CN220779633U - System for selectively absorbing and separating CO2 gas from mixed gas rich in CO2 - Google Patents
System for selectively absorbing and separating CO2 gas from mixed gas rich in CO2 Download PDFInfo
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- CN220779633U CN220779633U CN202322337698.3U CN202322337698U CN220779633U CN 220779633 U CN220779633 U CN 220779633U CN 202322337698 U CN202322337698 U CN 202322337698U CN 220779633 U CN220779633 U CN 220779633U
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- absorbent
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- 239000002250 absorbent Substances 0.000 claims abstract description 109
- 230000002745 absorbent Effects 0.000 claims abstract description 109
- 238000010521 absorption reaction Methods 0.000 claims abstract description 91
- 238000003795 desorption Methods 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims description 73
- 238000012546 transfer Methods 0.000 claims description 9
- 239000006096 absorbing agent Substances 0.000 claims description 7
- 238000000034 method Methods 0.000 abstract description 15
- 230000008901 benefit Effects 0.000 abstract description 7
- 230000008929 regeneration Effects 0.000 abstract description 4
- 238000011069 regeneration method Methods 0.000 abstract description 4
- 239000002131 composite material Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 7
- -1 dialkyl ether compounds Chemical class 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- HXKKHQJGJAFBHI-UHFFFAOYSA-N 1-aminopropan-2-ol Chemical group CC(O)CN HXKKHQJGJAFBHI-UHFFFAOYSA-N 0.000 description 1
- GIAFURWZWWWBQT-UHFFFAOYSA-N 2-(2-aminoethoxy)ethanol Chemical compound NCCOCCO GIAFURWZWWWBQT-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229940102253 isopropanolamine Drugs 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The utility model relates to the technical field of gas separation, in particular to a method for separating CO from CO-enriched gas 2 Selective absorption separation of CO from a mixed gas of (C) 2 The system of the gas consists of an absorption tower, a phase separator and a desorption tower; the lower part of the absorption tower is provided with a mixed gas inlet, the upper part is provided with an absorbent inlet, and the top part is provided with a purified gas outletThe mouth, the bottom is provided with an absorbent outlet, and the middle upper part is provided with a lean CO 2 An absorbent phase inlet; the middle part of the phase separator is provided with an absorbent inlet, and the upper part is provided with a lean CO 2 An absorbent phase outlet, the bottom of which is provided with a CO-rich part 2 An absorbent phase outlet; the middle part of the desorption tower is provided with rich CO 2 An absorbent phase inlet with CO at the top 2 A gas outlet, the bottom of which is provided with an absorbent outlet; the utility model can reduce CO 2 Equipment and operation cost required by regeneration can well absorb and separate CO from mixed gas 2 The method has the advantages of high absorption rate, large absorption capacity, good selectivity, high economic benefit, high practicability and easy popularization and use.
Description
Technical Field
The utility model belongs to the technical field of gas separation, in particular to a method for separating CO from CO-enriched gas 2 Selective absorption separation of CO from a mixed gas of (C) 2 A system of gases.
Background
In recent years, a series of environmental problems caused by the greenhouse effect have attracted worldwide attention, in which CO 2 The contribution to global warming exceeds 60%. In 2020, china discharges CO 2 About 102 billions of tons, accounting for 27% of the global emissions, are the first place in the world. Chinese CO 2 The emissions strive to peak before 2030 and strive to achieve carbon neutralization before 2060. China CO 2 The main source of emission is the industries of thermal power, petroleum and natural gas, and occupies more than 70 percent of the whole carbon emission, and CO suitable for the industries of thermal power, petroleum and natural gas is developed 2 The absorbent and the absorption process solve the problem of CO in China 2 Emission problems, the most effective approach to achieve the "two carbon" goal.
CO 2 The capturing method is classified according to the separation principle, and can be broadly classified into a solvent absorption method, an adsorption separation method, a membrane separation method, and a low temperature distillation method. Numerous COs 2 Among the trapping separation methods, the solvent absorption method is the most widely used and most established at presentCooked CO 2 Trapping method, CO 2 Is a decarburization technique most likely to be industrialized recently. According to CO 2 The different mechanisms of action of the absorption solvent can be classified into chemical absorption and physical absorption. Chemical absorption method for low partial pressure CO 2 The gas absorption effect is good, the reaction is stable, but the energy consumption in the analysis process is larger; the physical absorption method has the advantages of large absorption capacity, easy desorption, easy solvent regeneration, small equipment corrosion and the like, and is the choice with high feasibility and good economic benefit at present.
Existing selective absorption separation of CO from mixed gas 2 The systems for gases are directed to separate chemical and physical absorbents, and as the advantages of composite absorbents begin to stand out, efforts have been directed to the use of composite absorbents from being rich in CO 2 Selective absorption separation of CO from a mixed gas of (C) 2 A system of gases.
