System and method for recovering carbon dioxide from flue gas

Abstract

To downsize the recovery system of carbon dioxide (CO2) from a flue gas.SOLUTION: The recovery treatment of CO2 from a flue gas includes the steps of: supplying and cooling the CO2-containing flue gas into at least one direct contact type cooler (DCC) including a rotary packed bed (RPB); and passing the cooled flue gas discharged from the DCC through at least one absorber including the RPB, moving a solvent from the inner peripheral part of the RPB of the absorber toward the periphery and reacting it with the cooled flue gas flown in a reverse direction.SELECTED DRAWING: Figure 3A

Description

[Technical Field]

[0001] The present invention relates to chemical processes, and in particular to processes for recovering carbon dioxide from flue gases. [Background technology]

[0002] The subject matter addressed in the "Background" section should not be considered prior art merely as a result of being mentioned in the "Background" section. Similarly, the problems mentioned in the "Background" section or problems related to the subject matter in the "Background" section should not be considered problems already recognized in the prior art. The subject matter in the "Background" section merely represents different solutions, some of which may even themselves correspond to embodiments of the claimed technology.

[0003] Figure 1 shows a block diagram 100 of a conventional process for recovering carbon dioxide (CO2) from flue gas. A solvent that reacts only with CO2 is used to separate CO2 from the gas mixture. After reacting with CO2, the solvent can be thermally regenerated to release the CO2, making it reusable for further CO2 processing. CO2-laden flue gas 102 contacts a liquid solvent in a fixed-packed column 104. The liquid solvent cascades by gravity from the top to the bottom of the fixed-packed column 104, where it collects in a sump.

[0004] The second fixed packed column 106 has a structured packed bed and includes multiple scrubbing stations for the removal of solvent and volatile chemicals. As the CO2-depleted gas mixture passes through these scrubbing stations, residual solvent and volatile chemicals formed by decomposition reactions of the solvent components in the gas are removed. The CO2-depleted gas mixture 108 is then discharged from the top of the fixed packed column 104. All scrubbing stations are within the same structured packed bed and use either water or acid.

[0005] The solvent is fed into the top of the stripping tower 112 and falls by gravity above the packing to the bottom of the stripping tower 112. At the bottom, the solvent is drawn into the reboiler 114. Inside the reboiler 114, the solvent is heated to a temperature at which the water present in the solvent vaporizes under the operating pressure of the stripping tower 112. The water vapor and CO2 rise to the top of the stripping tower 112, where they are cooled to approximately 40°C by a condenser. This condenses the water vapor into water 116 and separates it from the gaseous CO2 118. The condensed water 116 is returned to the stripping tower 112 through the reflux drum 120, and the gaseous CO2 118 is used in downstream processes. Meanwhile, the solvent remaining at the bottom of the stripping tower 112 is returned to the absorber through the heat exchanger 110 as a solvent with a low CO2 content (CO2-lean solvent) and is reused in the CO2 absorption process described above.

[0006] The fixed-packed columns used in conventional processes are inefficient at mixing the CO2 present in the flue gas, and the solvent flow is limited by gravity, limiting the amount of solvent delivered to the water wash or pickling unit. Furthermore, the fixed-packed columns used in conventional processes are large, requiring a lot of space, which contributes to the high costs of installing and operating the system. Therefore, improved systems and processes for capturing CO2 from flue gas are highly desirable. Summary of the Invention

[0007] In the following, several embodiments of the present invention are presented and described in detail, all of their features being set forth. The words "comprise," "have," "include," "includes," and the like have the same meaning and are open-ended, i.e., they do not imply that subject matter is exhaustive or limited to the items listed.

[0008] It should also be noted that, hereinafter and in the claims, the singular terms "a," "an," and "the" include the plural unless the context clearly dictates otherwise. Although any systems and methods similar or equivalent to those described below can be used to practice or practice embodiments of the present invention, the preferred systems and methods are described below.

[0009] According to one aspect of the present invention, a process for recovering CO2 from flue gas is provided, comprising feeding the CO2-containing flue gas to at least one rotating packed bed (RPB) absorber, wherein a solvent is fed through the inner periphery of the at least one RPB absorber and moves toward the outer periphery of the RPB absorber to react with the flue gas flowing in the counter-flow direction.

[0010] Preferably, the process further comprises the step of thermally regenerating the solvent that has reacted with CO2, with the aim of recycling the solvent in the process.

[0011] More preferably, the process further comprises washing the flue gas with water and / or acid to remove any solvent remaining in the flue gas, optionally with the water wash and / or acid wash being carried out in a separate RPB.

[0012] Preferably, the housing of the RPB is mounted on a rotatable disk.

[0013] Preferably, feeding the flue gas comprising CO2 to at least one rotating RPB absorber comprises feeding the flue gas to 2, 3, 4, 5, or 6 RPB absorbers.

[0014] More preferably, 2, 3, 4, 5 or 6 of the RPB absorbers described above are arranged in series on a common shaft.

[0015] Preferably, the solvent reacts with counter-flowing flue gas to remove CO2 from the flue gas, resulting in a solvent that is high in CO2 (a CO2-rich solvent).

[0016] Preferably, the process further comprises passing the CO2-rich solvent through a stripper, which strips the CO2 from the CO2-rich solvent to form a CO2-lean solvent.

[0017] Preferably, the stripping device is a stripping tower, a fixed stripping tower, or an RPB stripping device.

[0018] Preferably, the CO2 lean solvent is reintroduced into at least one rotating RPB absorber.

[0019] Preferably, the process further comprises passing the CO2-rich solvent discharged from the at least one RPB absorber through an RPB O2 remover or fixed packed bed O2 remover to remove dissolved O2 from the solvent.

[0020] More preferably, the step of removing O2 from the CO2-rich solvent by passing the solvent through a RPBO2 remover or a fixed packed bed O2 remover removes at least 90% of the O2 present in the solvent.

[0021] Preferably, each RPB has a radius in the range of 0.2 m to 1.25 m, or 0.2 m to 0.8 m, an axial length in the range of 0.02 m to 1.0 m, or 0.2 m to 0.6 m, and a volume of 0.04 m 3 From 4.9m 3 up to, or 0.04m 3 From 0.6m 3 It is in the range of up to.

[0022] Another aspect of the present invention provides a system for capturing CO2 from flue gas. The system includes at least one RPB absorber configured to rotate. As the RPB absorber rotates, a solvent supplied through an inner periphery of the RPB absorber moves toward an outer periphery of the RPB absorber to react with counterflowing flue gas and capture CO2.

