Patent Application
20140193319
This application claims priority to European application 13150691.7 filed Jan. 9, 2013, the contents of which are hereby incorporated in its entirety.
The present invention relates to flue gas cleaning methods and systems employing the chilled ammonia process (CAP) for removal of carbon dioxide from process gases.
In the combustion of a fuel, such as coal, oil, peat, waste, etc., in a combustion plant, such as a power plant, a hot process gas is generated, such a hot process gas, often referred to as a flue gas, containing, among other components, 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 hot process gas generated in the combustion of the above mentioned fuels. There are also other industries that generate large amounts of CO2, including for example in the cement industry and steel industry.
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 term “chilled” refers to the operating temperature of the CO2 absorber 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 ammoniated solution or slurry in an absorber with a flue gas stream containing CO2. The ammoniated solution containing absorbed CO2 is subsequently regenerated by heating under increased pressure, whereby CO2 is removed from the solution, and the regenerated solution can be reused in the CO2 absorption process.
US2008/0178733 presents a gas cleaning system having a combined cooling and cleaning system comprising a first gas-liquid contacting device located upstream of the CO2 absorber and operative for cooling the process gas by means of a cooling liquid, and for absorbing into the cooling liquid sulfur dioxide of the process gas, such that a cooling liquid containing sulfate is obtained. The combined cooling and cleaning system further comprises a second gas-liquid contacting device located downstream of the CO2 absorber and operative for removing ammonia from the process gas, which has been treated in the CO2 absorber, by means of bringing the process gas containing ammonia into contact with the cooling liquid containing sulfate.
The sulfate of the cooling liquid and the ammonia removed from the flue gas of the cooling liquid is sometimes used in the production of an ammonium sulfate by-product useful as fertilizer.
The gas cleaning system of US2008/0178733 is well adapted for the treatment of relatively clean CO2 rich flue gas streams (low in e.g. particulate material and heavy metals) as produced, e.g. by modern power plants combusting higher quality fuels. However, industrial processes such as cement or steel production, burning lower quality coal or waste may generate flue gases with a higher acid, particulate material and/or heavy metal content than characteristic of most power plants. Although most cement plants utilize flue gas quench coolers combined with electrostatic precipitators to reduce particle and heavy metal concentrations, considerable residual levels remain in the flue gas. The remaining particulate material and heavy metal content can contaminate the cooling liquid, complicating the intended use the liquid by-product.
An object of the present invention is to provide an improved chilled ammonia process and system for cleaning a process gas containing carbon dioxide and contaminants, such as sulfur dioxide, heavy metals and particulate material.
According to aspects illustrated herein, there is provided a method of cleaning a process gas containing carbon dioxide and contaminants, said method comprising the steps of:
According to some embodiments, the method further comprises the steps of:
The first stage of the cooling and cleaning system of the prior art chilled ammonia process flow scheme, as described in US2008/0178733, first applies a washing step capturing SO2 using a solution of dissolved ammonia and SO2 forming sulfite which depending on the availability of dissolved O2 oxidizes to form sulfate producing an ammonia sulfate solution intended for use as fertilizer. Heavy metals or acidic components entering the chilled ammonia process plant via the flue gas have a tendency to accumulate in the first stage of the cooling and cleaning system causing problems with contamination of the liquid by-product, ultimately making it unsuitable for use as fertilizer. The cooling and cleaning system of US2008/0178733 also considers use of the ammonia sulfate solution to capture SO2 in connection with the cooling step.
The gas cleaning method and system in accordance with aspects described herein comprise a modification of the prior art chilled ammonia process flow scheme, which improves the operation of the chilled ammonia process when applied to a process gas having a higher acid, particulate material and/or heavy metal content. This is advantageous in cement or steel manufacturing facilities which of the produce flue gases having high content of for example sulfur dioxide, heavy metals and particulate material.
To avoid complications with contamination of the ammonium sulfate by-product, an alkaline cleaning step is introduced to heavy metal and particulate content of the process gas and to remove residual SO2 before the gas enters the chilled ammonia process cooling and cleaning system. Particulate material and other contaminants may be captured in a relatively low volume of liquid in the alkaline cleaning step, which facilitates work-up, recycling and/or waste management of the formed solution/slurry.
The term “alkaline”, as used herein in connection with the “alkaline solution or slurry” and “alkaline cleaning” generally refers to an aqueous solution having a pH value above 7.
According to some embodiments, the alkaline solution or slurry comprises NaOH or Ca(OH)2.