Disclosure of Invention
In order to solve the problems in the prior art, the utility model aims to provide a method for preparing a catalyst rich in CO 2 Selective absorption separation of CO from a mixed gas of (C) 2 A system for gas, the system being adapted to selectively absorb and separate CO from a mixed gas using a composite absorbent of a chemical absorbent and a physical absorbent 2 With CO 2 High absorption rate, large absorption capacity and the like.
The utility model is realized by the following scheme:
from being rich in CO 2 Selective absorption separation of CO from a mixed gas of (C) 2 The system of the gas consists of an absorption tower, a phase separator and a desorption tower;
the lower part of the absorption tower is provided with a mixed gas inlet, the upper part of the absorption tower is provided with an absorbent inlet, the top of the absorption tower is provided with a purified gas outlet, the bottom of the absorption tower is provided with an absorbent outlet, and the middle upper part of the absorption tower is provided with a lean CO 2 An absorbent phase inlet;
the middle part of the phase separator is provided with an absorbent inlet, and the upper part of the phase separator is provided withLean CO 2 The bottom of the phase separator is provided with a CO-rich outlet 2 An absorbent phase outlet;
the middle part of the desorption tower is provided with a CO-rich gas 2 An absorbent phase inlet, the top of the desorption tower is provided with CO 2 A gas outlet, wherein an absorbent outlet is arranged at the bottom of the desorption tower;
the absorbent outlet of the absorption tower is connected with the absorbent inlet of the phase separator, and the phase separator is rich in CO 2 The absorbent phase outlet and the desorption tower are rich in CO 2 The absorbent phase inlet is connected, and the phase separator is lean in CO 2 Absorbent phase outlet and CO lean of the absorber column 2 The absorbent phase inlet is connected, and the absorbent outlet of the desorption tower is connected with the absorbent inlet of the absorption tower.
Preferably, a cooler is arranged on the gas pipeline in front of the mixed gas inlet of the absorption tower.
Preferably, the absorbent outlet of the absorber is connected to the absorbent inlet of the phase separator by a first transfer pump.
Preferably, the phase separator is rich in CO 2 The absorbent phase outlet is communicated with the CO-rich of the desorption tower through a second delivery pump 2 The absorbent phase inlet is connected.
Preferably, the absorbent outlet of the desorption column is connected to the absorbent inlet of the absorption column by a third transfer pump.
Compared with the prior art, the utility model has the following steps:
the system of the utility model can be well matched with a composite absorbent to carry out selective absorption and separation of CO 2 The absorbent is phase separated by a phase separator so that only CO is needed 2 The enrichment phase is regenerated, and CO regenerated via the enrichment phase 2 Has higher purity and can reduce CO 2 Equipment and operation cost required by regeneration can well absorb and separate CO from mixed gas 2 And the desorbed absorbent can be reused as CO 2 Recycling the absorbent; at the same time, the mixed gas and CO in the absorption tower 2 The physical absorbent is in countercurrent contact, so that the whole system is further guaranteed to be high in absorption rate, large in absorption capacity and good in selectivity, economic benefit is improved, practicability is high, and popularization and use are easy.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present utility model, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 shows the selective absorption separation of CO provided by the present utility model 2 A system flow diagram of the gas.
Reference numerals illustrate:
1. an absorption tower; 2. a desorption tower; 3. a phase separator; 4. a first transfer pump; 5. a second transfer pump; 6. a third transfer pump; 7. a cooler.
Detailed Description
The following description of the embodiments of the present utility model will be made apparent and fully in view of the accompanying drawings, in which some, but not all embodiments of the utility model are shown. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be noted that the directions or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
Referring to FIG. 1, the present embodiment provides a method for generating a CO-enriched stream 2 Selective absorption separation of CO from a mixed gas of (C) 2 The system of the gas consists of an absorption tower 1, a phase separator 3 and a desorption tower 2;
the lower part of the absorption tower 1 is provided with a mixed gas inlet, the upper part of the absorption tower 1 is provided with an absorbent inlet, the top of the absorption tower 1 is provided with a purified gas outlet, the bottom of the absorption tower 1 is provided with an absorbent outlet, and the middle upper part of the absorption tower 1 is provided with a lean CO 2 An absorbent phase inlet;
the middle part of the phase separator 3 is provided with an absorbent inlet, and the upper part of the phase separator 3 is provided with a lean CO 2 The bottom of the absorber phase outlet and the phase separator 3 is provided with a CO-rich phase outlet 2 An absorbent phase outlet;
the middle part of the desorption tower 2 is provided with a CO-rich part 2 An absorbent phase inlet, the top of the desorption tower 2 is provided with CO 2 A gas outlet, wherein an absorbent outlet is arranged at the bottom of the desorption tower 2;
the absorbent outlet of the absorber 1 is connected with the absorbent inlet of the phase separator 3, and the phase separator 3 is rich in CO 2 The absorbent phase outlet and the desorption tower 2 are rich in CO 2 The absorbent phase inlet is connected, and the phase separator 3 is lean in CO 2 The absorbent phase outlet is CO lean with the absorber 1 2 The absorbent phase inlet is connected, and the absorbent outlet of the desorption tower 2 is connected with the absorbent inlet of the absorption tower 1.
