Patent Application
20220193601
The present invention relates to an absorbent for carbon dioxide (CO2) or hydrogen sulfide (H2S), or both of CO2 and H2S, and a device and a method for removing CO2 or H2S, or both of CO2 and H2S, and particularly relates to an absorbent for CO2 in a flue gas, and a CO2 recovery unit and method.
As a method for recovering and removing an acid gas contained in a gas (gas to be treated) including a natural gas, various industrial gases produced at chemical plants such as a synthetic gas, a flue gas, or the like, especially CO2, various methods have been conventionally proposed. Examples of such methods include a method in which CO2 and H2S in a flue gas are brought into contact with an alkanolamine aqueous solution as an absorbent, removed, and recovered.
For example, such an absorbent is an absorbent of monoethanolamine (MEA) that is a primary monoamine of alkanolamine. By oxygen and the like in the flue gas, degradation of the absorbent by itself advances. As a countermeasure for this, an absorbent obtained by blending a secondary cyclic diamine or a predetermined primary monoamine having high steric hindrance with a novel secondary monoamine has been known (for example, Patent Literature 1). An absorbent obtained by adding a tertiary monoamine to a mixture of a secondary monoamine and a secondary cyclic diamine has been also known (for example, Patent Literature 2 and Patent Literature 3). Furthermore, an absorbent obtained by mixing predetermined primary, secondary, and tertiary monoamines having high steric hindrance has been known (for example, Patent Literature 4). Furthermore, an absorbent obtained by mixing a secondary monoamine, a secondary cyclic diamine, and a tertiary monoamine has been known (for example, Patent Literature 5).
Patent Literature 1: Japanese Patent No. 5215595
Patent Literature 2: Japanese Patent No. 4634384
Patent Literature 3: Japanese Patent Application Laid-open No. 2013-086079
Patent Literature 4: Japanese Patent Application Laid-open No. 2008-168227
Patent Literature 5: Japanese Patent Application Laid-open No. 2017-64645
However, in terms of components of the absorbents disclosed in Patent Literature 1 to Patent Literature 5, and mixing ratios thereof, a problem arises in which a large amount of heat is required for a reboiler during recirculation of the absorbents.
In view of the circumstances, an object of the present invention is to provide an absorbent for CO2 or H2S, or both of CO2 and H2S that can reduce a reboiler duty during recirculation of the absorbent, and device and method for removing CO2 or H2S, or both of CO2 and H2S.
According to a first aspect of the present invention, an absorbent is for absorbing CO2 or H2S, or both of CO2 and H2S in a gas. The absorbent includes, as components, (a) a secondary linear monoamine; (b) a tertiary linear monoamine; and (c) a secondary cyclic diamine. A concentration of the secondary linear monoamine (a) is more than 30% by weight and less than 45% by weight. A concentration of the tertiary linear monoamine (b) is more than 15% by weight and less than 30% by weight.
According to a second aspect of the present invention, a device is for removing CO2 or H2S, or both of CO2 and H2S. The device includes an absorber that brings a gas containing CO2 or H2S, or both of CO2 and H2S into contact with an absorbent to remove CO2 or H2S, or both of CO2 and H2S; and an absorbent regenerator that regenerates a solution in which CO2 or H2S, or both of CO2 and H2S are adsorbed. The solution regenerated by removing CO2 or H2S, or both of CO2 and H2S in the absorbent regenerator is reused in the absorber. The absorbent used in the device uses the absorbent according to the first aspect.
According to a third aspect of the present invention, a method is for removing CO2 or H2S, or both of CO2 and H2S. The method includes: bringing a gas containing CO2 or H2S, or both of CO2 and H2S into contact with an absorbent to remove CO2 or H2S, or both of CO2 and H2S in an absorber; regenerating a solution in which CO2 or H2S, or both of CO2 and H2S are absorbed in an absorbent regenerator; and reusing the solution regenerated by removing CO2 or H2S, or both of CO2 and H2S in the absorbent regenerator in the absorber. The absorbent used to remove CO2 or H2S, or both of CO2 and H2S is the absorbent according to the first aspect.
