CN217490332U - A low partial pressure and low energy consumption flue gas CO2 capture system - Google Patents

Abstract

The utility model provides a low partial pressure low energy consumption flue gas CO2 entrapment system relates to CO ₂ Field of capture technology, the CO ₂ Trapping systemComprises an absorption tower and a liquid-rich pump, wherein the absorption tower is internally provided with a device for absorbing CO in the raw material gas ₂ The bottom of the absorption tower is communicated with a regeneration tower, material conveying resistance between the absorption tower and the regeneration tower is overcome by a pregnant solution pump, the outlet end of the top of the regeneration tower is connected with a steam compressor, the output end of the steam compressor is connected with a reboiler II, the steam compressor pressurizes acid gas generated by the regeneration tower and then is used for heating the reboiler II, and the output end of the reboiler II is connected with a separation device; the acid gas that produces to the regenerator through vapor compressor pressurizes, makes its pressure and temperature rise, and the steam that has increased the enthalpy is sent the heating chamber of reboiler II to and is used as heating steam, compares prior art and converts steam into the electric energy, will convert the operation that the electric energy was used for entire system again, and this scheme steam heat energy interest rate is higher, makes the relative traditional handicraft of regeneration energy consumption lower.

Description

A low partial pressure and low energy consumption flue gas CO2 capture system

technical field

The utility model relates to the technical field of _CO2 capture, in particular to a low partial pressure and low energy consumption flue gas CO2 capture system.

Background technique

Carbon peaking and carbon neutralization are major national strategies. _{CO 2} capture technology is an important link to achieve carbon neutrality. important role.

The organic amine series absorbents represented by MDEA, MEA and AMP are widely used in the flue gas carbon dioxide capture process. The method of removing carbon dioxide from the mixed gas; and the high energy consumption of regeneration has always been a pain point in the industry, accounting for more than two-thirds of the total operating cost.

Patent CN103566712B proposes a carbon dioxide capture process, which utilizes high-temperature flue gas waste heat by-produced steam for the reboiler heating of the device; uses the waste heat of the regeneration tower top gas by means of heating and expanding to drive the turbine to generate electricity, and the generated electricity can meet the needs of the whole system. Power supply to the active equipment of the purification system. Compared with the traditional process, the energy consumption of the reboiler is reduced by 15-25%. High-temperature flue gas waste heat by-product steam only utilizes external energy, and does not fundamentally reduce regeneration energy consumption. The energy conversion efficiency is relatively low by using the residual heat of the regeneration tower top gas to heat and expand the turbine to drive the power generation.

Under the premise that the state strongly advocates reducing energy consumption, how to effectively reduce renewable energy consumption and reduce the cost of carbon dioxide capture has become a key issue in carbon dioxide capture technology.

Utility model content

Aiming at the deficiencies of the prior art, the utility model provides a low partial pressure and low energy consumption flue gas _{CO 2} capture system, which includes an absorption tower and a rich liquid pump. Absorbent, the bottom of the absorption tower is communicated with the regeneration tower, the material conveying resistance between the absorption tower and the regeneration tower is overcome by the rich liquid pump, the outlet end of the top of the regeneration tower is connected with a steam compressor, and the steam compressor outputs The end is connected with a reboiler II, and the steam compressor pressurizes the acid gas produced by the regeneration tower to heat the reboiler II, and the input end of the reboiler II is communicated with the regeneration tower, and the reboiler II The output end is connected to a separation device, which separates the moisture in the acid gas from CO ₂ .

Further, the input end of the rich liquid pump is connected to the bottom of the absorption tower, and the output end of the rich liquid pump is connected to the upper part of the regeneration tower.

Further, a lean liquid pump is also connected to the bottom of the regeneration tower, a lean and rich liquid heat exchanger is arranged between the output end of the rich liquid pump and the regeneration tower, and the output end of the rich liquid pump is connected to the lean and rich liquid heat exchanger. The cold end inlet end is connected, the cold end outlet end of the lean and rich liquid heat exchanger is connected with the upper part of the regeneration tower; the output end of the lean liquid pump is connected with the hot end input end of the lean rich liquid heat exchanger, and the lean rich liquid exchange The output end of the hot end of the heater is connected with the input end of the water cooler, and the output end of the water cooler is communicated with the absorption tower.