The embodiment also comprises a cooler 7, wherein the cooler 7 is arranged on the gas pipeline in front of the mixed gas inlet of the absorption tower 1 and is used for enriching CO 2 Is cooled by the mixed gas of the (2) and is convenient for CO in the mixed gas 2 The gas is better absorbed in the absorber 1.
The embodiment further comprises a first delivery pump 4, wherein the absorbent outlet of the absorption tower 1 is connected with the absorbent inlet of the phase separator 3 through the first delivery pump 4, and efficient delivery of absorbent is realized through the first delivery pump 4.
The present embodiment further comprises a second transfer pump 5, the phase separator 3 being rich in CO 2 The absorbent phase outlet is in rich CO with the desorber 2 through a second transfer pump 5 2 The absorbent phase inlet is connected, and the second delivery pump 5 is used for realizing CO enrichment 2 Efficient delivery of the absorbent.
The embodiment further comprises a third delivery pump 6, wherein the absorbent outlet of the desorption tower 2 is connected with the absorbent inlet of the absorption tower 1 through the third delivery pump 6, and the high-efficiency delivery of the desorbed absorbent is realized through the third delivery pump 6.
The specific working process of the utility model is as follows:
is rich in CO 2 The mixed gas of (2) is cooled by a cooler 7 and then enters from the lower part of the absorption tower 1, the composite absorbent enters from the upper part of the absorption tower 1, the two are in countercurrent contact in the absorption tower 1, and CO in the mixed gas 2 The gas is absorbed by the composite absorbent in the absorption tower 1, the decarbonized purified gas is discharged from the top of the absorption tower 1, and the purified gas contains CO 2 The absorbent is discharged from the bottom of the absorption tower 1; CO-containing discharged from the absorption tower 1 by the first transfer pump 4 2 The absorbent is sent to a phase separator 3 for phase separation, and the upper layer is lean in CO 2 The absorbent phase, the lower layer is rich in CO 2 Absorbent phase, upper CO lean layer 2 The absorbent can be directly circulated to the middle part of the absorption tower 1, or can be completely desorbed and then enter the absorption tower 1, and the lower layer is rich in CO 2 The absorbent directly enters a desorption tower 2 for desorption, the desorbed absorbent is recycled to an absorption tower 1 from the bottom of the desorption tower 2, and the desorbed high-purity CO is desorbed 2 The gas is discharged from the top of the desorption column 2.
In the embodiment, the composite absorbent entering the absorption tower 1 is selected from polyalkoxy dialkyl ether compounds and alcohol amine chemical absorbent; the polyalkoxy dialkyl ether compound is polymethoxy dimethyl ether (PODE) n ) The alcohol amine chemical absorbent is isopropanolamine and/or diglycolamine.
For a better understanding of the above-described embodiments of the present utility model, they are further described below with reference to specific examples.
The selective absorption separation of CO is shown below in connection with FIG. 1 2 The gas system flow diagram further illustrates the utility model for better understanding of the utility model, but is not intended to limit the scope of the utility model.
As shown in FIG. 1, the synthesis gas after water gas conversion is treated by desulfurization (e.g. using zinc oxide adsorbent) to be rich in CO 2 Is composed of CO 2 ：38.54％，CO：0.84％，CH 4 ：0.08％，H 2 ：56.86％，N 2 : 3.68%) is cooled by a cooler 7 and enters the lower part of the absorption tower 1 at a flow rate of 25000 kmol/h to be in countercurrent contact with the composite absorbent entering the upper part of the absorption tower 1. The operating temperature of the absorption tower 1 is 25 ℃ and the operating pressure is 3.05 MPa. CO in mixed gas 2 Is absorbed, purified gas is discharged from the top of the absorption tower 1 and is rich in CO 2 CO of (c) 2 The rich liquid is discharged from the bottom of the absorption tower 1.
CO discharged from the bottom of the absorption tower 1 2 The rich liquid is sent into the middle part of the phase separator 3 for phase separation by the first delivery pump 4. Upper CO lean layer 2 The absorbent can be directly circulated to the middle part of the absorption tower 1, or can be completely desorbed and then enter the absorption tower 1, and the lower layer is rich in CO 2 The absorbent is sent into a second delivery pump 5 to directly enter a desorption tower 2 for desorption, the operation temperature of the desorption tower 2 is 25 ℃, and the operation pressure is 0.15 MPa. The desorbed absorbent is recycled to the upper part of the absorption tower 1 from the bottom of the desorption tower 2 through a third delivery pump 6 and is used as absorbent for recycling, and the desorbed high-purity CO is recovered 2 The gas is discharged from the top of the desorption column 2.