[0023] Preferably, the system further comprises a component for thermally regenerating the solvent that has reacted with CO2, for the purpose of reusing the solvent.

[0024] More preferably, the system further comprises a water wash unit, a pickling unit, or both, through which the flue gas is passed to remove any solvent remaining in the flue gas.

[0025] Preferably, the housing of the RPB is mounted on a rotatable disk.

[0026] Preferably, the system further comprises 2, 3, 4, 5, or 6 RPB absorbers configured to rotate.

[0027] More preferably, 2, 3, 4, 5 or 6 of the RPB absorbers described above are arranged in series on a common shaft.

[0028] Preferably, the solvent reacts with counter-flowing flue gas to remove CO2 from the flue gas, resulting in a CO2-rich solvent.

[0029] Preferably, the system further comprises a stripping device configured to strip CO2 from the CO2-rich solvent to form a CO2-lean solvent.

[0030] More preferably, the peeling device is an RPB peeling device.

[0031] Preferably, the system is configured to reintroduce the CO2 lean solvent into at least one rotating RPB absorber.

[0032] Preferably, the system further comprises an RPB absorber or fixed packed bed O2 remover for removing O2 from the CO2-rich solvent discharged from the at least one RPB absorber.

[0033] More preferably, the RPB02 remover or fixed packed bed O2 remover is configured to remove 90% or more of the O2 present in the CO2-rich solvent.

[0034] Preferably, each RPB has a radius in the range of 0.2 m to 1.25 m, or 0.2 m to 0.8 m, an axial length in the range of 0.02 m to 1.0 m, or 0.2 m to 0.6 m, and a volume of 0.04 m 3 From 4.9m 3 up to, or 0.04m 3 From 0.6m 3 It is in the range of up to.

[0035] In the process described in any one of paragraphs

[0009] to

[0021] or the system described in any one of paragraphs

[0022] to

[0034] , the solvent comprises a tertiary amine, a sterically hindered amine, a polyamine, a carbonate buffer, and / or water (optionally deionized). Optionally, the concentration of water is set in the range of 10% to 70% by weight.

[0036] Preferably, the viscosity of the solvent is set in the range of 1 cP to 10 cP.

[0037] More preferably, the solvent is any of the solvents disclosed in U.S. Patent Application Publication No. 2017 / 0274317, and / or comprises N-methyl-diethanolamine and / or 2-(diethylamino)ethanol as the tertiary amine, 2-amino-2-ethyl-1,3-propanediol, 2-amino-2-hydroxymethyl-1,3-propanediol, and / or 2-amino-2-methyl-1-propanol as the sterically hindered amine, 2-piperazine-1-ethylamine and / or 1-(2-hydroxyethyl)piperazine as the polyamine, potassium carbonate as the carbonate buffer, and / or deionized water.

[0038] Preferably, the solvent comprises the hindered amino alcohol amino-2-methyl-1-propanol, the polyamine aminoethylpiperazine, and water.

[0039] Another aspect of the invention provides an array of RPB absorbers, the array including two, three, four, five, or six RPB absorbers configured to rotate and arranged in series on a common shaft.

[0040] Another aspect of the present invention provides a vacuum solvent thermal regeneration system for removing refractory chlorides, decomposition products, and other contaminants from a CO2 capture solvent. The system includes a raw product exchanger configured to increase the temperature of the CO2 capture solvent, a reboiler configured to further increase the temperature of the CO2 capture solvent discharged from the raw product exchanger so that the refractory chlorides, decomposition products, and other contaminants accumulate therein, and a condenser configured to reduce the temperature of the washed CO2 capture solvent discharged from the raw product exchanger. The raw product exchanger and the reboiler are in communication with each other, and the process for removing the refractory chlorides, decomposition products, and other contaminants from the CO2 capture solvent is carried out in a batch or semi-batch manner.

[0041] Another aspect of the present invention provides a vacuum solvent thermal regeneration system for removing refractory chlorides, decomposition products, and other contaminants from a CO2 capture solvent. The system includes a reboiler configured to elevate the temperature of the CO2 capture solvent so that the refractory chlorides, decomposition products, and other contaminants accumulate therein. The reboiler is configured for batch or semi-batch operation to remove the refractory chlorides, decomposition products, and other contaminants from the CO2 capture solvent. The reboiler is in communication with a condenser. The condenser reduces the temperature of the washed CO2 capture solvent discharged from the reboiler. Preferably, the reboiler and the condenser are in direct communication.

[0042] Preferably, the vacuum solvent heat regeneration system is in communication with a system described in any one of paragraphs

[0022] to

[0038] .

[0043] In another aspect of the present invention, a process for recovering CO2 from flue gas is provided, the process comprising the steps of: Providing a CO2 capture solvent. Introducing the CO2 capture solvent into the RPB absorber and RPB stripper, and optionally into the O2 remover. Supplying steam to a reboiler. Bringing the CO2 capture solvent in the RPB stripper to the desired pressure. Pumping the CO2 capture solvent from around the RPB absorber and the RPB stripper. Introducing the flue gas into the RPB absorber. Monitoring the CO2 output from the RPB stripping device. Activating the RPBO2 scrubber or fixed packed bed O2 scrubber. Stopping the flow of flue gas to the RPB absorber. Monitoring the output of CO2 from the RPB stripper until the output stops. Turning off the steam supply to the reboiler. Stopping the circulation of the solvent. shutting down the RPB stripper, RPB absorber, water washer, pickler, and O2 remover; [Brief explanation of the drawings]

[0044] The accompanying drawings illustrate various embodiments of systems, methods, and the like according to the present invention from various perspectives. Those skilled in the art will appreciate that the boundaries of elements (such as boxes, boxes, or other shapes) shown in these drawings are merely illustrative. In some instances, a single element may be designed as multiple elements, or multiple elements may be designed as a single element. In other instances, an element shown as an internal component of one element may be incorporated as an external component of another element, or vice versa. Furthermore, elements may not be drawn to scale. The following description, made with reference to the drawings, is not intended to limit the invention and does not represent that the embodiments of the invention are exhaustive. The components in the drawings are not necessarily drawn to scale, and the focus is on the principles being illustrated.