According to some embodiments, the alkaline solution or slurry has a pH-value of 8 or higher.
The present inventors have also found that the resulting liquid slurry, low in volume flow and having a high content of particulate material and heavy metals can advantageously be returned, at least partly, to the process in which the process gas was generated or sent for waste treatment or disposal. As an example, in the case of cement production, the solids from the resulting slurry may be separated (e.g. by a hydrocyclone, a centrifuge or a filter) and returned to the kiln. Volatile components from the separated solids exit the kiln via the flue gas while the bulk of the heavy metals remain bound to solids in the kiln and exit with the cement clinker. Returning the solids from the alkaline cleaning step to the process in which the process gas was generated can significantly reduce the overall waste stream from the system.
The introduction of an alkaline cleaning in accordance with aspects described herein is advantageous in that it allows reintegration of heavy metals and acidic components back into the industrial process, at the same time preventing contamination of the chilled ammonia process by-products, e.g. ammonium sulfate. The alkaline cleaning system is further advantageous in that it provides efficient removal of SO2 at increased process temperatures without the draw backs of NH3 or SO2 losses associated with washing steps using ammonia sulfate solution. The alkaline cleaning system as described herein can readily be implemented into existing chilled ammonia systems.
The alkaline cleaning is preferably performed at a temperature above the dew point of the process gas in order to avoid bulk condensation of water vapor in the process gas leading to dilution of the alkaline solution or slurry. For this reason, the base or caustic compound of the alkaline solution or slurry should be selected among compounds having sufficiently low vapor pressure at the operating temperature of the alkaline cleaning step, to avoid loss of the base or caustic compound to the process gas. Specifically, ammonia is not suitable as the base or caustic compound in accordance with the aspects described herein due to its high vapor pressure at the relevant operating temperatures leading to contamination of down-stream systems, e.g. the cooling system.
According to some embodiments, the step of bringing the process gas into direct contact with an alkaline solution or slurry is performed at a temperature above the dew point of the process gas.
According to some embodiments, the step of bringing the process gas into direct contact with an alkaline solution or slurry does not involve any substantial condensation of water vapor present in the process gas.
The alkaline cleaning is preferably conducted independently of the other scrubbing or washing operations of the chilled ammonia process, specifically the cooling step, the CO2 absorption, the optional water wash, and ammonia removal step. This means that the scrubbing or washing liquids, specifically, the cooling liquid, the ammoniated solution or slurry, and wash liquids of the ammonia removal and optional water wash steps, or components thereof, are not utilized in the alkaline cleaning step/system. Conducting the alkaline cleaning independently of the other scrubbing or washing operations of the chilled ammonia process allows the parameters (e.g. temperature, volume flow, pH and solids content) of the alkaline solution or slurry to be optimized independently. This allows the alkaline cleaning to be efficiently performed at a low volume flow with high solids content, and at a relatively high temperature and pH value.
According to some embodiments, the contaminants include sulfur dioxide, heavy metals and particulate material.
According to some embodiments, the process gas is generated by a power plant, a cement production facility or a steel production facility.
Industrial processes such as cement and steel production burning lower quality coal (or waste) may generate flue gases with a higher acid or heavy metal content than characteristic of most power plants.
According to some embodiments, the process gas is generated by burning of a lower quality fuel, such as low quality coal or waste.
According to some embodiments, the process gas is generated by a cement production facility or a steel production facility. Implementation of the alkaline cleaning in accordance with aspects described herein is advantageous in cement or a steel production facilities since in such facilities, the alkaline solution or slurry containing heavy metals and sulfur dioxide captured from the process gas can be readily returned to the process in which the process gas was generated. According to some embodiments, the process gas is generated by a cement production facility.
According to some embodiments, the alkaline solution or slurry containing contaminants captured from the process gas is, at least partly, returned to the process in which the process gas was generated.
According to some embodiments, particulate material captured from the process gas or formed in the alkaline solution or slurry is, at least partly, separated from the alkaline solution or slurry. This configuration provides the dual advantage of i) retaining alkaline solution in the alkaline cleaning liquid loop, reducing the make-up base or caustic compound consumption, and ii) providing a high solids content material to be returned to the industrial process, e.g. cement production.
The introduction of an alkaline cleaning step in accordance with aspects described herein may be especially advantageous in chilled ammonia systems producing ammonium sulfate as a by-product.
According to some embodiments, the wash liquid comprises sulfate, e.g. from added sulfuric acid.