The present invention can provide an absorbent for absorbing CO2 or H2S, or both of CO2 and H2S in a gas, the absorbent containing, as components, (a) a secondary linear monoamine, (b) a tertiary linear monoamine, and (c) a secondary cyclic diamine, wherein when the concentration of the secondary linear monoamine (a) is more than 30% by weight and less than 45% by weight and the concentration of the tertiary linear monoamine (b) is more than 15% by weight and less than 30% by weight, a reboiler duty during recirculation of the absorbent can be reduced, and device and method for removing CO2 or H2S, or both of CO2 and H2S.
Hereinafter, preferred examples of the present invention will be described in detail with reference to the accompanying drawings. The present invention is not limited by the examples. When there are a plurality of examples, the present invention includes a combination of the examples.
An absorbent according to an example of the present invention is an absorbent for absorbing CO2 or H2S, or both of CO2 and H2S in a gas. The absorbent contains, as components, (a) a secondary linear monoamine, (b) a tertiary linear monoamine, and (c) a secondary cyclic diamine. The concentration of the secondary linear monoamine (a) is more than 30% by weight and less than 45% by weight, and the concentration of the tertiary linear monoamine (b) is more than 15% by weight and less than 30% by weight.
Herein, it is preferable that the concentration in % by weight of the secondary cyclic diamine (c) relative to the absorbent be lower than the concentration of the secondary linear monoamine (a), and be lower than the concentration of the tertiary linear monoamine (b).
The total concentration of the secondary linear monoamine (a), the tertiary linear monoamine (b), and the secondary cyclic diamine (c) is preferably more than 46% by weight and 75% by weight or less.
The total concentration of the components (a) to (c) that suitably falls within a range of 50% by weight to 70% by weight, and further suitably falls within a range of 55% by weight to 65% by weight is preferable. This is because the reboiler duty can be reduced during recirculation of the absorbent even when the concentration is high.
The lower limit of the concentration of the secondary cyclic diamine (c) is preferably 1% by weight or more, and more preferably 3% by weight or more.
Thus, when the concentrations of the secondary linear monoamine (a), the tertiary linear monoamine (b), and the secondary cyclic diamine (c) fall within the aforementioned ranges, the CO2 absorption capacity of the absorbent can be retained due to excellent CO2 absorbability of the secondary linear monoamine (a) and the secondary cyclic diamine (c), and the CO2 desorption capacity of the absorbent can be improved due to excellent CO2 releasability of the secondary linear monoamine (a) and the tertiary linear monoamine (b). Therefore, even when the concentration of agent of the absorbent is high, the reboiler duty during regeneration of the absorbent in which CO2 has been absorbed can be reduced.
The secondary linear monoamine (a) is preferably a compound represented by a chemical formula (I), which is represented in “Formula 1” below.
Specific examples of the secondary linear monoamine (a) include a compound selected from at least one of N-methylaminoethanol, N-ethylaminoethanol, N-propylaminoethanol, N-butylaminoethanol, and the like, but the present invention is not limited to the specific examples. The compounds may be combined.
The tertiary linear monoamine (b) is preferably a compound represented by a chemical formula (II), which is represented in “Formula 2” below.
Specific examples of the tertiary linear monoamine (b) include a compound selected from at least one of N-methyldiethanolamine, N-ethyldiethanolamine, N-butyldiethanolamine, 4-dimethylamino-1-butanol, 2-dimethylaminoethanol, 2-diethylaminoethanol, 2-di-n-butylaminoethanol, N-ethyl-N-methylethanolamine, 3-dimethylamino-1-propanol, 2-dimethylamino-2-methyl-1-propanol, and the like, but the present invention is not limited to the specific examples. The compounds may be combined.
The secondary cyclic diamine (c) is a piperazine derivative. Examples of such a piperazine derivative include a compound such as piperazine (C4H10N2), 2-methylpiperazine (C5H12N2), and 2,5-dimethylpiperazine (C6H14N2), or a mixture thereof.
The secondary linear monoamine (a) that is a component constituting an absorption component in the present invention has general characteristics in which by a reaction with CO2 in a flue gas, a carbamate containing an amine as the absorption component in the molecule is produced, and CO2 is fixed. Therefore, the secondary linear monoamine (a) has high absorption capacity.
However, under a high concentration condition, it is necessary to prevent deterioration in the absorption rate and absorption performance due to increased viscosity of the absorbent, and to prevent deterioration in regeneration performance.