[0045] [Figure 1] 1 is a block diagram 100 of a conventional process for recovering CO2 from flue gas according to the prior art. [Figure 2] 2 is a block diagram 200 of a system for capturing CO2 from flue gas, according to an embodiment. [Figure 3A] 3 is a block diagram 300 illustrating the functionality of an RPB absorber 302 in a system for capturing CO2 from flue gas, according to another embodiment. [Figure 3B] A block diagram 3000 showing the function of an RPB absorber 3020 in a system for capturing CO2 from flue gas. [Figure 4A] 4 is a block diagram 400 illustrating a vacuum solvent heat regeneration system according to an embodiment. [Figure 4B] 40 is a block diagram 4000 illustrating a vacuum solvent heat regeneration system according to an embodiment. [Figure 5A]5 is a flowchart 500 illustrating a process for recovering CO2 from flue gas according to an embodiment. [Figure 5B] 5 is a flowchart 500 illustrating a process for recovering CO2 from flue gas according to an embodiment. [Figure 6] 6 is a block diagram 600 illustrating an RPB absorber. [Figure 7] 1 is a graph showing the vapor-liquid equilibrium (VLE) relationship that emerges between the partial pressure of CO2 in a gas and the amount (i.e., concentration) of CO2 in a solvent at 40 degrees Celsius. [Figure 8] This is a design drawing of a system 1200 that captures 10 tons of CO2 per day. DETAILED DESCRIPTION OF THE INVENTION

[0046]

[0013] Embodiments of the present invention will now be described in more detail with reference to the accompanying drawings, in which example embodiments are shown, in which like elements are designated by like reference numerals. However, because the invention defined in the claims can be embodied in many different forms, the claims should not be construed as limiting the embodiments of the invention to the examples given below. The embodiments given below are non-limiting examples, and are only some of many possible examples.

[0047] FIG. 2 shows a block diagram 200 of a system for capturing CO2 from flue gas. First, flue gas 202 is fed into a single RPB absorber 204. A solvent is fed through the inner periphery of the same RPB absorber 204. Inside the RPB absorber 204, a packed bed is housed within a rotatable disk. The disk rotates at high speed, generating centrifugal force that acts on the solvent as it disperses in the packed bed. This centrifugal force moves the solvent radially from the inner periphery to the outer periphery of the RPB absorber 204. The solvent then comes into countercurrent contact with the CO2-laden flue gas 202. This rotation of the RPB absorber 204 increases the mixing of the flue gas 202 with the solvent, thereby increasing the amount of CO2 transferred from the flue gas 202 to the liquid solvent.

[0048] After the CO2 is absorbed by the solvent, the remaining flue gas is washed in one or more water washers 206, 208 and / or one or more pickling units 210. In some cases, the water washers in the packed bed can be replaced with another RPB absorber than the RPB absorber 204. Wash water is supplied from the inner periphery of the other RPB absorber and flows radially through the packed bed to the outer periphery of the other RPB absorber due to centrifugal force generated by the rotation of the absorber. CO2-depleted flue gas is introduced from the outer periphery of the other RPB absorber and flows toward the inner periphery of the absorber. This results in countercurrent contact between the wash water and the CO2-depleted flue gas. A similar process can be applied to pickling units by replacing the wash water with an appropriately concentrated acid solution. After washing, the purified flue gas 212 is released into the atmosphere.

[0049] In some embodiments, the RPB absorber 204 may be replaced by multiple RPB absorbers, i.e., a first RPB absorber and a second RPB absorber. The first and second RPB absorbers have relatively small radii, are arranged in series on a common shaft, and are used to remove CO2 present in the flue gas 202. After a portion of the CO2 is removed in the first RPB absorber, the flue gas 202 flows from the outlet of the first RPB absorber to the inlet of the second RPB absorber. In the second RPB absorber, the flue gas 202 countercurrently contacts the CO2-lean solvent output from the stripper. Thus, the flue gas 202 discharged from the second RPB absorber is depleted of CO2. The flue gas 202 is sent to a water wash and then vented to the atmosphere. The CO2-rich solvent discharged from the first RPB absorber is sent to the stripper for regeneration.

[0050] In one embodiment, the solvent exiting the second RPB absorber and entering the first RPB absorber may be cooled in a heat exchanger 214 as it travels from the second RPB absorber to the first RPB absorber. The CO2-rich solvent 216 released from the RPB absorber 204 is sent to an RPB O2 remover 218. The flue gas 202 exiting the RPB absorber 204 contains oxygen (O2). O2 can react with the solvent to form decomposition products. As a result, the decomposition products formed from the solvent must be removed and replaced with fresh solvent. Because the RPB absorber 204 and RPB stripper 226 are significantly smaller than fixed absorbers and strippers, the residence time of the solvent and gas is significantly shorter. Therefore, the rate of solvent decomposition during each cycle of the above process for capturing CO2 from flue gas is significantly lower.

[0051] In one embodiment, a portion of the O2 present in the flue gas 202 is absorbed by the solvent present within the RPB absorber 204. Such absorption of O2 is undesirable for a number of reasons, including oxidative decomposition of the solvent and contamination of the captured CO2 with O2. Therefore, an RPB O2 remover or fixed packed bed O2 remover 218 may be used to remove dissolved O2 from the CO2-rich solvent. This device strips O2 from the CO2-rich solvent by countercurrently contacting a small stream of CO2 gas output from the stripper with the CO2-rich solvent. Due to the low partial pressure of O2 in the CO2 gas output from the stripper, O2 dissolved in the liquid solvent is transferred from the solvent to the CO2 gas. Stream 220, containing the O2 dissolved in the solvent as a gas, is released from the top of the RPB O2 remover 218 or fed back to the RPB absorber 204.

[0052] The CO2-rich solvent contains 5-10 mg / L or 10-15 mg / L of dissolved O2 as it exits the RPB absorber 204. This O2 decomposes the solvent in the heat exchanger 222 and the RPB stripper 226. Therefore, it is desirable to strip the O2 from the CO2-rich solvent as it exits the RPB absorber. The CO2-rich solvent flow is 12,500 lb. / h, or 25 gpm. The Henry's law constant for O2 is ∼20,000 atm / mole fraction at 50°C. Therefore, a CO2 flow of 15 lb. / h is required to remove 95% of the O2. 15 lb. / h of CO2 will carry away ∼0.1 lb. / h of O2.

[0053] In one embodiment, the solvent may enter the RPB02 remover 218 at the center of the rotating packed bed. As described above, centrifugal force pushes the solvent from the center to the periphery of the rotating packed bed. When the solvent reaches the end of the packed bed, it impacts the wall of the packed bed's casing and flows into a sump. A small stream of CO2 for O2 stripping 240 is supplied through a perforation in the casing wall and is pressurized to flow in the opposite direction of the solvent, from the periphery to the center of the packed bed. A perforation in the center of the packed bed allows the gas to exit the RPB02 remover 218. The rotation of the packed bed vigorously mixes the solvent with the O2 stripping gas. The CO2-rich solvent 260 then exits the RPB02 remover 218 and passes through a heat exchanger 222.