According to some embodiments, the ammonia of the process gas containing ammonia and the sulfate of the wash liquid containing sulfate at least partly react to form ammonium sulfate in aqueous solution.
According to some embodiments, the formed ammonium sulfate is, at least partly, used in the production of fertilizer.
According to other aspects, there is provided a gas cleaning system for cleaning a process gas containing carbon dioxide and contaminants, said gas cleaning system comprising:
According to some embodiments, the gas cleaning system further comprises:
The features and advantages of the gas cleaning system correspond to the features and advantages described above in respect of the gas cleaning method.
According to some embodiments, the contaminants include sulfur dioxide, heavy metals and particulate material.
According to some embodiments, the gas cleaning system is integrated with a process burning a lower quality fuel, such as low quality coal or waste.
According to some embodiments, the gas cleaning system is integrated with a power plant, a cement production facility or a steel production facility.
According to some embodiments, the gas cleaning system is integrated with a cement production facility or a steel production facility.
According to some embodiments, the gas cleaning system is integrated with a cement production facility.
According to some embodiments, the alkaline cleaning system is configured to return, at least partly, alkaline solution or slurry the containing contaminants absorbed from the process gas to the process in which the process gas was generated.
According to some embodiments, the alkaline cleaning system further comprises a liquid/solid separator operative for separating, at least partly, solids formed in the alkaline solution or slurry from the solution.
Further objects, features and advantages of the present invention will be apparent from the description and the claims. The above described and other features are exemplified by the following figures and detailed description.
Many aspects of the invention can be better understood with reference to the following drawings. The figures are exemplary embodiments, wherein the like elements are numbered alike.
As used throughout the present description the unit “ppm” refers to parts per million on a volume basis.
As used throughout the present description the unit “%” refers to % on a volume basis.
The terms “flue gas” and “process gas” are used interchangeably throughout the present description.
The gas cleaning system may for example be useful in a power plant, a cement production facility or a steel production facility. The gas cleaning system is especially useful in industrial processes such as cement or steel production generating flue gases with a higher acid, particulate material and/or heavy metal content than characteristic of most power plants.
During the combustion of a fuel, such as coal or oil, a hot process gas, often referred to as a flue gas or process gas, is generated. The flue gas, which contains polluting substances, including dust particles, sulfur dioxide, SO2, sulfur trioxide, SO3, and carbon dioxide, CO2, leaves the boiler via a gas duct. The gas duct is operative for forwarding the flue gas to a conventional air pollution control system. The flue gas forwarded from the industrial process or associated air pollution control system should have a temperature adjusted to the water content and the and the ambient pressure. Depending on the industrial process the water dew point temperature may range from about 40 to about 80° C.
The CO2 removal stage 2 is similar to the carbon dioxide removal system described in WO 2006/022885. The type of carbon dioxide removal system described in WO 2006/022885 is sometimes referred to as the Chilled Ammonia Process, CAP. A flue gas temperature of 0-20° C., preferably 0-10° C., is suitable for the CO2 removal stage 5. The cooling system 3 is operative for cooling the flue gas to a suitable temperature for the CO2 removal stage 5.
Hence, the CO2 removal stage 5 comprises, with reference to
A duct 16 is operative for forwarding flue gas, having a low concentration of CO2, from the CO2 absorber 10 to a water wash vessel 17, which is optional and which is operative for removing ammonia, NH3, from the flue gas that has been treated in the CO2 absorber 10. The water wash vessel 17 could have a similar design as the water wash vessel described in WO 2006/022885. A stream of cold water or cold and slightly acidic solution is supplied to the water wash vessel 17 via pipe 18. A duct 19 is operative for forwarding flue gas, that has been cleaned in the water wash vessel 17, to the ammonia removal system 4 for further cleaning.
The alkaline cleaning system (ACS) 6, cooling system 3, and ammonia removal system 4 will be described in more detail hereinafter.
In typical prior chilled ammonia gas cleaning systems the cooling system is also used for removal of acidic gaseous components, such as SO2, and also for removal of other contaminants, such as particulate material and heavy metals, which are typically present in the gas stream downstream of wet or dry flue gas desulfurization (FGD) systems or other air quality control systems typically employed.
The gas cleaning systems according to the embodiments described herein further comprise an alkaline cleaning system 6, arranged upstream of the cooling system 3 with respect to the main flow direction of the gas stream.