Further, the bottom of the regeneration tower is connected to the input end of the reboiler I, and the output end of the reboiler I is connected to the regeneration tower.

Further, the capture system further includes a recovery device arranged at the top of the absorption tower, and the recovery device recovers the absorbent in the purified gas passing through the absorption tower.

Further, the recovery device includes a water washing device connected to the top of the absorption tower, and the water washing device removes the absorbent in the raw gas through the water liquid; the water washing device includes a circulating water tank, and the liquid outlet end of the circulating water tank is connected to the circulating water The input end of the water pump is connected, the output end of the circulating water pump is connected to the input end of the water cooler of the absorption tower, the liquid inlet end of the circulating water tank and the output end of the water cooler of the absorption tower are both connected with the top of the absorption tower, and the liquid inlet end of the circulating water tank is located at the top of the absorption tower. Bottom of the output end of the water cooler of the absorption tower.

Further, a vane type high-efficiency demister is arranged at the outlet end of the top of the absorption tower.

Further, the separation device includes a separator connected to the output end of the reboiler II, and an acid gas water cooler is connected to the output end of the separator.

Further, the bottom end of the pretreatment tower is connected to the input end of the water washing pump, the output end of the water washing pump is connected to the input end of the water cooler of the pretreatment tower, and the output end of the water cooler of the pretreatment tower is connected to the top of the pretreatment tower.

The beneficial effects of the present utility model:

(1) By connecting a steam compressor at the outlet end of the top of the regeneration tower, the acid gas generated by the regeneration tower is pressurized by the steam compressor, so that the pressure and temperature rise, and the enthalpy of the steam also increases, which increases the heat The enthalpy steam is sent to the heating chamber of the reboiler to be used as heating steam to keep the rich liquid in the reboiler in a boiling state. After multiple conversions, the steam thermal energy rate of the scheme of the utility model is higher, so that the energy consumption of regeneration is lower than that of the traditional process.

(2) By recovering the heat of the lean liquid, and heating the recovered heat to the rich liquid before entering the regeneration tower, so that the rich liquid has a higher temperature before entering the regeneration tower, and after entering the regeneration tower, the rich liquid is desorbed and desorbed by heating The absorbent part in the liquid contains CO ₂ . At this time, because the rich liquid has a higher temperature, the consumption of low-pressure steam in the reboiler is reduced, and the cost of capturing CO ₂ is reduced.

(3) By setting a vane-type high-efficiency demister at the outlet end of the top of the absorption tower, the vane-type high-efficiency demister, when the raw gas entrains small-sized droplets into the vane-type high-efficiency hair remover, it will be divided into multiple areas by the blades , in the process of passing through each area, the gas will be transformed by the blade for many times. Under the action of the inertial force, the liquid will collide with the blade with kinetic energy. With the help of the Brownian motion of the molecules and the filament capillary effect, the liquid droplets The droplets adhere to the surface of the blade through the coalescence effect, and the droplets are collected below under their own gravity; the absorbent in the raw gas is efficiently recovered, and the consumption of the absorbent is reduced to about 0.6kg/tCO ₂ , which further effectively reduces the cost of carbon dioxide capture .

Description of drawings

Fig. 1 is the _CO2 capture system schematic diagram of embodiment 1;

Fig. 2 is the _CO2 capture system schematic diagram of embodiment 2;

Figure 3 is a schematic diagram of the _CO capture method.

Description of drawing numbers: 1, pretreatment tower, 2, water washing pump, 3, water cooler of pretreatment tower, 4, absorption tower, 5, circulating water tank, 6, circulating water pump, 7, water cooler of absorption tower, 8, intermediate cooling device, 9, rich liquid pump, 10, lean and rich liquid heat exchanger, 11, regeneration tower, 12, reboiler I, 13, reboiler II, 14, lean liquid pump, 15, water cooler, 16, filtration device, 17, amine purification system, 18, steam compressor, 19, separator, 20, acid gas water cooler, 21, acid gas cooler, 22, reflux pump.

Detailed ways

In order to make the purposes, technical solutions and advantages of the embodiments of the present utility model clearer, the technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model. The embodiments described above are a part of the embodiments of the present invention, but not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present invention.