[0054] In another embodiment, CO2-rich solvent enters conventional (fixed) packed-bed O2 remover 218 at the top of the packed tower, while a small stream of CO2 240 for O2 stripping is fed from the bottom of the packed tower. This creates countercurrent contact between the gas and liquid phases. The packed bed may have a through-hole in the center, which allows gas to escape from conventional O2 remover 218. CO2-rich solvent 260 then exits conventional O2 remover 218 and passes through heat exchanger 222.

[0055] In the heat exchanger 222, the CO2-rich solvent 260 is heated by the CO2-lean solvent 242, resulting in the hot CO2-rich solvent 224 being fed to the RPB stripper 226, and the regenerated solvent 228 is fed back to the RPB absorber 204. The hot CO2-rich solvent 224 is fed to the RPB stripper 226 through the inner periphery of the RPB. The RPB stripper 226 rotates, generating centrifugal force. This centrifugal force acts on the hot CO2-rich solvent 224 once it is dispersed in the packed bed. This centrifugal force moves the hot CO2-rich solvent 224 radially, from the inner periphery of the packed bed toward the outer periphery of the RPB. During this movement, the hot CO2-rich solvent 224 is agitated by intense turbulence, forming many droplets. This increases the available surface area for CO2 migration. At the periphery of the RPB, the hot CO2 rich solvent 224 is exhausted through the inner wall of the RPB stripper casing into a solvent reservoir where it collects.

[0056] In one embodiment, the solvent 230 collected in the solvent reservoir may be sent to a reboiler 232. The solvent 230 is heated in the reboiler 232. The temperature in the reboiler 232 is set to vaporize the water in the solvent 230. The water vapor is vaporized under the operating pressure of the RPB stripper 226. The water vapor formed in the reboiler 232 is introduced to the periphery of the RPB stripper 226.

[0057] In one embodiment, the RPB stripper 226 may have a stripping point at its inner periphery to allow the water vapor and CO2 to exit the RPB stripper 226. The water vapor and CO2 are sent to a condenser 234. Inside the condenser 234, the water vapor present with the CO2 is condensed into condensate 238, i.e., water. The condensed water is separated from the CO2 in a reflux line 236. The condensation of the water vapor in the condenser 234 induces a pressure difference between the inner and outer periphery of the packed bed within the stripper. This pressure difference provides a driving force for the water and CO2 to exit the RPB stripper 226. The CO2 is directed downstream to a device 240 for downstream processing.

[0058] In one embodiment, the condensate 238 may be mixed with the hot CO2-rich solvent 224 and then fed into the RPB stripper 226 through the inner periphery of its packed bed. The CO2-lean solvent 242 produced in the reboiler 232 is returned to the process through the heat exchanger 222.

[0059] Figure 3A is a block diagram 300 showing the function of an RPB absorber 302 in a system for capturing CO2 from flue gas. First, flue gas 304 is fed into the RPB absorber 302 to react with a solvent. The RPB absorber 302 is mounted on a rotatable disk, and as it rotates, it receives centrifugal force, which brings the solvent into countercurrent contact with the flue gas containing CO2. After the CO2 is absorbed by the solvent, the remaining flue gas is washed using a water wash and / or an acid wash.

[0060] In one embodiment, wash water may be supplied through the inner periphery 306 of the RPB absorber 302. The wash water flows radially due to centrifugal force, passing through a packed bed within the RPB absorber 302 and reaching the outer periphery of the RPB absorber 302. During water washing, the CO2-depleted flue gas to be treated is introduced into the outer periphery of the RPB absorber 302 and flows toward the inner periphery 306, resulting in countercurrent contact between the wash water and the CO2-depleted flue gas. Similarly, a concentrated acid solution is used to perform acid washing on the CO2-depleted flue gas. After water washing and acid washing, the CO2-depleted flue gas 308 is released.

[0061] In some embodiments, the RPB absorber 302 may be replaced by multiple RPB absorbers, i.e., a first RPB absorber and a second RPB absorber. The first and second RPB absorbers have relatively small radii and are arranged in series on a common shaft to remove CO2 present in the flue gas 304. After a portion of the CO2 is removed in the first RPB absorber, the flue gas 304 flows from the outlet of the first RPB absorber to the inlet of the second RPB absorber. Inside the second RPB absorber, the flue gas 304 countercurrently contacts with the CO2-lean solvent output from the stripper. The flue gas 304 discharged from the second RPB absorber is depleted of CO2. This flue gas 304 is sent to a water wash and then released to the atmosphere. The CO2-rich solvent discharged from the first RPB absorber is sent to the stripper for regeneration.

[0062] In one embodiment, after CO2-rich solvent 310 exits RPB absorber 302, it may be sent to RPB O2 remover 312. A portion of the O2 present in flue gas 304 is absorbed by the solvent present within RPB absorber 302. Because such absorption of O2 is undesirable for the reasons discussed above, RPB O2 remover 312 is used to remove O2 from the CO2-rich solvent. Due to the low partial pressure of O2 in the recovered CO2, any O2 dissolved in the solvent transfers from the solvent to the gas phase. Gas 314 is released from the top of RPB O2 remover 312. Meanwhile, CO2-rich solvent 316 exits RPB O2 remover 312 and is provided to heat exchanger 318.

[0063] In the heat exchanger 318, the CO2-rich solvent 316 is heated by the CO2-lean solvent 350. The hot CO2-rich solvent 320 is then provided to the RPB stripper 322, and the cooled CO2-lean solvent 324 is treated and provided to the RPB absorber 302. The RPB stripper 322 rotates, generating centrifugal force. This centrifugal force acts on the hot CO2-rich solvent 320 as it disperses in the packed bed. This forces the hot CO2-rich solvent 320 through the inner wall of the RPB stripper casing and collects in a solvent sump.

[0064] In one embodiment, the solvent 328 collected in the solvent reservoir may be transported to a reboiler 330. The solvent 328 is heated in the reboiler 330. The steam generated in the reboiler 330 is introduced to the outer periphery of the RPB stripper 322. The inner periphery of the RPB stripper 322 has a stripping point for discharging the steam and CO2 out of the RPB stripper 322. The steam and CO2 are transported to a condenser, where the steam present with the CO2 is condensed into a condensate. The condensed water is separated from the CO2. The steam condenses in the condenser, inducing a pressure difference between the inner and outer periphery of the packed bed in the stripper. This pressure difference provides the driving force for the water and CO2 to exit the RPB stripper 322. The CO2 332 separated from the water is directed downstream to the device 240. A small portion of the CO2 332 is supplied to the O2 removal device 312.