The flue gas, optionally processed in a conventional air pollution control system as described above, enters the ACS 6 via the duct 20. The ACS comprises at least one gas-liquid contacting device 21. Each gas-liquid contacting device is arranged to bring the gas stream into contact with an alkaline solution or slurry. The contacting may preferably be performed in counter current flow such that the gas enters the gas-liquid contacting device 21 at one end (typically at the bottom) and the liquid enters the gas-liquid contacting device at the other end (typically at the top). The flue gas with a reduced content of SO2, particulate material and/or heavy metals leaves the ACS via the duct 22 and is forwarded to the cooling system 3.
The alkaline solution or slurry comprises an aqueous solution of a base or caustic compound. The base or caustic compound of the alkaline solution or slurry may for example be NaOH or Ca(OH)2. The alkaline solution or slurry preferably has a pH value of 8 or higher. The pH value of the alkaline solution or slurry is maintained by introduction of make-up base or caustic compound or composition by a base storage and dosing system 23.
The incoming process gas entering the ACS 6 comprises varying amounts of water vapor and may in some cases be saturated with water vapor. In order to avoid dilution of the alkaline solution or slurry by bulk condensation of water vapor from the incoming gas stream, the alkaline cleaning step is performed at a temperature above the dew point of the process gas. For this reason, the base or caustic compound of the alkaline solution or slurry should be selected among compounds having sufficiently low vapor pressure at the operating temperature of the alkaline cleaning step, to avoid loss of the base or caustic compound to the process gas. Specifically, the base or caustic compound should not be ammonia due to its high vapor pressure at the relevant operating temperatures leading to contamination of down-stream systems, e.g. the cooling system.
When the alkaline solution or slurry is brought into contact with the process gas in the gas/liquid contacting device 21, at least a part of the sulfur dioxide, heavy metals and particulate material of the process gas is captured in the alkaline solution or slurry.
The alkaline solution or slurry may thus further contain amounts of contaminants absorbed from the gas stream such sulfate and other sulfur derivatives formed upon dissolution of sulfur dioxide and sulfur trioxide from the gas stream in the alkaline solution or slurry. The alkaline solution or slurry may also comprise significant amounts of particulate material captured from the gas stream or formed due to chemical reaction between different components in the alkaline solution or slurry.
The alkaline solution or slurry leaving the gas-liquid contacting device is recirculated to the gas-liquid contacting device via a liquid loop 24.
The amount of alkaline solution or slurry in the liquid loop 24 of the ACS 6 may preferably be kept essentially constant. An increase in the volume of alkaline solution or slurry in the loop is compensated by the removal of alkaline solution or slurry from the loop via one or more bleed streams.
The ACS comprises a bleed stream 25 for removing a portion of the alkaline solution or slurry circulating in the liquid loop 24. The alkaline solution or slurry removed via the bleed stream 25 can be returned, at least partly, to the process in which the process gas was generated or sent for waste treatment or disposal.
The ACS 6 may optionally further comprise a liquid/solid separator 26 operative for separating, at least partly, solids formed in the alkaline solution or slurry. The liquid/solid separator 26 may for example comprise a hydrocyclone, a centrifuge or a filter. The liquid/solid separation results in a low solids stream which may be returned to the gas/liquid contacting device 21 of the ACS, and a high solids (or sludge) stream 27, which may be returned to the process in which the process gas was generated, or sent for waste treatment or disposal.
The main functions of the ACS are i) to remove, at least partly, sulfur dioxide, from the process gas, ii) to remove, at least partly, heavy metals, from the process gas, and iii) to remove, at least partly, particulate material, from the process gas.
The gas conditioning stage 2 has a cooling system 3 and an ammonia removal system 4, each comprising one or more gas-liquid contacting devices.
The flue gas enters the cooling system via the duct 22. The cooling system 3 (also referred to herein as the “direct contact cooler” or “DCC”) comprises at least one gas-liquid contacting device 28. Each gas-liquid contacting device is arranged to bring the gas stream into contact with a cooling liquid. The contacting may preferably be performed in counter current flow such that the gas enters the gas-liquid contacting device at one end (typically at the bottom) and the liquid enters the gas-liquid contacting device at the other end (typically at the top). The cooled flue gas leaves the cooling system via the duct 29.
The cooling liquid, is generally water or an aqueous solution. The liquid may contain amounts of contaminants absorbed from the gas stream such sulfate and other sulfur derivatives formed upon dissolution of sulfur dioxide and sulfur trioxide from the gas stream in the cooling liquid.
