Patent Application
20140116252
The proposed invention relates to a gas/liquid contacting vessel for treatment of a gas stream, and to a flue gas treatment system for removal of carbon dioxide (CO2) from a flue gas using a liquid absorbent.
In the combustion of a fuel, such as coal, oil, peat, waste, etc., in a combustion plant, such as those associated with boiler systems for providing steam to a power plant, a hot process gas (or flue gas) is generated. Such a flue gas will often contain, among other things, carbon dioxide (CO2). The negative environmental effects of releasing carbon dioxide to the atmosphere have been widely recognized, and have resulted in the development of processes adapted for removing carbon dioxide from the flue gas generated in the combustion of the above mentioned fuels.
Many of the developed flue gas cleaning processes involve contacting the flue gas with an absorbent liquid capable of absorbing CO2 from the gas to produce a flue gas which is lean in CO2 and an absorbent which is rich in CO2. In processes used for industrial separation of CO2, liquid solutions or slurries comprising amine compounds, e.g. monoethanolamine (MEA), or ammonia are commonly used as absorbents. A CO2 absorber is employed to establish suitable conditions (temperature, pressure, turbulence, etc.) for chemical absorption of CO2 into the absorbent from a mixed gas stream. The “rich” absorbent containing absorbed CO2 is subsequently regenerated, whereby absorbed CO2 is separated from the absorbent, and the regenerated “lean” absorbent is then reused in the CO2 absorption process. Thus, a circulating absorbent stream is formed. Regeneration is generally achieved by heating the absorbent in a reboiler to a temperature at which CO2 is released from the absorbent.
Another type of flue gas treatment process, is the chilled ammonia process. The chilled ammonia based systems and processes (CAP) provide a relatively low cost means for capturing and removing CO2 from a gas stream, such as, for example, a post combustion flue gas stream. An example of such a system and process has previously been disclosed in the published international patent application WO 2006/022885 titled “Ultra Cleaning of Combustion Gas Including the Removal of CO2”. The general principle of the chilled ammonia process resembles that of the amine based process described above. The term “chilled” refers to the operating temperature of the absorber vessel in the chilled ammonia process, which is generally in the range of 0-20° C., and preferably in the range of 0-10° C. In the process described in WO 2006/022885, the absorption of CO2 from a flue gas stream is achieved by contacting a chilled ammonia ionic solution or slurry in an absorber with a flue gas stream containing CO2. The ionic solution containing absorbed CO2 is subsequently regenerated by heating under increased pressure, whereby CO2 is removed from the ionic solution, and the regenerated ionic solution can be reused in the CO2 absorption process.
The absorbers and regenerators in both of the above described techniques rely on solvent contacting flue gas or steam, in order to capture and release CO2, respectively. In order for the necessary mass transfer to occur efficiently, the packing in the columns must be adequately wetted, so as to prevent breakthrough of flue gas or steam. The design of these columns draws upon experience in the chemical industry, whereby the majority of operation occurs at or near the “design point”.
Many industrial combustion processes, however, operate at varying loads, resulting in varying flue gas flow rates. One example is the combined cycle power plant (CCPP). One of the large advantages of CCPP is the operational flexibility, in which the entire load range can be covered within short periods of time. For this reason, CCPP are viewed as a means of complementing the highly variable power output from more unpredictable renewable sources (e.g. wind, solar). The flue gas flow rate is a strong function of the gas turbine load, with the value almost halving between 100% and 50% gas turbine load. When implementing a CO2 absorption system in a CCPP, the varying flue gas flow rate is problematic because the absorber and regenerator columns in the absorption system are rarely operated near their design point, thereby resulting in both technical and financial inefficiency. In particular, at low loads, the fluid flow rate may be too small to uniformly wet the packing, thereby permitting breakthrough of the flue gas.
One approach to overcome this problem is by using multiple trains (consisting of several smaller units), but this is an expensive solution that could be difficult to control.
It is an object of the present invention to alleviate at least one of the above mentioned problems.
According to aspects illustrated herein, there is provided a gas/liquid contacting vessel for treatment of a gas stream at varying mass flow rates, said vessel comprising
at least two distinct gas/liquid contacting compartments separated from each other by a substantially vertical partition, each compartment having a gas inlet and a liquid outlet near a bottom end thereof and a gas outlet and a liquid inlet near a top end thereof, and a mass transfer device arranged between said bottom end and top end,
wherein one of said compartments is operable for gas/liquid contacting independently of another of said compartments.