Meanwhile, in the tertiary linear monoamine (b) that is another component of the present invention, CO2 is mainly dissolved as a bicarbonate salt without producing a carbamate by a reaction with CO2. Therefore, the absorption performance of the tertiary linear monoamine (b) is inferior to the absorption performance of the secondary linear monoamine (a). Even under a high concentration condition, an increase in viscosity of the absorbent can be comparatively moderated. The tertiary linear monoamine (b) has excellent regeneration performance.
Based on the aforementioned properties of both the components constituting the absorbent, a composition of components of the absorption component that suppresses an increase in viscosity of the absorbent, retains absorption performance even under a high concentration condition of the absorption component, and prevents a reduction in regeneration performance to reduce the reboiler duty has been intensively studied. In the present invention, it has been found that as a composition of the absorption component in which the concentration of the tertiary linear monoamine (b) is set within a relatively high and suitable range even under a composition condition where the concentration of the secondary linear monoamine (a) is high, the composition contains, as components, the secondary linear monoamine (a), the tertiary linear monoamine (b), and the secondary cyclic diamine (c), that the concentration of the secondary linear monoamine (a) is set within a range of more than 30% by weight and less than 45% by weight, and that the concentration of the tertiary linear monoamine (b) is set within a range of more than 15% by weight and less than 30% by weight.
Herein, for measurement of increased viscosity of the absorbent, the viscosity (A) when a regenerated CO2 absorbent (lean solution), of the absorbent that is circulated and reused in a CO2 absorber for removing CO2 in a flue gas and an absorbent regenerator that releases absorbed CO2, is supplied to the CO2 absorber, and the viscosity (B) of an CO2 absorbent (rich solution) in which CO2 has been absorbed at a CO2 recovery portion of the CO2 absorber are measured. Under mixing of the present invention as presented in Test Examples described below, it is confirmed that an increase in viscosity of the absorbent is suppressed.
Furthermore, it is preferable that the mixing ratio of the components (components a, b, and c) be defined so that the weight ratio of the tertiary linear monoamine (b) to the total weight of the secondary linear monoamine (a) and the secondary cyclic diamine (c) is more than 0.3 and less than 0.85.
When it is thus defined, an absorbent containing, as components of the absorption component, the secondary linear monoamine (a) and the tertiary linear monoamine (b) at high concentrations and having excellent saving energy due to a suitable weight ratio “(b) tertiary linear monoamine/((a) secondary linear monoamine +(c) secondary cyclic diamine)” can be provided.
It is preferable that the mixing ratio of the components (components a and b) be defined so that the weight ratio of the tertiary linear monoamine (b) to the secondary linear monoamine (a) is more than 0.5 and less than 1.0.
When it is thus defined, an absorbent containing, as the component of the absorption component, the tertiary linear monoamine (b) at a high concentration and having excellent saving energy due to a suitable weight ratio “(b) tertiary linear monoamine/(a) secondary linear monoamine” can be provided.
In the present invention, for example, it is preferable that the absorption temperature of the absorber for a chemical absorption method during contact with a flue gas containing CO2 or the like generally fall within a range of 30 to 80° C. To the absorbent used in the present invention, a corrosion inhibitor, a degradation inhibitor, or the like is added, if necessary.
It is preferable that the CO2 partial pressure at an inlet of a CO2 absorber during absorption in which CO2 in a gas to be treated is adsorbed be low CO2 partial pressure (for example, 0.003 to 0.1 MPa) in terms of application of the chemical absorption method.
In the present invention, when the pressure of the absorbent regenerator that releases CO2 or the like from the absorbent in which CO2 or the like has been absorbed is 130 to 200 kPa (absolute pressure), it is preferable that the regenerator bottom temperature of the absorbent regenerator that is the regeneration temperature of the regenerator be 110° C. or higher. This is because it is necessary to increase the amount of absorbent circulated in a system during regeneration at lower than 110° C., and the regeneration is not preferred in terms of regeneration efficiency. Regeneration at 115° C. or higher is more preferred.
Examples of a gas to be treated in the present invention include, but not limited to, a coal gasified gas, a synthesis gas, a coke-oven gas, a petroleum gas, a natural gas, a flue gas, and the like. Any gas may be used as long as it contains a gas containing an acid gas such as CO2 or H2S.