[0065] In one embodiment, the cooled CO2 lean solvent 324 is passed to the RPB absorber 302 via a heat regenerator 326.

[0066] Figure 3B is a block diagram 3000 illustrating the function of an RPB absorber 3020 in a system for capturing CO2 from flue gas. Unlike the configuration shown in Figure 3A, a heat regenerator 3260 is installed at the connection point between the reboiler 3300 and the heat exchanger 3180. In some embodiments, the heat exchanger 3180 and the RPB absorber 3020 may be directly connected. Other elements of block diagram 3000 correspond to elements in Figure 3A, and therefore have a "0" added to the end of their reference numbers. For example, 312 in Figure 3A is 3120 in Figure 3B.

[0067] In one embodiment, as shown in block diagram 400 of FIG. 4A, CO2-lean solvent 402 may be discharged from the cooler outlet and then introduced into a vacuum solvent thermal regeneration system. The vacuum solvent thermal regeneration system is operated to remove refractory chlorides (HSS), decomposition products, and other contaminants from the solvent while their concentration is 2% by weight or greater. The CO2-lean solvent 402 input into the vacuum solvent thermal regeneration system is fed to a raw product exchanger 404. The raw product exchanger 404 increases the temperature of the mixture from 40° C. to 165° C. by heating the mixture with steam 412 from a reboiler 408.

[0068] The CO2-lean solvent 406 exiting the raw product exchanger 404 is then passed to a reboiler 408, which circulates a thermal fluid between itself and the reboiler, raising the temperature of the solvent to between 165°C and 180°C. Sodium hydroxide may be added to the reboiler 408 to liberate HSS and decomposition products from the CO2 capture solvent. In one embodiment, at the end of operation, a residue 410 may be sent to an incinerator for disposal. The vapor component 412 of the mixture passes through the raw product exchanger 404 and enters a condenser 416. The vapor component 412 is condensed to a liquid 418 and then sent to an absorber. The vacuum solvent heat recovery system operates in a semi-batch mode, allowing the HSS and impurities to accumulate in the reboiler 408. After the batch operation is complete, if the liquid level is low, water may be added to the reboiler 408 to facilitate disposal of the residue 410.

[0069] In another embodiment, as shown in block diagram 4000 of FIG. 4B, CO2-lean solvent 4020 discharged from the pump may be taken into a vacuum solvent thermal regeneration system. The temperature of CO2-lean solvent 4020 is 120 degrees Celsius. The vacuum solvent thermal regeneration system is operated to remove HSS, decomposition products, and other contaminants from the solvent while their concentration is 2% by weight or greater. The CO2-lean solvent 4020 input into the vacuum solvent thermal regeneration system is supplied to a reboiler 4080.

[0070] Reboiler 4080 circulates a thermal fluid through it, raising the temperature of the solvent to between 120°C and 180°C. Sodium hydroxide 4200 may be added to reboiler 4080 to liberate HSS and decomposition products from the solvent. In some embodiments, demineralized water 4220 may be added to reboiler 4080. In some embodiments, medium-pressure steam 4240 may be added to reboiler 4080, and medium-pressure steam 4260 may be removed from reboiler 4080. At the end of operation, residue 4100 is sent to an incinerator for disposal. The vapor component 4120 of the mixture is passed to condenser 4160. In some embodiments, cooling water 4300 may be added to condenser 4160, and cooling water 4320 may be removed from condenser 4160. The vapor component 4120 may be condensed to liquid 4180, which may then be sent through a heat exchanger to an absorber as treated solvent (not shown). The vapor component 4120 is sent to the absorber via vacuum pump 4280. The vacuum solvent heat regeneration system is operated in semi-batch mode, allowing the HSS and impurities to accumulate in reboiler 4080. After batch operation is completed, if the liquid level is low, water may be added to reboiler 4080 to facilitate disposal of residue 4100.

[0071] An inherent advantage of using an RPB stripper compared to the use of a fixed stripper tower is that the increased mixing within the RPB stripper results in a greater transfer of CO2 from the liquid phase to the gas phase. This allows the use of RPB strippers that are much smaller than strippers traditionally used. The use of the above-described system and process for capturing CO2 from flue gases also provides the following advantages: Low water content in the solvent reduces the energy required to capture a unit amount of CO2; High CO2 capture rates reduce the capital cost of the CO2 capture plant; Short exposure of the solvent to O2 reduces the percentage of solvent that is decomposed, reducing the need for solvent replenishment; Intermediate cooling increases the amount of CO2 captured by the solvent, reducing the energy required to capture a unit amount of CO2; High temperature uniformity within the RPB absorber and the short residence time of the solvent between the RPB absorber and the RPB stripper reduces the percentage of solvent that is decomposed, reducing the need for solvent replenishment.

[0072] Further advantages of using the above system and process to capture CO2 from flue gas include: Low capital cost of the water wash and pickle units because they are small; Low capital cost due to the implementation of the RPB absorber, water wash, pickle and stripper on a single shaft; Low capital cost of the O2 remover; Low rate of aerosol formation due to the elimination of localized temperature rises from within the RPB absorber; Low rate of solvent cracked and high rate of solvent recovered due to the use of a vacuum solvent heat regeneration system.

[0073] 5 is a flowchart 500 of a process for capturing CO2 from flue gas, according to one embodiment. The flowchart 500 will be described in relation to elements disclosed in the previously described figures.

[0074] Flowchart 500 in FIG. 5 illustrates the architecture, functionality, and operation of a system required for the process of recovering CO2 from flue gas. It should be noted that in alternative embodiments, the functions described in the blocks may occur in an order different from that shown in the figures. For example, two blocks shown consecutively in FIG. 5 may actually occur substantially simultaneously, or the blocks may occur in the reverse order depending on the functionality involved. Furthermore, the process descriptions or blocks in the flowchart should be understood as representing decisions made by a hardware structure, such as a state machine. Flowchart 500 begins at step 502 and proceeds to step 526.

[0075] In step 502, wash water and acid solution begin circulating through the system. In step 504, the RPB absorber and RPB stripper begin rotating. In step 506, liquid solvent is ensured in the reboiler and absorber solvent sump. In step 508, steam is supplied to the reboiler, allowing the stripper pressure to reach the setpoint. In step 510, the circulation pump begins circulating CO2-rich and CO2-lean solvent. In step 512, flue gas begins flowing into the system. In step 514, CO2 output from the RPB stripper is monitored. In step 516, the RPB stripper remover is activated once CO2 output from the RPB stripper is available. In step 518, the flue gas flow is stopped. In step 520, the system waits until CO2 output ceases. In step 522, steam supply to the reboiler is stopped. In step 524, the solvent circulation is stopped. In step 526, the RPB stripper, RPB absorber, water washer, pickler, and O2 remover are shut down.