In other words, it is proposed to utilize a single column that is split into two or more substantially vertical compartments, to which the incoming fluids and gases can be distributed according to the mass flow rate of the flue gas. This allows for the ratio of flow rate to residence time (liquid-to-gas ratio) to be maintained closer to a predetermined value than possible with conventional single compartment vessels. This means the operation can be conducted closer to the design point and that CO2 capture efficiency can be kept high across a larger load range. Furthermore, the liquid absorbent flow rate can be optimized, resulting in lower liquid absorbent consumption. Also, in systems utilizing regeneration of the liquid absorbent by heating, this in turn leads to reduced regenerator steam consumption when operating the system at partial load.
A gas/liquid contacting vessel, such as an absorber vessel, generally comprises a substantially cylindrical container, wherein at least a portion of the inner volume of the container is filled with a mass transfer device operative for facilitating contact between a gas and a liquid. The gas/liquid contacting vessel is commonly arranged in a substantially vertical orientation and configured to receive a liquid through a liquid inlet near the top of the vessel and a gas through a gas inlet near the bottom of the vessel. During operation of the vessel, a gas fed through the gas inlet and a liquid fed through the liquid inlet are brought into contact with each other in the mass transfer device.
The bottom end generally refers to a section of the vessel below a mass transfer device, whereas the top end generally refers to a section of the vessel above a mass transfer device. The gas inlet and liquid outlet may generally be positioned below the mass transfer device, and the gas outlet and liquid inlet may generally be positioned above the mass transfer device. The gas inlet may be positioned between the liquid outlet and the mass transfer device.
According to some embodiments, all of the gas inlets of the gas/liquid contacting compartments are fluidly connectable to a common gas source.
According to some embodiments, all of the liquid inlets of the gas/liquid contacting compartments are fluidly connectable to a common liquid source.
According to some embodiments, the gas/liquid contacting vessel comprises shut-off means, whereby gas and/or liquid flow to a gas/liquid contacting compartment can be blocked independently of another of said compartments.
According to some embodiments, the mass transfer devices comprised packed beds.
According to some embodiments, the gas/liquid contacting vessel defines an inner volume having a circular horizontal cross-section, and the at least two distinct gas/liquid contacting compartments are defined by an inside wall of the vessel and one or more substantially vertical walls extending throughout a substantially vertical cross-section of the inner volume of the vessel.
According to other embodiments, the gas/liquid contacting vessel defines an inner volume having a circular horizontal cross-section, and at least one of the distinct gas/liquid contacting compartments is defined by a tubular wall extending substantially vertically throughout the inner volume of the vessel.
According to some embodiments, the gas/liquid contacting vessel has two gas/liquid contacting compartments. For practical reasons, two gas/liquid contacting compartments are often sufficient for achieving a substantially improved efficiency of the vessel during large variations in the mass flow rate of the flue gas. Two gas/liquid contacting compartments also involve a minimum of adaption of present vessel designs for implementation. An additional advantage is the potential use of the vessel in a combustion plant utilizing, or prepared for, flue gas recirculation (FGR). In combustion plants utilizing FGR, often about 50 percent of the flue gas produced is recirculated back to the combustion process, resulting in an about 50 percent decrease in the mass flow rate of the flue gas to the flue gas treatment system. Thus, a gas/liquid contacting vessel having two gas/liquid contacting compartments may easily be adapted for operation with flue gas recirculation.
According to other aspects illustrated herein, there is provided a flue gas treatment system for removal of carbon dioxide (CO2) from a flue gas using a liquid absorbent, comprising
a CO2 absorber vessel and
an absorbent regenerator vessel,
wherein the CO2 absorber vessel comprises a gas/liquid contacting vessel for treatment of a gas stream at varying mass flow rates, said vessel comprising
at least two distinct gas/liquid contacting compartments separated from each other by a substantially vertical partition, each compartment having a gas inlet and a liquid outlet near a bottom end and a gas outlet and a liquid inlet near a top end, and a mass transfer device arranged between said bottom end and top end,
wherein one of said compartments is operable for gas/liquid contacting independently of another of said compartments.
The gas/liquid contacting vessel of the flue gas treatment system may be further defined as described above with reference to the first aspect.
According to some embodiments of the flue gas treatment system, each of said CO2 absorber vessel and said absorbent regenerator vessel comprise a gas/liquid contacting vessel as defined above.