The warm cooling liquid leaving the gas-liquid contacting device is cooled, e.g. in a cooling tower (not shown), and recirculated to the gas-liquid contacting device 28 via a liquid loop 30. In the cooling tower, ambient air is supplied via an inlet duct to the cooling tower and cools the warm cooling liquid in accordance with the well-known principles of cooling towers.
The amount of cooling liquid in the liquid loop 30 of the cooling system may preferably be kept essentially constant. Variations in the volume of cooling liquid in the loop may be compensated by the addition or removal of liquid to the loop. Generally, the incoming flue gas to be cleaned will contain a certain amount of water vapor, which is at least partly condensed when the gas is cooled in the cooling system leading to an increase of the volume of cooling liquid in the loop. This increase should preferably be balanced by a corresponding decrease. This decrease may be achieved, e.g. by water vapor leaving the system with the cleaned flue gas, or in different cooling devices, such as cooling towers, or by cooling liquid leaving the system in one or more bleed streams 31.
The main functions of the cooling system are i) to reduce the flue gas temperature to the required temperature for the absorption process, ii) to condense the major part of the water vapor contained in the incoming process gas to minimize the water ingress to the CO2 absorber system, at the same time significantly reducing the volumetric gas flow and increasing the CO2 concentration, and iii) to remove residual trace components, primarily SO2 and other acidic components from the process gas.
The cold flue gas from the CO2 absorber 10 and optional water wash vessel 17 enters the ammonia removal system 4 via the duct 19. The ammonia removal system 4 (also referred to herein as the “direct contact heater” or “DCH”) comprises at least one gas-liquid contacting device 33. Each gas-liquid contacting device is arranged to bring the gas stream leaving the CO2 removal stage 5 into contact with a wash liquid. The contacting may preferably be performed in counter current flow such that the gas enters the gas-liquid contacting device 33 at one end (typically at the bottom) and the wash liquid enters the gas-liquid contacting device at the other end (typically at the top). The flue gas, depleted in ammonia and reheated, leaves the ammonia removal system via duct 34, which is operative for forwarding the flue gas to a stack which releases the flue gas to the atmosphere.
The wash liquid, is generally an aqueous solution comprising sulfuric acid. The wash liquid absorbs ammonia from the gas stream leaving the CO2 removal stage 5 to produce a gas stream depleted in ammonia and a wash liquid containing sulfate from the sulfuric acid and ammonia from the gas stream. Sulfate and ammonia react in the wash liquid to form ammonium sulfate. A bleed stream 35 containing primarily dissolved ammonium sulfate at a concentration of 20-35 wt % is purged from this section for disposal or commercial use as fertilizer.
The wash liquid leaving the gas-liquid contacting device is recirculated to the gas-liquid contacting device via a liquid loop 36 and a low pH value of the wash liquid is maintained by introduction of make-up sulfuric acid (H2SO4) by a sulfuric acid storage and dosing system 37.
The amount of wash liquid in the liquid loop 36 of the ammonia removal system 4 may preferably be kept essentially constant. Variations in the volume of cooling liquid in the loop may be compensated by the addition or removal of liquid to the loop 36.
The main functions of the ammonia removal system are i) to reduce the ammonia content of the gas stream leaving the CO2 removal stage to a concentration acceptable for release to the atmosphere, and ii) to reheat the gas stream leaving the CO2 removal stage.
The gas stream entering the ammonia removal system 4 will generally be at a temperature of about 7-10° C. and have an ammonia content of less than 200 ppm. In the ammonia removal system 4 the ammonia content of the gas stream is reduced, preferably to about 5 ppmv or less, and the temperature of the gas stream is raised, preferably to 40° C., before the gas is sent to the stack.
Optionally, the cooling system 3 and ammonia removal system 4 are arranged in liquid connection such that liquid used in one system may be reused in the other system. For example, warm cooling liquid from the cooling system 3 may be used for reheating the cold gas stream in the ammonia removal system 4.
The gas cleaning system 1 of
The ACS 6 comprises a gas-liquid contacting device 21 operative for removing contaminants from the flue gas by contacting it directly with an alkaline solution or slurry, which is supplied via a liquid loop 24 and circulation pump 39. A set of nozzles is operative for distributing the alkaline solution or slurry over the gas-liquid contacting device 21, which could have the form of a structured packing, or another suitable type of gas-liquid contacting filling. The flue gas, saturated with water and having a temperature of, for example 40-80° C., enters the ACS 6 and is forwarded upwards, through the gas-liquid contacting device 21. The flue gas leaves the ACS with a reduced content of SO2, particulate material and/or heavy metals. The alkaline solution or slurry comprising SO2, particulate material and/or heavy metals captured from the flue gas is collected at the bottom of the gas-liquid contacting device 21.