Is rich in CO 2 Is the mixture gas of (i.e. the originalFeed gas, noted stream 1), purge gas (noted stream 2) and high purity CO 2 The specific flow rates and gas compositions of the gases (noted as stream 3) are shown in table 1.
TABLE 1 gas flow Rate and gas composition
As can be seen from the data in Table 1, the composite absorbent adopting the PODEn compound alcohol amine chemical solvent can well selectively absorb and separate CO from the mixed gas 2 。
The system of the utility model can be well matched with a composite absorbent to carry out selective absorption and separation of CO 2 The absorbent is phase separated by a phase separator 3 so that only CO is required 2 The enrichment phase is regenerated, and CO regenerated via the enrichment phase 2 Has higher purity and can reduce CO 2 Equipment and operation cost required by regeneration can well absorb and separate CO from mixed gas 2 And the desorbed absorbent can be reused as CO 2 Recycling the absorbent; at the same time, the mixed gas and CO in the absorption tower 1 2 The physical absorbent is in countercurrent contact, so that the whole system is further guaranteed to be high in absorption rate, large in absorption capacity and good in selectivity, economic benefit is improved, practicability is high, and popularization and use are easy.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (5)
1. From being rich in CO 2 Selective absorption separation of CO from a mixed gas of (C) 2 The system of the gas is characterized by comprising an absorption tower, a phase separator and a desorption tower;
the lower part of the absorption tower is provided with a mixed gas inlet, the upper part of the absorption tower is provided with an absorbent inlet, the top of the absorption tower is provided with a purified gas outlet, the bottom of the absorption tower is provided with an absorbent outlet, and the middle upper part of the absorption tower is provided with a lean CO 2 An absorbent phase inlet;
the middle part of the phase separator is provided with an absorbent inlet, and the upper part of the phase separator is provided with a lean CO 2 The bottom of the phase separator is provided with a CO-rich outlet 2 An absorbent phase outlet;
the middle part of the desorption tower is provided with a CO-rich gas 2 An absorbent phase inlet, the top of the desorption tower is provided with CO 2 A gas outlet, wherein an absorbent outlet is arranged at the bottom of the desorption tower;
the absorbent outlet of the absorption tower is connected with the absorbent inlet of the phase separator, and the phase separator is rich in CO 2 The absorbent phase outlet and the desorption tower are rich in CO 2 The absorbent phase inlet is connected, and the phase separator is lean in CO 2 Absorbent phase outlet and CO lean of the absorber column 2 The absorbent phase inlet is connected, and the absorbent outlet of the desorption tower is connected with the absorbent inlet of the absorption tower.
2. The CO-enriched slave according to claim 1 2 Selective absorption separation of CO from a mixed gas of (C) 2 The gas system is characterized in that a cooler is arranged on a gas pipeline in front of a mixed gas inlet of the absorption tower.
3. The CO-enriched slave according to claim 1 2 Selective absorption separation of CO from a mixed gas of (C) 2 A system of gases, characterized in that the absorbent outlet of the absorption column is connected to the absorbent inlet of the phase separator by means of a first transfer pump.
4. The slave rich according to claim 1Containing CO 2 Selective absorption separation of CO from a mixed gas of (C) 2 A system of gases characterized in that the phase separator is rich in CO 2 The absorbent phase outlet is communicated with the CO-rich of the desorption tower through a second delivery pump 2 The absorbent phase inlet is connected.
5. The CO-enriched slave according to claim 1 2 Selective absorption separation of CO from a mixed gas of (C) 2 The system of gas is characterized in that the absorbent outlet of the desorption tower is connected with the absorbent inlet of the absorption tower through a third delivery pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322337698.3U CN220779633U (en) | 2023-08-29 | 2023-08-29 | System for selectively absorbing and separating CO2 gas from mixed gas rich in CO2 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322337698.3U CN220779633U (en) | 2023-08-29 | 2023-08-29 | System for selectively absorbing and separating CO2 gas from mixed gas rich in CO2 |
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| Publication Number | Publication Date |
|---|---|
| CN220779633U true CN220779633U (en) | 2024-04-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322337698.3U Active CN220779633U (en) | 2023-08-29 | 2023-08-29 | System for selectively absorbing and separating CO2 gas from mixed gas rich in CO2 |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220779633U (en) |
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- 2023-08-29 CN CN202322337698.3U patent/CN220779633U/en active Active
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