CO.sub.2 and H.sub.2S is also referred to as “rich solution” 12A. The rich solution 12A is supplied to the top portion 14a side of the absorbent regenerator 14 without heat exchange via a rich solution pump (not illustrated), while keeping the low temperature.

(12) When the rich solution 12A introduced from the top portion 14a side is introduced into the regenerator from the vicinity of the top portion 14a of the regenerator 14 having filling portions 14A and 14B by a spraying means (not illustrated) or the like and flows down in the regenerator, the rich solution 12A generates an endothermic reaction due to water vapor 22 from the reboiler 15, and discharges and regenerated most of CO.sub.2 and H.sub.2S. The absorbent 12, which has released a part or the most of CO.sub.2 and H.sub.2S in the absorbent regenerator 14, is referred to as “semi-lean solution”. When reaching the lower part of the regenerator 14, the semi-lean solution becomes the absorbent in which substantially all of CO.sub.2 and H.sub.2S have been removed. The absorbent regenerated by substantially all of CO.sub.2 and H.sub.2S are removed is referred to as “lean solution” 12B. The lean solution 12B is indirectly heated by saturated water vapor 23 in the reboiler 15, generates the water vapor 22, and is returned to the bottom portion 14c side of the regenerator 14.

(13) Further, CO.sub.2 and H.sub.2S gas 25 accompanied by water vapor released from the rich solution 12A and the semi-lean solution in the regenerator is derived from the top portion 14a of the regenerator 14, the water vapor is condensed by a condenser 26, water 28 is separated by a separation drum 27, and CO.sub.2 and H.sub.2S gas 29 is released and recovered to the outside of the system. The water 28 separated by the separation drum 27 is supplied to the top portion 14a of the absorbent regenerator 14.

(14) The regenerated absorbent (lean solution) 12B is cooled by being heat-exchanged with the semi-rich solution 12C by the semi-rich solution heat exchanger 17, the pressure thereof is subsequently increased in a lean solvent pump (not illustrated), and after the regenerated absorbent is cooled by a lean solvent cooler 30, it is supplied to the absorber 13 again and is reused as the absorbent 12.

(15) In this example, a part of the absorbent 12 is extracted from the vicinity of the middle stage 13b below the uppermost stage of the absorber 13 by the third supply line L.sub.3. In addition, the extraction amount is adapted to measure the temperature, the pressure, the flow rate, the CO.sub.2 density, the H.sub.2S density or the like of the introduction gas to be introduced, and collectively determine these conditions, thereby determining an optimum extraction position and extraction amount.

(16) The extracted semi-rich solution 12C is heated by heat exchange with the high-temperature lean solution 12B extracted from the bottom portion 14c of the regenerator 14 by the semi-rich solution heat exchanger 17, and is supplied downward from the vicinity of the middle stage 14b of the regenerator 14, and more preferably, from the middle stage 14b.

(17) Incidentally, CO.sub.2 in the introduction gas 11 is absorbed by the absorbent 12 together with H.sub.2S within the absorber 13.

(18) As in the present invention, by reducing the flow rate of the absorbent flowing down below the absorber 13 so as to extract a part of the absorbent from the vicinity of the middle stage 13b of the absorber 13 by the third supply line L.sub.3, since the mass transfer of the gas side is dominant in H.sub.2S and the mass transfer of the liquid side is dominant in CO.sub.2, the absorption rate of CO.sub.2 is further lowered.

(19) Thus, as the CO.sub.2 absorption amount is lowered, that is, the CO.sub.2 density in the absorbent is lowered, the absorption amount of H.sub.2S increases.

(20) Even in consideration of a decrease in the H.sub.2S absorption amount due to a decrease in the flow rate of the absorbent 12, the H.sub.2S absorption amount hardly decreases.

(21) Therefore, it is possible to improve the selectivity of H.sub.2S.

(22) By introducing the rich solution 12A having the high CO.sub.2 and H.sub.2S density from the top portion 14a of the regenerator 14 without heat exchange, and by supplying the semi-rich solution 12C having relatively lower CO.sub.2 and H.sub.2S density than the rich solution 12A to the vicinity of the middle stage 14b of the regenerator 14 or to the lower side thereof after heating by the semi-rich solution heat exchanger 17, it is possible to reduce the heating capacity of the reboiler 15. Thus, it is possible to reduce the water vapor consumption due to the reboiler 15.

(23) In addition, in this example, the rich solution 12A and the semi-rich solution 12C extracted from the absorber 13 are introduced to each of flash drums 31, 32 to separate non-condensable gas 33 (33a, 33b) such as N.sub.2, H.sub.2 and CO here. Also, the non-condensable gas is joined with the CO.sub.2 and H.sub.2S gas 29 separated by the separation drum 27.

(24) FIG. 2 is a schematic diagram in which an example of a temperature condition of the recovery system of the gas containing CO.sub.2 and H.sub.2S according to the first example is added. In FIG. 2, a square frame indicates the temperature.