It should be noted that when an element is referred to as being "fixed to" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present.

Example 1

Below in conjunction with accompanying drawing 1 in the embodiment of the present utility model, the technical solution in the embodiment of the present utility model will be clearly and completely described, and the process is as follows:

Referring to Figure 1, a low partial pressure and low energy consumption flue gas CO ₂ capture system includes a pretreatment tower 1, an absorption tower 4, a regeneration tower 11 and a lean-rich liquid heat exchanger 10; the raw material gas first enters the pretreatment Tower 1, the bottom end of the pretreatment tower 1 is connected to the input end of the water washing pump 2, the output end of the water washing pump 2 is connected to the input end of the pretreatment tower water cooler 3, and the output end of the pretreatment tower water cooler 3 is connected to the top of the pretreatment tower 1, namely The output end of the pretreatment tower water cooler 3 extends into the pretreatment tower 1 .

When in use, start the water washing pump 2, and the solution falls from the top of the pretreatment tower 1 through the water cooler 3 of the pretreatment tower, and the raw material gas is introduced into the pretreatment tower 1, and the raw material gas is in countercurrent contact with the solution to achieve the removal of impurities from the raw material gas. For the purpose of cooling, the solution in the pretreatment tower 1 flows out from the bottom of the pretreatment tower 1, and is cooled by the pretreatment tower water cooler 3 and returned to the pretreatment tower 1 for recycling, and the raw gas entering the pretreatment tower 1 is washed, A purified gas is formed; wherein, the solution can be water, or other liquids that can replace water to realize the impurity removal and cooling of the raw material gas, so as to prevent the raw materials with too high temperature from entering the absorption tower 4 and reduce the subsequent absorption of _CO by the absorbent. efficiency.

The raw material gas after cooling and impurity removal is introduced into the lower part of the absorption tower 4, and when the raw material gas entering the absorption tower 4 contacts with the absorbent, the CO ₂ in the raw material gas is absorbed by the absorbent;

An absorbent recovery device is arranged at the top of the absorption tower 4, and the recovery device recovers the absorbent in the purified gas passing through the top of the absorption tower 4; wherein the recovery device includes a water washing device connected to the top of the absorption tower 4, and the water washing device passes through the water liquid The absorbent in the purified gas is washed away, the absorbent is melted into the water, and then the purified gas from which the absorbent has been washed is discharged into the atmosphere through the top of the absorption tower 4.

The washing equipment includes a circulating water tank 5, the liquid outlet end of the circulating water tank 5 is connected with the input end of the circulating water pump 6, the output end of the circulating water pump 6 is connected with the input end of the absorption tower water cooler 7, wherein the liquid inlet end of the circulating water tank 5 and the output end of the absorption tower water cooler 7 are connected. The ends are all communicated with the inner top of the absorption tower 4, and the liquid inlet end of the circulating water tank 5 is located at the bottom of the output end of the absorption tower water cooler 7, which is convenient for recycling the cleaning liquid sprayed from the output end of the absorption tower water cooler 7; Instead of liquid water, the liquid of the absorbent in the purified gas is washed away, and it is melted with the absorbent.

When in use, the temperature of the water liquid entering into the water cooler 7 of the absorption tower is set at about 39-40° C. to ensure the effect of the water liquid absorbing the absorbent.

In order to strengthen the gas-liquid mass transfer efficiency of the absorbent entrained in the water-liquid absorption and purification gas at the top of the absorption tower 4, and improve the cleaning effect of the water-liquid, we set up the output end of the water cooler 7 of the absorption tower and the liquid inlet end of the circulating water tank 5. Three-layer sieve tray.

In order to further recover the absorbent in the purified gas and reduce the consumption of the absorbent, we set up a vane-type high-efficiency demister and a vane-type high-efficiency demister at the outlet end of the top of the absorption tower 4. The principle is: the gas phase (ie the raw material gas) is entrained with Small-sized droplets enter the blade-type high-efficiency hair remover, which will be divided into multiple areas by the blades. During the process of passing through each area, the gas will be rapidly transformed by the blades for many times. Under the action of inertial force, the liquid will The blades collide with kinetic energy. With the help of the Brownian motion of molecules and the capillary effect of filaments, the droplets are attached to the surface of the blade through the coalescence effect, and the droplets are collected below under their own gravity; the absorbent in the raw gas is efficiently recovered, so that the The consumption of absorbent is reduced to about 0.6kg/ _tCO2 , which effectively reduces the cost of carbon dioxide capture.