According to some embodiments, said CO2 absorber vessel and said absorbent regenerator vessel each comprises two gas/liquid contacting compartments.
According to some embodiments, the flue gas treatment system is selected from the group consisting of an amine based gas treatment system and an ammonia based gas treatment system, such as a chilled ammonia based gas treatment system.
According to other aspects illustrated herein, there is provided a combined cycle power plant comprising a gas/liquid contacting vessel or a flue gas treatment system according to the aspects described above.
According to other aspects illustrated herein, there is provided the use of a gas/liquid contacting vessel or a flue gas treatment system according to the aspects described above for removal of CO2 from a flue gas stream.
According to other aspects illustrated herein, there is provided a method of operating a gas/liquid contacting vessel according to the aspects described above, comprising
According to some embodiments, the gas/liquid contacting vessel is a CO2 absorber vessel of a flue gas treatment system according to the aspects described above.
According to some embodiments, the flue gas stream to be treated in the method is produced in a combustion plant utilizing, or prepared for, flue gas recirculation.
The above described and other features are exemplified by the following figures and detailed description. Further objects and features of the present invention will be apparent from the description and the claims.
Referring now to the figures, which are exemplary embodiments, and wherein the like elements are numbered alike:
a-3e are schematic horizontal cross section views of gas/liquid contacting vessels having different substantially vertical partition configurations.
Herein, the inventive concept as applied to the absorber and/or regenerator vessels of an amine absorption based CO2 capture system will be described in detail with reference to the drawings. It is realized that the inventive concept may also be applied to other gas/liquid contacting components of a flue gas treatment system, for example water wash units for removal of trace contaminants, strippers and direct contact coolers/heaters.
The term “gas”, as used herein, is intended to encompass gases as well as liquids in vapor form. Specifically, the gas processed in the gas/liquid contacting vessels described herein may be a gas, such as CO2, or a liquid, for example water, in vapor form.
The term “in fluid contact with” with regard to two components of a
system, one component being upstream of the other, then during the normal operation of the system, essentially all of the fluid passing through
the system passes first through the upstream component and then through
the other component. The terms “fluid contact” and “fluid communication” as used herein are synonymous.
The term “configured to receive”, as used herein, means that the system may comprise piping, tubing, fittings and/or other similar means for fluid transport, as well as suitable pumps or other similar liquid displacement devices, such that a fluid may be transported from one position to another.
The gas/liquid contacting vessel 100 comprises a substantially vertically oriented substantially cylindrical container, defining an inner volume having a circular horizontal cross-section. The inner volume of the gas/liquid contacting vessel 100 is divided into two distinct gas/liquid contacting compartments 101a, 101b by an inside wall 103 of the vessel, i.e. an inner surface of an exterior wall of the vessel, and one or more substantially vertical walls 102 extending throughout a substantially vertical cross-section of the inner volume of the vessel. The gas/liquid contacting vessel 100 and substantially vertical partition(s) can be of any suitable construction material, e.g. stainless steel, as will be recognized by a person skilled in the art. The partition(s) may be attached to the inside walls, e.g. by welding or other suitable techniques, such that the partition(s) together with the inside walls of the vessel define the distinct gas/liquid contacting compartments.
The gas/liquid contacting compartments 101a, 101b are distinct, meaning that gas and or liquid in one compartment may be prevented from entering the other compartment. This allows one of the two compartments to be operable for gas/liquid contacting independently of the other compartment.
Each gas/liquid contacting compartment 101a, 101b has a gas inlet 104a, 104b arranged near a bottom end of the compartment, which is configured to receive a gas stream from a gas duct 105, and a gas outlet 106a, 106b arranged near a top end of the compartment configured to discharge the gas stream from the compartment via a gas duct 107. Each gas/liquid contacting compartment 101a, 101b further has a liquid inlet 108a, 108b arranged near a top end of the compartment, which is configured to receive a liquid absorbent from a liquid absorbent supply duct 109, and a liquid outlet 110a, 110b arranged near a bottom end of the compartment configured to discharge the liquid absorbent from the compartment to a liquid discharge duct 117.
Each gas/liquid contacting compartment 101a, 101b further comprises a mass transfer device 111a, 111b operative for facilitating contact between a gas and a liquid, arranged between said gas inlet 104a, 104b and said liquid inlet 108a, 108b.