(25) As illustrated in FIG. 2, in a recovery system 10A of the gas containing CO.sub.2 and H.sub.2S, the introduction gas 11 is introduced into the absorber 13. The absorbent 12 (lean solution 12B) is introduced into the absorber so as to face it and absorbs CO.sub.2 and H.sub.2S.

(26) Since the absorption is an exothermic reaction, the semi-rich solution 12C extracted from the vicinity of the middle stage 13b of the absorber 13 is 46° C. Meanwhile, the rich solution 12A extracted from the bottom portion 13c is 44° C.

(27) The rich solution 12A is introduced from the top portion 14a of the regenerator 14 as it is, while keeping a temperature of 44° C., without the heat exchange.

(28) In contrast, the semi-rich solution 12C is heat-exchanged with the high-temperature (123° C.) lean solution 12B in the semi-rich solution heat exchanger 17, and the semi-rich solution 12C becomes 113° C. and is introduced from the vicinity of the middle stage 14b of the regenerator 14. In addition, the temperature of the CO.sub.2 and H.sub.2S gas 25 accompanied by the water vapor from the top portion 14a of the regenerator 14 is 116° C., and the temperature thereof after passing through the condenser 26 is 40° C.

(29) Thus, a reduction in the reboiler heating capacity of the reboiler 15 in the regenerator 14 is achieved.

(30) FIG. 3 is a gas recovery system of the related art (Patent Literature 2).

(31) As illustrated in FIG. 3, in a recovery system 100 of the gas containing CO.sub.2 and H.sub.2S, the rich solution 12A extracted from the bottom portion 13c of the absorber 13 is adapted to be introduced from the top portion 14a side of the regenerator 14 after heat-exchange in a rich solution heat exchanger 16.

(32) Here, in the recovery system 100 of the gas containing CO.sub.2 and H.sub.2S illustrated in FIG. 3, the introduction gas 11 is introduced into the absorber 13. The absorbent 12 (lean solution 12B) is introduced into the absorber so as to face the introduction gas 11, and absorbs CO.sub.2 and H.sub.2S.

(33) Since this absorption is an exothermic reaction, the semi-rich solution 12C extracted from the vicinity of the middle stage 13b of the absorber 13 is 49° C. Meanwhile, the rich solution 12A extracted from the bottom portion 13c is 44° C.

(34) The rich solution 12A and the semi-rich solution 12C are heat-exchanged in series in the rich solution heat exchanger 16 and the semi-rich solution heat exchanger 17 by the high-temperature (122° C.) lean solution 12B, respectively, and the rich solution 12A becomes 77° C. and is introduced from the top portion 14a of the regenerator 14. Also, the semi-rich solution 12C becomes 104° C. and is introduced from the vicinity of the middle stage 14b of the regenerator 14. The temperature of CO.sub.2 and H.sub.2S gas 25 accompanied by water vapor from the top portion 14a of the regenerator 14 is 118° C., and the temperature thereof after passing through the condenser 26 is 40° C.

(35) Table 1 is a comparison of the load of the reboiler 15 of each regenerator, the load of the rich solution heat exchanger 16, the load of the semi-rich solution heat exchanger 17 and the load of the condenser 26, in the recovery system of the example and the gas recovery system of first and second conventional examples.

(36) In the first conventional example (Patent Literature 2), the rich solution 12A and the semi-rich solution 12C are heat-exchanged with the lean solution 12B in the rich solution heat exchanger 16 and the semi-rich solution heat exchanger 17.

(37) In the second conventional example, the rich solution 12A is heat-exchanged with the lean solution 12B in the rich solution heat exchanger 16.

(38) TABLE-US-00001 TABLE 1 First Second Present Conventional Conventional Load Example Example Example Rebolier 1.09 1 1.33 (15) Heat — 1 1.94 exchanger (16) Heat 1 1 — exchanger (17) Cooler 0.67 1 1.18 (26)

(39) As illustrated in Table 1, in the recovery system of this example, it was possible to reduce the reboiler load as compared to the second conventional example.

(40) Also, it was possible to significantly suppress the load of the condenser 26 which cools the CO.sub.2 and H.sub.2S gas 25 accompanied by the water vapor discharged from the regenerator 14 compared to the first and second conventional examples.

(41) Also, it was possible to reduce the cost and improve the heat balance of the overall process reduce, by eliminating the heat exchanger from the first conventional example.

REFERENCE SIGNS LIST

(42) 10, 10A, 100 RECOVERY SYSTEM OF GAS CONTAINING CO.sub.2 AND H.sub.2S

(43) 11 INTRODUCTION GAS

(44) 12 ABSORBENT

(45) 12A RICH SOLUTION

(46) 12B LEAN SOLUTION

(47) 12C SEMI-RICH SOLUTION

(48) 13 ABSORBER

(49) 14 ABSORBENT REGENERATOR (REGENERATOR)

(50) 15 REBOILER

(51) 17 SEMI-RICH SOLUTION HEAT EXCHANGER