The alkaline solution or slurry comprising SO2, particulate material and/or heavy metals captured from the flue gas is forwarded via the liquid loop 24 to a liquid/solid separator 26. The liquid/solid separator 26 comprises a hydrocyclone, a centrifuge or a filter operative for separating, at least partly, particulate material in the alkaline solution or slurry. The liquid/solid separator may for example comprise a hydrocyclone, a centrifuge or a filter. The liquid/solid separation results in a low solids stream which is returned to the gas/liquid contacting device of the ACS via the liquid loop 24 for capturing further contaminants, and a high solids (or sludge) stream, which leaves the ACS via line 27. The high solids (or sludge) stream may be returned to the process in which the process gas was generated, or sent for waste treatment or disposal.
In order to maintain the liquid balance of the ACS, a portion of the low solids stream from the liquid/solid separator 24 can be withdrawn as a bleed stream via pipe 25 and product pump 40 and sent for reuse, waste treatment or disposal.
In order to maintain the pH value of the alkaline solution or slurry, the ACS comprises a base storage and dosing system 23 operative for introducing make-up base or caustic compound. The base or caustic compound of the alkaline solution or slurry may for example be NaOH or Ca(OH)2.
A control device (not shown) may be operative for controlling the operation of the ACS 6. The control device may comprise an automatic controller, which may be a general-purpose computer, application specific computing device or other programmable controller. The control device may comprise sensors for automated or manual measurement of relevant parameters, such as e.g. pH or temperature. For example, a pH-meter may be operative for measuring the pH of the alkaline solution or slurry leaving the liquid/solid separator 26 and for sending a signal containing information about the measured pH to the control device. In response to such a signal the control device may control the supply of make-up base or caustic compound from the base storage and dosing system 23.
The cooling system 3 comprises two gas-liquid contacting devices 41, arranged separately and in sequence with respect to the main flow direction of the flue gas stream.
The flue gas leaving the ACS via duct 22 first reaches a first gas-liquid contacting device 41, also referred to herein as the first direct contact cooler (DCC). The first DCC 41 is operative for cooling of the flue gas by contacting it directly with a cooling liquid, preferably water or an aqueous solution, which is supplied via pipe 42. A set of nozzles is operative for distributing the liquid over the gas-liquid contacting device 41, which could have the form of a structured packing, or another suitable type of gas-liquid contacting filling. The flue gas enters the first DCC 41 via a gas inlet and is forwarded upwards, through the gas-liquid contacting device 41. The flue gas leaves the first DCC 41 at a reduced temperature via a duct 43. The cooling liquid and the flue gas are contacted with each other in the gas-liquid contacting device 41 under exchange of heat. The warm cooling liquid is collected at the bottom of the first DCC 41 and forwarded via pipe 44.
The flue gas leaving the first DCC 41 via duct 43 then reaches a second gas-liquid contacting device 45, also referred to herein as the second DCC. The second DCC 45 is operative for further cooling of the flue gas by contacting it directly with a refrigerated cooling liquid, which is supplied via a pipe 46. A set of nozzles is operative for distributing the liquid over the gas-liquid contacting device 45, which could have the form of a structured packing, or another suitable type of gas-liquid contacting filling. The flue gas enters the second DCC 45 via duct 43 and is forwarded upwards, through the gas-liquid contacting device 45. The further cooled flue gas leaves the second DCC via duct 29. The refrigerated cooling liquid and the flue gas are contacted with each other in the gas-liquid contacting device 45 under exchange of heat. The cooling liquid used in the second DCC is collected at the bottom of the second DCC 45, forwarded via pipe 47 and circulation pump 48 to a chiller 49, and refrigerated by a refrigerant in chiller 49 before being recirculated to the second DCC 45.
The flue gas leaving the cooling system 3 via duct 29 has a temperature of 0-20° C., preferably 0-10° C. The duct 29 is operative for forwarding the flue gas to the CO2 removal stage. The flue gas in duct 29 may optionally be subjected to one or more indirect coolers (not shown) operative for cooling the flue gas to the desired temperature of 0-20° C., preferably 0-10° C. before it is fed to the CO2 absorber.
Advantages provided by embodiments described herein include:
All features and advantages described herein are applicable to both the gas cleaning method and gas cleaning system of the different aspects described herein.
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 |
|---|---|---|---|
| 13150691.7 | Jan 2013 | EP | regional |