The mass transfer device 111a, 111b is configured to provide efficient contact between a gas stream and an liquid stream fed through the respective gas and liquid inlets of the compartment. The mass transfer device may, e.g., comprise one or more commonly known structured or random packing materials, or a combination thereof, provided in the form of an absorption column, such as a packed bed column. The mass transfer device may preferably be arranged to operate in countercurrent flow mode. As an example, the mass transfer device may comprise an absorption column arranged to operate in countercurrent flow mode, wherein the gas stream is fed near a bottom end of the compartment, below the mass transfer device, and a liquid absorbent is fed near a top end of the compartment, above the mass transfer device, such that the gas stream is brought into contact with the liquid absorbent as it rises up through the column. The gas stream then leaves the column near the top of the compartment, while the liquid absorbent leaves the column near the bottom of the compartment.
Each gas/liquid contacting compartment 101a, 101b may also be provided with a liquid distribution device 112a, 112b, e.g. comprising an array of spray heads, in liquid connection with the liquid inlet 108a, 108b and operative for distributing a liquid fed via the liquid inlet evenly onto the mass transfer device 111a, 111b.
The gas/liquid contacting compartments 101a, 101b described with reference to
In order to enable independent operation of one or more of the gas/liquid contacting compartments 101a, 101b, the vessel comprises shut-off means, whereby gas and/or liquid flow to one of the a gas/liquid contacting compartments can be blocked independently of the other of said compartments.
Referring to the embodiment of
The shut-off means, e.g. fluid valves, may be arranged on the gas and/or liquid supply ducts 105, 109 as indicated in
The regenerator vessel 200 comprises a substantially vertically oriented substantially cylindrical container, defining an inner volume having a circular horizontal cross-section. The inner volume of the gas/liquid contacting vessel 200 is divided into two distinct gas/liquid contacting compartments 201a and 201b by an inside wall 203 of the vessel, i.e. an inner surface of an exterior wall of the vessel, and one or more substantially vertical walls 202 extending throughout a substantially vertical cross-section of the inner volume of the vessel. The gas/liquid contacting vessel 200 and substantially vertical partition(s) can be of any suitable construction material, e.g. stainless steel, as will be recognized by a person skilled in the art. The partition(s) may be attached to the inside walls, e.g. by welding or other suitable techniques, such that the partition(s) together with the inside walls of the vessel define the distinct gas/liquid contacting compartments. The regenerator vessel and gas/liquid contacting compartments may optionally be designed for operation at increased pressure, such as pressures in the range of 1 to 50 bar gauge or in the range of 10 to 30 bar gauge.
The gas/liquid contacting compartments 201a, 201b are distinct, meaning that gas and or liquid in one compartment may be prevented from entering the other compartment. This allows one of the compartments 201a or 201b to be operable for gas/liquid contacting independently of the other compartment.
Each gas/liquid contacting compartment 201a, 201b has a gas inlet 204a, 204b arranged near a bottom end of the compartment, which is configured to receive a gas stream (i.e. steam) from the reboiler 220, and a gas outlet 206a, 206b arranged near a top end of the compartment configured to discharge released CO2 and residual water vapor from the compartment. Each gas/liquid contacting compartment further has a liquid inlet 208a, 208b arranged near a top end of the compartment, which is configured to receive a CO2 rich liquid absorbent from the absorber vessel via a liquid absorbent supply duct 209, and a liquid outlet 210a, 210b arranged near a bottom end of the compartment configured to discharge the CO2 lean liquid absorbent from the compartment to a liquid discharge duct 217. One portion of the discharged CO2 lean liquid absorbent may be returned to the absorber vessel via liquid duct 218 for absorbing more CO2, while another portion is directed via liquid duct 219 to the reboiler 220 for production of steam for the regeneration process.
Each gas/liquid contacting compartment 201a, 201b further comprises a mass transfer device 211a, 211b, arranged between said gas inlet 204a, 204b and said liquid inlet 208a, 208b, and operative for facilitating contact between the steam produced by the reboiler 220 and the CO2 rich liquid absorbent.
The mass transfer device 211a, 211b may, e.g., comprise one or more commonly known structured or random packing materials, or a combination thereof, provided in the form of an absorption column, such as a packed bed column. The mass transfer device may preferably be arranged to operate in countercurrent flow mode. As an example, the mass transfer device may comprise an absorption column arranged to operate in countercurrent flow mode, wherein the steam from the reboiler is fed near a bottom end of the compartment, below the mass transfer device, and the CO2 rich liquid absorbent is fed near a top end of the compartment, above the mass transfer device, such that the steam is brought into contact with the liquid absorbent as it rises up through the column.