A process that can be employed in a method for removing CO2 or H2S, or both of CO2 and H2S in a gas of the present invention is not particularly limited, and an example of a removal device that removes CO2 will be described with reference to
In
In a method for recovering CO2 using this CO2 recovery unit 12, the flue gas 14 containing CO2 from the industrial combustion facility 13 such as a boiler or a gas turbine is pressurized by a flue gas blower 22, sent to the flue gas cooling device 16, cooled in the flue gas cooling device 16 using the cooling water 15, and sent to the CO2 absorber 18.
In the CO2 absorber 18, the flue gas 14 comes into countercurrent contact with the CO2 absorbent 17 that is an amine absorbent according to this example, and CO2 in the flue gas 14 is absorbed into the CO2 absorbent 17 by a chemical reaction. A CO2-removed flue gas in which CO2 has been removed in the CO2 recovery portion 18A comes into gas-liquid contact with circulating cleaning water 21 containing a CO2 absorbent that is supplied from a liquid distributor in a water-cleaning portion 18B in the CO2 absorber 18, the CO2 absorbent 17 entrained with the CO2-removed flue gas is recovered, and a flue gas 23 in which CO2 has been removed is then discharged outside the system. The rich solution 19 that is the CO2 absorbent in which CO2 has been absorbed is pressurized by a rich solution pump 24, heated using the lean solution that is the CO2 absorbent 17 regenerated in the absorbent regenerator 20 in a rich-lean solution heat exchanger 25, and supplied to the absorbent regenerator 20.
The rich solution 19 released from an upper portion of the absorbent regenerator 20 to the inside thereof causes an endothermic reaction using steam that is supplied from the bottom portion, and most of CO2 is released. The CO2 absorbent in which a part or most of CO2 has been released in the absorbent regenerator 20 is referred to as a semi-lean solution. This semi-lean solution becomes the CO2 absorbent (lean solution) 17 in which almost all of CO2 has been removed when the solution reaches the bottom portion of the absorbent regenerator 20. A part of this lean solution 17 is overheated by steam 27 in a reboiler 26, and steam for CO2 desorption is supplied to the inside of the absorbent regenerator 20.
On the other hand, from the top portion of the absorbent regenerator 20, a CO2 entraining gas 28 with steam released from the rich solution 19 and the semi-lean solution in the regenerator is delivered, the water vapor is condensed by a condenser 29, water is separated in a separation drum 30, and a CO2 gas 40 is released outside the system, compressed by a separate compressor 41, and recovered. A CO2 gas 42 that has been compressed and recovered passes through a separation drum 43, and is injected into an oilfield using enhanced oil recovery (EOR), or stored in an aquifer. Thus, a global warming countermeasure is made. Reflux water 31 separated and refluxed from the CO2 accompanying gas 28 with water vapor in the separation drum 30 is supplied to the upper portion of the absorbent regenerator 20 by a reflux water circulation pump 35 and a cleaning water 21 side. The regenerated CO2 absorbent (lean solution) 17 is cooled using the rich solution 19 in the rich-lean solution heat exchanger 25, then pressurized by a lean solution pump 32, cooled using a lean solution cooler 33, and then supplied to the inside of the CO2 absorber 18. In this embodiment, the outline thereof is only described, and some of accompanying devices are omitted.
Hereinafter, preferred test examples exhibiting the effects of the present invention will be described, but the present invention is not limited to the test examples.
CO2 was absorbed using an absorption test device not illustrated.
N-butylaminoethanol (more than 30% by weight and less than 45% by weight) as the secondary linear monoamine (a), N-methyldiethanolamine (more than 15% by weight and less than 30% by weight) as the tertiary linear monoamine (b), and 2-methylpiperazine (a concentration lower than those of (a) and (b)) as the secondary cyclic diamine (c) were dissolved and mixed in water, to prepare the absorbent of Test Example 1-1 so that the total amine component concentration of an absorption component was 55% by weight.
The absorbent of Test Example 1-2 was prepared in the same manner as in Test Example 1-1 except for using piperazine as the secondary cyclic diamine (c).
The absorbent of Test Example 1-3 was prepared in the same manner as in Test Example 1-1 except for using N-butyldiethanolamine as the tertiary linear monoamine (b).