[0076] FIG. 6 shows a block diagram 600 of a prototype RPB absorber according to one embodiment. This prototype allows for solvent experiments under various conditions and allows for temperature and flow rate measurements, even in hazardous locations. A simulated flue gas is generated by mixing CO2 602, which passes through flow controller 604, with air 610, which passes through flow controller 612. This simulated flue gas is then fed to a humidifier 606 equipped with a hot water source 614. The temperature of the simulated flue gas after humidifier 606 is measured by a temperature measurement controller 616. The simulated flue gas is then fed to an RPB absorber 626. This RPB absorber has an inner diameter of 0.08 m, an outer diameter of 0.3 m, and a radial packed bed depth of 0.11 m. The length of the packed bed along the axis of rotation is 0.02 m. The RPB absorber 626 is housed in a polypropylene case with an inner diameter of 0.36 m. The RPB absorber 626 is driven by a synchronous motor with a maximum speed of 3000 rpm.

[0077] RPB absorber 626 is supplied with solvent from amine supply tank 608. Inside 620 of tank 608, a hot water system 622 uses circulating hot water to heat the solvent. The flow rate of solvent from amine supply tank 608 is measured by flow meter 618, and the temperature of amine supply tank 608 is measured by thermometer 628. The temperature of gas 632 exiting RPB absorber 626 is measured by thermometer 630, and the temperature of amine 636 exiting RPB absorber 626 is measured by thermometer 634. Experimental Example Experimental Example 1: Determining operating conditions for multiple solvents

[0078] In this example, operating conditions for several solvents were determined and are shown in Table 1.

[0079] CO2 uptake was measured for a range of solvent flow rates and a range of rotation speeds. The parameter settings are shown in Table 1. [Table 1]

[0080] In each experiment, the CO2602 feed was kept at 12 mol %. This concentration is similar to that found in coal-fired flue gas. The temperature of the liquid solvent was 40°C. The liquid-to-gas ratio is an important parameter in the CO2 capture process. The higher the solvent flow rate, the better the absorber performance, provided that flooding (the phenomenon of liquid solvent backflow) does not occur in the absorber. Since the solvent absorbs only a small amount of CO2, it is necessary to increase the stripper load as the solvent amount increases. Taking this into consideration, the optimal solvent flow rate can be found. Increasing the stripper load increases the energy required to carry out the CO2 capture process. The experimental results shown in Table 1 indicate the required number of transfer units (NTU) OG) can be calculated. For 30 wt% monoethanolamine, a rotation speed of 600 rpm and a liquid-to-gas ratio of 3.3 resulted in 12.1% CO2 being fed and 9.1% CO2 being discharged. Therefore, the number of transfer units required is

number

number

[0081] The gas-side transfer unit height was found to be 0.39 m. This indicates that the gas-side transfer unit is significantly reduced in the RPB absorber compared to the fixed absorber. Table 2 shows the experimental results for five solvents in accordance with one embodiment. [Table 2]

[0082] Experiments were conducted at multiple liquid-to-gas ratios and rotational speeds for each solvent, providing a method for determining the size of the RPB absorber required to capture 90% of the CO2 at 600 rpm. Experimental Example 2: Simulation of a vacuum solvent heat regeneration system to determine the operating parameters required to maximize solvent recovery.

[0083] For this example, experimental results for a vacuum solvent thermal regeneration system are shown in Table 3. A sample of solvent obtained from an operating CO2 capture plant was regenerated in the experimental setup, and the results for the regenerated solvent are shown in Table 3. Additionally, a sensitivity analysis was simulated to optimize the operating parameters to maximize the capture amount and minimize the energy required. [Table 3]

[0084] In this example, a simulation of a vacuum solvent heat regeneration system was used to determine the operating parameters required to maximize solvent CDRMax recovery. Table 4 shows the results of a simulation of the vacuum solvent heat regeneration system performed in accordance with one embodiment. Table 4 displays the optimal results at 165 degrees Celsius and 0.75 bar(a). [Table 4] Experimental Example 3: Relationship between the amount of CO2 in the vapor and the amount (i.e., concentration) of CO2 in the solvent at 40 degrees Celsius

[0085] In this example experiment, the relationship between the amount of CO2 in the vapor and the amount (i.e., concentration) of CO2 in the solvent at 40 degrees Celsius was determined. Figure 7 shows a graph illustrating the vapor-liquid equilibrium (VLE) relationship that appears between the partial pressure of CO2 in the vapor and the amount (i.e., concentration) of CO2 in the solvent at 40 degrees Celsius. Experimental Example 4: Viscosity of solvents without and with CO2

[0086] In this example, the viscosity of a solvent without CO2 uptake and a solvent with CO2 uptake were determined. Table 5 shows the viscosity at 40 degrees Celsius of a solvent without CO2 uptake and a solvent with CO2 uptake. [Table 5] The values ​​are expressed as weight percent in Table 5. In each case, demineralized water was used to effect the equilibration. Experimental Example 5: Methodology for selecting the size of RPB to improve its performance

[0087] In this experimental example, an RPB design was determined that could capture 90% of the CO2 from the flue gas of a "coal-based fuel" containing 10% CO2 by volume, and capture 10 tons of CO2 per day.

[0088] In this example, the inner diameter of the RPB (d i ), outer radius (r o ), inner radius (r i The diameter (mm), length (mm), and axial length (z) were determined. These parameters were used to determine the cross-sectional area and total volume required for the RPB.

[0089] Inner diameter of RPB (d i ) was chosen so that the RPB would contain space for a mechanism to disperse the liquid solvent, while preventing excessive gas velocity from entraining the solvent during operation of the RPB.

[0090] The axial length (z) of the RPB was determined to be the minimum acceptable value within the range that would provide a sufficient volume for the packed bed to move the required amount of material without flooding the RPB.