1, the input end of the rich liquid pump 9 is connected to the bottom of the absorption tower 4, the output end of the rich liquid pump 9 is communicated with the upper part of the regeneration tower 11, and the top outlet end of the regeneration tower 11 is connected with a steam compressor 18. The output end of the steam compressor 18 is connected to a reboiler, and the reboiler includes a reboiler II13 and a reboiler I12 connected to the bottom of the regeneration tower 11. The steam compressor 18 pressurizes the acid gas generated at the top of the regeneration tower 11. It is then used to heat the reboiler II13 to maintain the boiling state of the lean liquid in the reboiler II13. The output end of the regeneration tower 11 is connected to a separation device, and the separation device separates the moisture in the acid gas from CO ₂ to obtain CO ₂ ; Boiler II13 adopts shell-and-tube thermosyphon type; the output end of reboiler I12 is communicated with regeneration tower 11.

When in use, the absorbent absorbs _CO2 in the absorption tower 4 to form a rich liquid, which is transported to the regeneration tower 11 through the rich liquid pump 9, and the rich liquid enters from the upper part of the regeneration tower 11, and the rich liquid is in the regeneration tower 11. The absorbent CO ₂ in the rich liquid is desorbed, and the water in the rich liquid is evaporated into water vapor; the acid gas is compressed and pressurized by the steam compressor 18; after the acid gas is pressurized to 2.5-3.5 bar.g, it is used for heating again Boiler II13 fully recovers the latent heat of acid gas. Compared with the existing process, the energy utilization efficiency is high, which greatly reduces the consumption of low-pressure steam for regeneration, and reduces the energy consumption of regeneration by about 30% compared with the traditional process.

The principle of steam compressor 18: Because the acid gas contains about 70% water vapor, this gas is compressed by the compressor to increase its pressure and temperature, and the enthalpy of the acid gas also increases, which increases the enthalpy of the gas. The acid gas is sent to the reboiler II13 of the regeneration tower 11 as heating steam, so that the lean liquid in the reboiler II13 is kept in a boiling state, and the water vapor in the acid gas is condensed into water, so that the latent heat in the secondary steam is obtained. Make full use of it, so as to achieve the purpose of energy saving.

Referring to Figure 1, the separation device includes a separator 19 connected to the output end of the reboiler II 13, the output end of the separator 19 is connected to an acid gas water cooler 20, and the output end of the acid gas water cooler 20 is connected to an acid gas separator 21. A reflux pump 22 is connected to the liquid phase outlet of the acid gas separator 21.

After the acid gas from the reboiler II13 passes through the separator 19, the liquid phase passes through its own pressure to remove the acid gas separation 21 to recover the absorbent, and after the gas phase is decompressed to 50 kPa.g, it enters the acid gas water cooler 20 for further cooling and then enters the acid gas separation. Device 21, the liquid phase is pumped back to the regeneration tower 11 through the reflux pump 22, and the gaseous phase obtains CO ₂ product gas with a purity of 99.5%, which is sent to the subsequent process section for use.

Please refer to Figure 1. In order to ensure the absorption efficiency of the absorbent to absorb _{CO 2} , we add an intermediate water cooler 8 in the middle of the absorption tower 4 to reduce the temperature of the rich liquid to about 39-40 ° C. The effect of increasing the temperature on the decrease of the absorption efficiency increases the absorption rate of the absorbent by about 10%.

When in use, after the absorbent absorbs CO ₂ in the upper part of the absorption tower ₄ , the temperature of the absorbent will rise, and the absorption coefficient of the absorbent at low temperature is relatively high. The absorption rate of the absorbent improves the _CO2 capture efficiency.