The absorbent of Test Example 1-4 was prepared in the same manner as in Test Example 1-1 except for using N-ethylaminoethanol as the secondary linear monoamine (a) and piperazine as the secondary cyclic diamine (c).
The absorbent of Test Example 1-5 was prepared in the same manner as in Test Example 1-4 except for using N-ethyldiethanolamine as the tertiary linear monoamine (b).
In Comparative Example, monoethanolamine (MEA) was dissolved and mixed in water at 30% by weight, to prepare an absorbent of Comparative Example 1. Component compositions of Test Examples and Comparative Example are listed in Table 1 below.
<Evaluation of Reboiler Duty Ratio>
The reboiler duties when the absorbents of Test Examples and Comparative Example were used were measured. The reboiler duty in each of Test Examples was compared with the reboiler duty when the absorbent of Comparative Example was used, and was evaluated as a reboiler duty ratio. The evaluation results are illustrated in
As illustrated in
The total amine component concentration of an absorption component of the absorbent of each of Test Examples 1-1 to 1-5 was increased from 55% by weight to 65% by weight. Thus, absorbents of Test Examples 2-1 to 2-5 were prepared. Component compositions of Test Examples 2-1 to 2-5 are listed in Table 2 below. Comparative Example 1 is the same as listed in Table 1, and the mixing formulation is omitted. The evaluation results evaluated in the same manner as in Test Example 1-1 are illustrated in
As illustrated in
Therefore, it is found that the absorbents of Test Examples 1-1 to 1-5 and 2-1 to 2-2 that are the three-component-based absorbents (the secondary linear monoamine (a), the tertiary linear monoamine (b), and the secondary cyclic diamine (c) are dissolved in water) can reduce the reboiler duty as compared with Comparative Example 1 using monoethanolamine. In particular, it is found that the absorbents of Test Examples 1-1, 1-2, 2-1, and 2-2 can reduce the reboiler duty by 10% or more.
Accordingly, even when the concentration of an absorbent is high, an absorbent having excellent saving energy as compared with a conventional absorbent can be provided, and a reduction in reboiler duty during regeneration of an absorbent in which CO2 or H2S, or both of CO2 and H2S in a gas have been absorbed can be attained.
In Test Example 1-6, the absorbent of the composition of Test Example 1-1 was used, the concentration of N-butylaminoethanol as the secondary linear monoamine (a) was fixed to 32% by weight, and the component concentration of N-methyldiethanolamine as the tertiary linear monoamine (b) was changed. Thus, an absorbent of Test Example 1-6 was prepared. An absorbent of Comparative Example was the same as the absorbent prepared by dissolving and mixing the aforementioned monoethanolamine (MEA) at 30% by weight in water. A component composition of this Test Example is listed in Table 3 below. The result is illustrated in
As illustrated
As an absorbent of Test Example 3, the absorbent of the composition of Test Example 1-2 described above was used. The absorbent of Test Example 3 was subjected to a comparison test with the conventional art (Comparative Examples 2 and 3) under a concentration where the total amine component concentration (% by weight) of an absorption component was high.
Here, in Comparative Example 2, a mixing composition of Test Example 6 of Japanese Patent Application Laid-open No. 2013-086079 was adapted, and in Comparative Example 3, a mixing composition of Test Example 1-2 of Japanese Patent Application Laid-open No. 2017-64645 was adapted. The mixing composition is listed in Table 3.
Here, the concentrations in Test Example 3 and Comparative Examples 2 and 3 were adjusted as described below.
In each example under a condition where the total amine concentration of the absorption component is 55% by weight, the concentration of the secondary linear monoamine (a) is represented by A55% by weight, the concentration of the tertiary linear monoamine (b) is represented by B55% by weight, and the concentration of the secondary cyclic diamine (c) is represented by C55% by weight. In each example under a condition where the total amine concentration of the absorption component is changed to T % by weight, the concentration of the secondary linear monoamine (a) is represented by AT% by weight, the concentration of the tertiary linear monoamine (b) is represented by BT% by weight, and the concentration of the secondary cyclic diamine (c) is represented by CT% by weight. In each example, the mixing ratio of the components A55:B55:C55=AT:BT:CT is fixed. The concentration (% by weight) of each component under a condition where the total amine concentration of the absorption component is T % by weight is calculated for each composition as listed in Table 5 below.