[0091] In a conventional fixed packed column, the height (H) of the packed bed required to transfer a specific amount of material is determined by the following formula: That is, the height (H) is calculated by multiplying the gas-side transfer unit height (HTU OG ) and the number of transfer units on the gas side (NTU OG ) is the product of

number

[0092] In an RPB, the conditions required for the packed bed are different from those of a conventional fixed packed column. This is because the packed bed of an RPB is not linear in the height direction. Therefore, the following analogy can be used: The cross-sectional area of ​​the packed bed (π(r o 2 -r i 2 )) is equivalent to the height (H) of the packed bed in a conventional fixed packed column. This is the total moving unit area (ATU) of the gas side. OG ) and total transfer units on the gas side (NTU OG ) and is expressed by the following equation.

number

[0093] The cross-sectional area of ​​the packed bed (π(r o 2 -r i 2 To determine the ATU OG and NTU OG Both y and y must be known. These can be derived experimentally using the following equations: in is the mole fraction of the component to be absorbed contained in the supplied gas, and y out is the mole fraction of the absorbed component contained in the exhaust gas, and Q G is the volumetric flow rate of the gas, z is the axial length of the RPB, and K G a is the mass transfer coefficient on the gas side.

number

[0094] In this example, solvent trials were conducted using a prototype RPB absorber. To simulate conditions expected in an actual CO2 capture plant, a lean CO2 solvent with a CO2 concentration of 0.1 moles per mole of solvent alkalinity was used. Gas-side mass transfer coefficients were then measured under conditions typical of an operational CO2 capture plant.

[0095] The solvent test in this example required the calculation of the gas-side mass transfer coefficient. The cross-sectional area of ​​the packed bed, the axial length, and the volumetric gas flow rate were known, and the mole fraction of CO2 in the supplied gas (y in ) and the mole fraction of CO2 contained in the emitted gas (y out ) and were both measured.

[0096] In this example experiment, the K G The a value was used to determine the radial depth of the packed bed that would allow 90% CO2 recovery from flue gas with a CO2 concentration of 10% by volume. Experimental Example 6: Size of RPB to capture 1 ton of CO2 per day

[0097] In this experimental example, the size of the RPB was determined with the goal of capturing 1 ton of CO2 per day. [Table 6] As shown in Table 6, the dimensions of the RPB absorption device and stripping device are all less than 1 m. Thus, the RPB absorption device and stripping device are relatively small and compact. Experimental Example 7: Design of an RPB that captures 10 t of CO2 per day

[0098] In this experimental example, the design of an RPB was determined with the goal of capturing 10 t of CO2 per day at a capture rate of 90% from flue gas with a CO2 concentration of 10% by volume.

[0099] Figure 8 shows a CO2 capture system 1200. This system 1200 is used to capture 10 tons of CO2 per day. In Figure 8, solid lines indicate the path of the liquid solvent, and dashed lines indicate the path of the gas.

[0100] In this example, flue gas 1201 enters the inlet of system 1200. This flue gas 1201 contains 10% CO by volume and has a temperature of 140 degrees Celsius. After entering system 1200, flue gas 1201 passes through fan 1202. This fan 1202 may be required to overcome pressure drops that occur in the piping and downstream processing.

[0101] In this example, two operations were performed in the CO2 capture system 1200.

[0102] In a first operation, the flue gas 1201 is cooled in a direct contact cooler (DCC) 1203 using water circulated through a DCC drum 1204, a circulation pump 1205, and a heat exchanger 1206. The DCC 1203 may be an RPB. The water used for cooling is cooled in the heat exchanger 1206. Excess condensate in the flue gas 1201 is discharged through an outlet 1207.

[0103] In a second operation, SOx column 1208 is used to remove acid gases such as SOx and NOx by alkaline scrubbing. SOx column 1208 may be an RPB. Water is circulated through the SOx column drum 1209, circulation pump 1210, and cooler 1211. An alkaline component 1212 is dosed to the water using pump 1213. The water contacts flue gas 1201 in SOx column 1208. Excess liquid is discharged from the circulation through outlet 1214.

[0104] The flue gas 1201 then passes through a CO2 absorber 1215, which may be an RPB. The flue gas 1201 is in countercurrent contact with a CO2 capture solvent. The CO2 absorber 1215 contains two packed beds within which the flue gas 1201 and the CO2 capture solvent are in contact. Between these packed beds, the temperature of the CO2 capture solvent is controlled by an intercooling heat exchanger, which is comprised of heat exchanger 1218, pump 1217, and drum 1216. The flue gas 1201 leaves the CO2 absorber depleted in CO2 and passes to a water wash 1219, which may be an RPB. The CO2 capture solvent leaves the CO2 absorber enriched in CO2 and passes to a CO2-rich solvent drum 1220. The CO2 capture solvent passes from this drum 1220 via a CO2-rich solvent boost pump 1221 into an O2 remover 1222.

[0105] In this example, CO2-depleted flue gas 1201 enters a water wash unit 1219. In the water wash unit 1219, the flue gas 1201 is contacted with two streams of water circulating through two water wash packings 1223, 1226 (arranged in series). The water passing through each packing 1223, 1226 is circulated by wash water pumps 1224, 1227, cooled in heat exchangers 1225, 1228, and then returned to the water wash unit 1219. The treated flue gas 1201 is discharged through an outlet 1229.

[0106] In this example, the CO2 capture solvent enters the O2 remover 1222 at a CO2-rich content. The O2 remover 1222 may be an RPB. In the O2 remover 1222, the CO2 capture solvent contacts a CO2 stream. The CO2 stream and entrained O2 are returned to the CO2 absorber 1215. After the O2 is removed, the CO2 capture solvent is pumped through a surge drum 1230, a CO2-rich solvent pump 1231, and a crossover heat exchanger 1232 into the stripper 1233. A CO2-lean solvent cooler 1242 may be located between the crossover heat exchanger 1232 and the CO2 absorber 1215.

[0107] In this example, steam generated in reboiler 1238 is supplied to stripper 1233 and used to heat the CO2 capture solvent and strip CO2 therefrom. Stripper 1233 may be an RPB. The steam, consisting of water vapor, vaporized solvent components, and CO2 gas, enters reflux exchanger 1234 from stripper 1233. There, the temperature of the steam drops from 120°C to 40°C, causing the water vapor and solvent components to condense into a liquid phase. The water vapor is then passed to reflux tank 1235, where gaseous CO2 is liberated from the liquid components. The liquid components are then returned to the CO2 capture process as reflux. The reflux is pumped to stripper 1233 by reflux pump 1236, while CO2, with a purity greater than 95%, exits reflux exchanger 1234 through outlet 1237. This stream of CO2 is returned to the O2 removal unit 1222 and is used as a purge gas in the O2 removal process.

[0108] In this example, the operating pressure of the stripper was 1 bar(g), the operating pressure of the steam fed to the reboiler (saturated steam pressure) was 3.5 bar(g), and the design pressure of the stripper, reboiler, reflux exchanger, reflux tank, steam system, and condensate system was 10 bar(g).