Example 2

Please refer to FIG. 2 , in order to recover and reuse the heat of the lean liquid, a lean-rich liquid heat exchanger 10 is arranged between the output end of the rich liquid pump 9 and the regeneration tower 11 . The cold end inlet end of the liquid heat exchanger 10 is connected, the cold end outlet end of the lean and rich liquid heat exchanger 10 is connected with the upper part of the regeneration tower 11; the output end of the lean liquid pump 14 is connected with the hot end inlet of the lean rich liquid heat exchanger 10, The outlet of the hot end of the liquid heat exchanger 10 is connected to the input end of the water cooler 15 .

When in use, the lean liquid pump 14 first transports the lean liquid to the lean-rich liquid heat exchanger 10 for heat exchange, and the lean-rich liquid heat exchanger 10 adopts a low-temperature difference lean-rich liquid heat exchanger. In order to reduce the sensible heat of the lean liquid, the lean-rich liquid heat exchanger 10 heats the above-mentioned rich liquid that is about to enter the regeneration tower 11, so that the rich liquid has a higher temperature before entering the regeneration tower 11, reduces the consumption of low-pressure steam at the bottom of the regeneration tower 11, and improves the The efficiency of desorption of CO ₂ is reduced, and the cost of CO ₂ capture is reduced; then the lean liquid is sent to the water cooler 15 for cooling, and then sent to the absorption tower 4 after cooling.

Example 3

Please refer to Figure 3, a low partial pressure and low energy consumption flue gas _CO2 capture system, including the following steps:

S1. Absorb CO ₂ , pass the feed gas through the absorbent, and the absorbent absorbs CO ₂ in the feed gas to form a rich liquid,

S2. Desorption of rich liquid to produce acid gas, which mainly contains CO ₂ , H ₂ O and absorbent;

S3. Compress the acid gas, pressurize the acid gas to 2.5-3.5 bar.g, increase its pressure and temperature, recover the latent heat of the acid gas, and apply the recovered latent heat to the reboiler for heating the bottom of the regeneration tower;

S4, cooling and separation, the acid gas is cooled, the saturated steam is condensed into a liquid phase, and the liquid phase is separated from CO ₂ to obtain CO ₂ .

In order to reduce the consumption of the absorbent, after step S1 is performed, the absorbent is recovered, the water liquid is sprayed into the purified gas, the absorbent entrained in the raw gas is recovered, and the absorbent is dissolved in the water liquid.

Before performing step S1, the raw material gas is first washed with water to remove impurities in the raw material gas, and the temperature of the raw material gas is lowered. When the raw material gas is washed with water, the water and the raw material gas are in countercurrent contact, and the cleaning effect is better.

The temperature of the rich liquid prepared in step S1 is lowered, and the temperature of the rich liquid is lowered to 39-40°C.

In order to make full use of the sensible heat of the lean liquid, after step S2 is performed, the rich liquid after desorption of CO ₂ forms a lean liquid, the heat of the lean liquid is recovered, and the recovered heat is used to warm the rich liquid before desorption in step S2.

The lean liquid after recovering sensible heat is cooled to 39-40°C, and the cooled lean liquid enters the absorption tower to spray and absorb CO ₂ .

The rich liquid is desorbed in the regeneration tower 11, and the acid gas is generated at the top of the regeneration tower 11. The reboiler II 13 and the steam compressor 18 are connected to the regeneration tower 11. The acid gas is compressed and pressurized by the steam compressor 18, and the recovered acid gas is The latent heat acts on the rich liquid in the heating reboiler II13.

It should be noted that, in this document, if there are relational terms such as first and second, etc., it is only used to distinguish one entity or operation from another entity or operation, and does not necessarily require or imply these entities or operations There is no such actual relationship or order between them. Moreover, the terms "comprising", "comprising" or any other variation thereof are intended to encompass a non-exclusive inclusion such that a process, method, article or device that includes a list of elements includes not only those elements, but also includes not explicitly listed or other elements inherent to such a process, method, article or apparatus. Without further limitation, an element qualified by the phrase "comprising a..." does not preclude the presence of additional identical elements in a process, method, article or apparatus that includes the element.