As illustrated in
As an absorbent of Test Example 4, the absorbent of the composition of Test Example 1-2 was used. The absorbent of Test Example 4 was subjected to a comparison test of changed viscosity of the absorbent with the conventional art (Comparative Examples 2 and 3) under a concentration where the total amine component concentration (% by weight) of an absorption component was high.
In Comparative Example 2, a mixing composition of Test Example 6 of Japanese Patent Application Laid-open No. 2013-086079 was adapted, and in Comparative Example 3, a mixing composition of Test Example 1-2 of Japanese Patent Application Laid-open No. 2017-64645 was adapted.
In measurement of viscosity of the absorption component, the viscosity (A) of the absorbent before introduction into the CO2 absorber 18 of the CO2 recovery unit 12 in
The mixing ratio of components of the absorption component of Test Example 4 was the fixed total amine component concentration of the absorption component of Test Example 1-2 listed in Table 1 (55% by weight). The mixing ratio of components of the absorption component of Test Example 5 was the fixed total amine component concentration of the absorption component of Test Example 2-2 (65% by weight). A viscosity standard was based on a value (viscosity A) measured at the position (A) where the absorbent was supplied to the CO2 absorber 18 in Test Example 3, which was considered to be 1 as a standard. The results are listed in Tables 6 and 7.
The absorbents of the compositions of Test Examples 4 and 5 were compared with Comparative Examples 2 and 3 as the conventional art, as listed in Tables 6 and 7. It is found that an increase in viscosity of the absorbents is suppressed even under a condition where the concentration of the absorption component is high.
In Test Example 6, the absorbent of the composition of Test Example 1-1 was used, the concentration of N-butylaminoethanol as the secondary linear monoamine (a) was fixed to 32% by weight, and the component ratio by weight of N-methyldiethanolamine as the tertiary linear monoamine (b) ((tertiary linear monoamine (b)/(secondary linear monoamine (a) +secondary cyclic diamine (c)) was changed. Thus, an absorbent of Test Example 6 was prepared.
In Comparative Example, an absorbent was prepared by dissolving and mixing the aforementioned monoethanolamine (MEA) at 30% by weight in water. A component composition of this Test Example is listed in Table 8 below. The results are illustrated in
As illustrated
In Test Example 6, the absorbent of the composition of Test Example 1-1 was used, the concentration of N-butylaminoethanol as the secondary linear monoamine (a) was fixed to 32% by weight, and the component ratio by weight of N-methyldiethanolamine as the tertiary linear monoamine (b) ((tertiary linear monoamine (b)/secondary linear monoamine (a)) was changed. Thus, an absorbent of Test Example 5 was prepared.
In Comparative Example, an absorbent was prepared by dissolving and mixing the aforementioned monoethanolamine (MEA) at 30% by weight in water. A component composition of this Test Example is the same as those in Table 7. The results are illustrated in
As illustrated
A combination of the secondary linear monoamine (a), the tertiary linear monoamine (b), and the secondary cyclic diamine (c) of the present invention is not limited to a combination in which an effect is demonstrated in this Test Example. As a suitable combination other than Test Examples of the preferred combinations, an example is listed in Tables 9 to 12.
Table 9 is an example of preferred combinations in which N-methylaminoethanol is used as the secondary linear monoamine (a).
Table 10 is an example of preferred combinations in which N-ethylaminoethanol is used as the secondary linear monoamine (a).
Table 11 is an example of preferred combinations in which N-propylaminoethanol is used as the secondary linear monoamine (a).
Table 12 is an example of preferred combinations in which N-butylaminoethanol is used as the secondary linear monoamine (a).
12 CO2 recovery unit
13 Industrial combustion facility
14 Flue gas
16 Flue gas cooling device
17 CO2 absorbent (lean solution)
18 CO2 absorber
19 CO2 absorbent containing absorbed CO2 (rich solution)
20 Absorbent regenerator
21 Cleaning water
| Number | Date | Country | Kind |
|---|---|---|---|
| 2019-076616 | Apr 2019 | JP | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2020/007613 | 2/26/2020 | WO | 00 |