[0109] In this example, the CO2 capture solvent (no longer containing CO2) exits the stripper 1233, passes through a reboiler 1238, is pressurized using a CO2 lean solvent pump 1239, passes through a crossover heat exchanger 1232, and returns to the CO2 absorber 1215 via a CO2 lean solvent cooler 1242.

[0110] In this example, the DCC 1203, SOx tower 1208, and water wash unit 1219 are located in separate RPB shafts. Experimental Example 8: Selection of size of facility using RPB for treatment

[0111] In this example, process simulation software such as ProTreat® (by Optimized Gas Treating) was used to size the conventional fixed packed bed, while the methodology of Example 5 was used to size the RPB-based equipment.

[0112] Table 7 compares the dimensions of a facility capable of recovering 10 t of CO2 per day from flue gas with a CO2 concentration of 10% by volume between the case of using an RPB and the case of using a conventional fixed packed bed. [Table 7]

[0113] Comparing the dimensional data of the equipment using RPB with that of the equipment using a conventional fixed packed bed shown in Table 7, the volume of the packed bed required to achieve a CO2 capture rate of 90% is reduced by an order of magnitude or nearly so for the equipment using RPB. Experimental Example 9: Selection of the size of auxiliary processing equipment in a system including an RPB

[0114] In this example, process simulation software such as ProTreat® (by Optimized Gas Treating) was used to size the equipment according to Example 8 utilizing the RPB.

[0115] Tables 8, 9, and 10 show the specifications of the equipment included in a plant capable of capturing 10 t of CO2 per day from flue gas containing 10% CO2 by volume using an RPB. In particular, these tables show the specifications of the pumps, fans, heat exchangers, and tanks required for such a plant. [Table 8] [Table 9] [Table 10]

[0116] As the above embodiments demonstrate, the volume of packed bed required for an RPB-based facility to achieve 90% CO2 capture has been reduced by an order of magnitude or nearly so. This is beneficial because it reduces capital investment and size while still achieving comparable or better CO2 capture performance. As described in the above embodiments, the use of RPBs offers benefits over known systems.

[0117] Although the embodiments of the present invention and its advantageous effects have been described in detail above, it should be understood that various changes, substitutions, and alterations can be made to the embodiments without departing from the scope of the invention as defined by the appended claims. Furthermore, the above description is not intended to limit the examples of processes, machines, methods, components of matter, methods, and steps utilized in the present invention to the specific examples described in the specification. As will be readily understood from the disclosure herein, existing or subsequent processes, machines, methods, components of matter, methods, or steps that perform substantially the same function or provide substantially the same effect as the above examples may be utilized in the present invention. Therefore, it is intended by the appended claims that such processes, machines, methods, components of matter, methods, or steps fall within the scope of the present invention.

[0118] When used in this specification and the appended claims, the words "comprise," "have," "include," and their variations mean that certain features, steps, or numbers are included, but these words should not be interpreted as excluding the presence of other features, steps, or elements.

[0119] Where appropriate, features that are expressed in a particular form in the above description, the appended claims, or the accompanying drawings, or that are disclosed as means for performing a particular function, or as a method or process for providing a particular effect, may be used separately or in various combinations with other features to realize the invention in various forms.

Claims

1. Carbon dioxide (CO 2 ) is recovered, passing the flue gas through at least one absorber including a rotating packed bed (RPB), wherein a solvent provided through an inner periphery of the at least one absorber moves toward an outer periphery of the at least one absorber, and the solvent reacts with the flue gas flowing in a counter-direction to remove CO2 from the flue gas and form a CO2-rich solvent; passing the CO2-rich solvent through a stripper, the stripper acting to strip CO2 from the CO2-rich solvent to form a CO2-lean solvent; It is equipped with The peeling device is a peeling device including an RPB. A process characterized by:

2. CO for the purpose of recycling the solvent in the process. 2 and thermally regenerating the solvent that has reacted with The process of claim 1 further comprising:

3. scrubbing the flue gas with water and / or acid to remove any remaining solvent in the flue gas; Further provided with Either or both of the water wash and pickling are carried out in a separate RPB. The process of claim 1.

4. The process of claim 1 , wherein the housing of the RPB is mounted on a rotatable disk.

5. The CO 2 supplying the flue gas to an absorber, the flue gas comprising: feeding the flue gas to two, three, four, five, or six absorbers, including RPBs; The process of claim 1 , comprising:

6. 6. The process of claim 5, wherein the two, three, four, five, or six absorbers are arranged in series on a common shaft.

7. The CO 2 10. The process of claim 1, wherein lean solvent is reintroduced into the absorber.

8. CO released from the absorber 2 The rich solvent is then added to the RPB or fixed packed bed containing 2 The O dissolved in the solvent is passed through a removal device. 2 removing from the solvent. The process of claim 1 further comprising:

9. The CO 2 Rich solvent 2 The solvent is passed through a removal device to remove O 2 In the step of removing O present in the solvent, 2 The process of claim 8, wherein the process removes 90% or more of the above.

10. Each RPB is The radius is in the range of 0.2 m to 1.25 m, or 0.2 m to 0.8 m; the axial length is in the range of 0.02 m to 1.0 m, or 0.2 m to 0.6 m; The volume is 0.04 m 3 From 4.9m 3 up to, or 0.04 m 3 From 0.6m 3 The process of claim 1 , wherein the range is from

11. the solvent comprises a tertiary amine, a sterically hindered amine, a polyamine, a carbonate buffer, and / or water; The concentration of the water is set in the range of 10% by weight to 70% by weight. The process of claim 1.

12. 12. The process of claim 11, wherein the viscosity of the solvent is set in the range of 1 cP to 10 cP.

13. The solvent is as tertiary amines, N-methyl-diethanolamine and / or 2-(diethylamino)ethanol; sterically hindered amines include 2-amino-2-ethyl-1,3-propanediol, 2-amino-2-hydroxymethyl-1,3-propanediol, and / or 2-amino-2-methyl-1-propanol; The polyamine includes 2-piperazine-1-ethylamine and / or 1-(2-hydroxyethyl)piperazine; potassium carbonate as a carbonate buffer; and / or Contains deionized water, The process of claim 11.

14. The solvent is containing amino-2-methyl-1-propanol as the sterically hindered amino alcohol, containing aminoethylpiperazine as a polyamine, and Contains water, The process of claim 11.

15. The method of claim 14, wherein the flue gas containing CO 2 is supplied to at least one direct contact cooler (DCC) comprising a rotating packed bed (RPB) to cool the flue gas.

2. The process of claim 1, further comprising:

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