Each gas/liquid contacting compartment 201a, 201b may also be provided with a liquid distribution device 212a, 212b, e.g. comprising an array of spray heads, in liquid connection with the liquid inlet 208a, 208b and operative for distributing a liquid fed via the liquid inlet evenly onto the mass transfer device 211a, 211b.
In order to enable independent operation of one or more of the gas/liquid contacting compartments 201a, 201b, the vessel comprises shut-off means, whereby gas and/or liquid flow to one of the a gas/liquid contacting compartments can be blocked independently of the other of said compartments.
Referring to the embodiment of
The shut-off means, e.g. fluid valves, may be arranged on the gas and/or liquid supply ducts 205, 209 as indicated in
a represents a gas/liquid contacting vessel having two gas/liquid contacting compartments, a and b, each defined by an inside wall of the vessel and a substantially vertical wall extending throughout a substantially vertical cross-section plane of the inner volume of the vessel. The two compartments a and b may preferably be volumetrically equal, but can also be volumetrically different.
b represents a gas/liquid contacting vessel having four gas/liquid contacting compartments, a-d, each defined by an inside wall of the vessel and a two substantially vertical walls extending throughout two different substantially vertical cross-section planes of the inner volume of the vessel. The four compartments a-d may preferably be volumetrically equal, but can also be volumetrically different.
c represents a gas/liquid contacting vessel having eight gas/liquid contacting compartments, a-h, each defined by an inside wall of the vessel and a two substantially vertical walls extending throughout two different substantially vertical cross-section planes of the inner volume of the vessel. The eight compartments a-h may preferably be volumetrically equal, but can also be volumetrically different.
d represents a gas/liquid contacting vessel having a first gas/liquid contacting compartment, a, defined by a tubular wall extending substantially vertically throughout the inner volume of the vessel and a second gas/liquid contacting compartment, b, defined by an outside surface of the first gas/liquid contacting compartment and an inside wall of the vessel.
e represents a gas/liquid contacting vessel having a plurality of distinct gas/liquid contacting compartments, each defined by a tubular wall extending substantially vertically throughout the inner volume of the vessel.
A gas/liquid contacting vessel as described above with reference to
The amine based CO2 absorption process is based on the chemistry of the amine-CO2-H2O system and the ability of the amine solution to absorb CO2 at low temperature (approx. 45° C.) and to release the CO2 at moderately elevated temperature (approx. 125° C.). Examples of amine compounds commonly used in absorption of CO2 include, but are not limited to, monoethanolamine (MEA), diethanolamine (DEA) and methyldiethanolamine (MDEA). CO2 and water produce carbonic acid which reacts with the amine solution in the absorption column, forming chemical compounds (carbonates) and resulting in the removal of CO2 from the gaseous stream. At higher temperatures, the reaction is reversed to release CO2 in a concentrated form.
When each of the absorber vessel 100 and the regenerator vessel 200 of an absorption based carbon dioxide (CO2) capture system comprise gas/liquid contacting vessels having at least two distinct gas/liquid contacting compartments, the absorber vessel and the regenerator vessel may preferably have the same number of gas/liquid contacting compartments.
When one or each of the absorber vessel and the regenerator vessel of the absorption based carbon dioxide (CO2) capture system comprise gas/liquid contacting vessels having at least two distinct gas/liquid contacting compartments, the capacity of the flue gas treatment system can be adjusted according to the mass flow rate of the incoming flue gas to be treated. This allows for the ratio of flow rate to residence time (liquid-to-gas ratio) to be maintained closer to a predetermined value than possible with conventional single compartment vessels. This means the operation can be conducted closer to the design point and that CO2 capture efficiency can be kept high across a larger load range. Furthermore, the liquid absorbent flow rate can be optimized, which in turn leads to reduced regenerator steam consumption when operating the system at partial load.
While the invention has been described with reference to a number of preferred embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from the essential scope thereof. Therefore, it is intended that the invention not be limited to the particular embodiments disclosed as the best mode contemplated for carrying out this invention, but that the invention will include all embodiments falling within the scope of the appended claims. Moreover, the use of the terms first, second, etc. do not denote any order or importance, but rather the terms first, second, etc. are used to distinguish one element from another.
| Number | Date | Country | Kind |
|---|---|---|---|
| 11164420.9 | May 2011 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/IB2012/000844 | 5/1/2012 | WO | 00 | 1/14/2014 |