The above embodiments are only used to illustrate the technical solutions of the present utility model, but not to limit them; although the present utility model has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that: it can still be used for the foregoing implementations. The technical solutions described in the examples are modified, or some technical features thereof are equivalently replaced; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims (9)

1. a low partial pressure and low energy consumption flue gas _CO capture system, comprising an absorption tower (4) and a rich liquid pump (9), and the absorption tower (4) is provided with an absorption for absorbing _CO in the raw material gas It is characterized in that the bottom of the absorption tower (4) is communicated with the regeneration tower (11), and the material conveying resistance between the absorption tower (4) and the regeneration tower (11) is overcome by the rich liquid pump (9), so the A steam compressor (18) is connected to the top outlet end of the regeneration tower (11), and a reboiler II (13) is connected to the output end of the steam compressor (18). The acid gas generated in 11) is pressurized and used to heat the reboiler II (13), the input end of the reboiler II (13) is communicated with the regeneration tower (11), and the output of the reboiler II (13) The end is connected with a separation device, which separates the moisture in the acid gas from _CO2 . 2. A low partial pressure and low energy consumption flue gas CO ₂ capture system according to claim 1, wherein the input end of the rich liquid pump (9) is connected to the bottom of the absorption tower (4), and the rich liquid pump (9) is connected to the bottom of the absorption tower (4). The upper part of the regeneration tower (11) at the output end of the liquid pump (9) is communicated. 3. A low partial pressure and low energy consumption flue gas CO ₂ capture system according to claim 2, wherein a lean liquid pump (14) is also connected at the bottom of the regeneration tower (11), and the rich liquid A lean-rich liquid heat exchanger (10) is arranged between the output end of the pump (9) and the regeneration tower (11), and the output end of the rich liquid pump (9) is connected to the cold end inlet end of the lean-rich liquid heat exchanger (10). connection, the outlet end of the cold end of the lean-rich liquid heat exchanger (10) is communicated with the upper part of the regeneration tower (11); the output end of the lean liquid pump (14) is connected to the input end of the hot end of the lean-rich liquid heat exchanger (10) The output end of the hot end of the lean and rich liquid heat exchanger (10) is connected to the input end of the water cooler (15), and the output end of the water cooler (15) is communicated with the absorption tower (4). 4. A low partial pressure and low energy consumption flue gas CO ₂ capture system according to claim 1, wherein the bottom of the regeneration tower (11) is connected to the input end of the reboiler I (12), and the The output end of the reboiler I (12) is communicated with the regeneration tower (11). 5. A low partial pressure and low energy consumption flue gas _CO2 capture system according to claim 1, characterized in that the capture system further comprises a recovery device arranged at the top of the absorption tower (4), the recovery device The absorbent in the purified gas passing through the absorption tower (4) is recovered. 6. A low partial pressure and low energy consumption flue gas CO ₂ capture system according to claim 5, wherein the recovery device comprises a water washing device connected to the inner top of the absorption tower (4), the water washing device The absorbent in the purified gas is removed by water washing; the water washing equipment includes a circulating water tank (5), the liquid outlet end of the circulating water tank (5) is connected to the input end of the circulating water pump (6), and the circulating water pump (6) outputs The end is connected with the input end of the absorption tower water cooler (7), the liquid inlet end of the circulating water tank (5) and the output end of the absorption tower water cooler (7) are both communicated with the inner top of the absorption tower (4), and the circulating water tank (5) ) The liquid inlet end is located at the bottom of the output end of the absorption tower water cooler (7). 7 . The flue gas CO ₂ capture system with low partial pressure and low energy consumption according to claim 1 , wherein a vane type high-efficiency demister is arranged at the outlet end of the top of the absorption tower ( 4 ). 8 . 8. The flue gas CO ₂ capture system with low partial pressure and low energy consumption according to claim 1, wherein the separation device comprises a separator (19) connected to the output end of the reboiler II (13), An acid gas water cooler (20) is connected to the output end of the separator (19). 9. A low partial pressure and low energy consumption flue gas CO ₂ capture system according to any one of claims 1-8, characterized in that the capture system further comprises a pretreatment tower (1), the pretreatment tower (1) The bottom end is connected to the input end of the water washing pump (2), the output end of the water washing pump (2) is connected to the input end of the pretreatment tower water cooler (3), and the output end of the pretreatment tower water cooler (3) is connected to the The top of the pretreatment tower (1) is connected.

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