Patent Application
20110186441
None
Embodiments of the invention relate to methods and systems for electrolytic recovery of retained gasses from absorption liquid to regenerate the absorption liquid.
One approach to reducing emissions of carbon dioxide gas includes recovery of the carbon dioxide from power plants and other point sources. Such recovery depends on ability to remove or capture the carbon dioxide from other gasses. By example, sequestration of the carbon dioxide once captured provides ability to dispose of the carbon dioxide without creating atmospheric environmental issues.
A prior technique that enables the recovery of the carbon dioxide utilizes an amine solution that absorbs the carbon dioxide and is then regenerated by steam stripping. However, generating steam by burning fossil fuels in order to release the carbon dioxide from the amine solution produces more carbon dioxide and contributes to operational costs making the recovery expensive. Other problems associated with such prior systems include need to further purify an overhead containing the carbon dioxide released during the steam stripping to remove water and need to compress the carbon dioxide via inefficient as compression. Size of vessels required for the steam stripping can also limit ability to locate the prior systems where desired. Further, raising temperature of the amine solution with the steam stripping results in undesired increasing corrosiveness of the amine solution in contact with components of the system.
Therefore, a need exists for improved methods and systems that enable carbon dioxide capture.
In one embodiment, a method of capturing carbon dioxide from a gas mixture includes contacting an aqueous solution formed from amine and metal ions with the gas mixture thereby forming metallocarbamate complexes from the amine, the metal ions and the carbon dioxide. Separating the aqueous solution from unabsorbed constituents of the gas mixture occurs after the contacting. Applying an electric potential to the aqueous solution recovered by the separating causes dissociation of the metallocarbamate complexes in order to liberate the carbon dioxide for capture.
According to one embodiment, a method of capturing carbon dioxide from a gas mixture includes forming an aqueous solution by mixing monoethanolamine and copper ions from copper sulfate. Contacting the aqueous solution with the gas mixture forms metallocarbamate complexes from the monoethanolamine, the copper ions and the carbon dioxide. The method further includes separating the aqueous solution from unabsorbed constituents of the gas mixture after the contacting. Pumping the aqueous solution recovered by the separating increases pressure of the aqueous solution to above a first pressure associated with the contacting prior to applying an electric potential to the aqueous solution to liberate from the aqueous solution the carbon dioxide at a second pressure above the first pressure.
For one embodiment, a method of capturing carbon dioxide from a gas mixture includes forming an aqueous solution by mixing amine and metal ions with less of the metal ions added on a mole basis than the amine. Contacting the aqueous solution with the gas mixture causes the aqueous solution to absorb the carbon dioxide. Separating the aqueous solution from unabsorbed constituents of the gas mixture occurs after the contacting. In addition, the method includes applying an electric potential to the aqueous solution recovered by the separating such that throughout the applying of the electric potential one of the metal ions reacts with more than one molecule to facilitate liberation of the carbon dioxide and regeneration of the aqueous solution.
The invention, together with further advantages thereof, may best be understood by reference to the following description taken in conjunction with the accompanying drawings.
Embodiments of the invention relate to capturing carbon dioxide. A solution formed from metal ions combined with an amine reagent absorbs carbon dioxide from gas introduced into the solution. Subsequent electrolysis of the solution results in dissociation of complexes formed upon the carbon dioxide being absorbed. The electrolysis thus liberates the carbon dioxide for capture and regenerates the solution for reuse.
The solution absorbs the carbon dioxide from the gas mixture such that the treated gas contains a lower concentration of the carbon dioxide than present in the gas mixture as introduced into the absorber vessel 100 at the gas input 102. In some embodiments, flue gas defines the gas mixture, which thus may include between about 3% and about 30% carbon dioxide by volume and other exhaust gasses, such as about 70% to about 95% nitrogen. For some embodiments, passage of the gas mixture through the absorber 100 removes at least about 70%, at least about 80% or at least about 90% of the carbon dioxide from the gas mixture.
In operation, the solution in the absorber vessel 100 over time becomes saturated with the carbon dioxide and for continuous operation must therefore be replenished with new or regenerated solution. A rich liquid conduit 106 from the absorber vessel 100 couples the absorber vessel 100 with an optional pump 107 and an electrolysis cell 108, which is used to regenerate the solution by releasing the carbon dioxide from complexes formed from the amine, the carbon dioxide and the metal ions. The electrolysis cell 108 includes a counter electrode 110 and a working electrode 112 that supply an electric potential to the solution in the electrolysis cell 108. The working electrode 112 reduces metal in the complex resulting in release of the carbon dioxide. Alternating between positive and negative potentials ensures the metal ions are not depleted by elemental metal plating on the working electrode 112. For some embodiments, a liquid-gas phase selective membrane may facilitate separation of the carbon dioxide from the solution upon the carbon dioxide being liberated from the complexes. A carbon dioxide recovery outlet 114 of the electrolysis cell 108 captures the carbon dioxide liberated within the electrolysis cell 108.
Controlling voltage applied during the electrolysis and selection of the counter and working electrodes 110, 112 can avoid competing reactions and decomposition of water concurrent with the release of the carbon dioxide from the solution in the electrolysis cell 108. While the voltage depends on reactant concentrations in the solution and composition of the electrodes 110, 112, the voltage in some embodiments cycles between about −3 volts to about +3 volts. Alternating between positive and negative potentials about each minute, for example, ensures that the metal ions are not depleted from the solution as a result of precipitation or plating on the working electrode 112.
Experiments utilizing stainless steel for both the electrodes 110, 112 liberated the carbon dioxide but also resulted in some water electrolysis. As shown by an Example herein, providing the working electrode 112 made out of carbon allows separation of the carbon dioxide without release of hydrogen, which occurs with the carbon at higher voltages relative to carbon dioxide being liberated. A conductive metal that is either inert in the solution or provides the metal ions may form the counter electrode 110. Platinum for example may form the counter electrode 110 in order to avoid introduction of metal ions such as iron that can form undesired complexes with the amine.
The pump 107 in fluid communication with the solution inside the absorber vessel 100 and inside the electrolysis cell 108 functions to increase pressure of the solution that is fed to the electrolysis cell 108 to above a first pressure, such as ambient pressure, associated with the contacting inside the absorber vessel 100. In some embodiments, the pump 107 maintains the solution inside the electrolysis cell 108 at sufficient elevated pressure such that the carbon dioxide is released at a second pressure, such as above about 6750 kilopascal, higher than the first pressure. The carbon dioxide output through the recovery outlet 114 may not require further compression for transport or sequestration purposes due to use of the pump 107.
A lean liquid line 116 couples the electrolysis cell 108 to the absorber vessel 100 to resupply the solution for more carbon dioxide absorption. The lean liquid line 116 contains the solution formed from the amine and the metal ions with the carbon dioxide removed upon the solution being regenerated in the electrolysis cell 108. The solution thus cycles through the absorber vessel 100 and the electrolysis cell 108 for treating a stream of the gas mixture fed into the gas input 102.
For some embodiments, the amine used to form the solution includes a linear or noncyclical amine in water such that the solution is aqueous. A general formula provided as
may represent the amine with R1 being CxH2xOH and R2 being one of hydrogen and CyH2yOH, given x and y are from 1 to 8, or 2 to 4. Specific alcohol amines that were tested and demonstrated suitability include monoethanolamine (MEA), diethanolamine (DEA), diisopropanolamine (DIPA) and diglycolamine (DGA).
In some embodiments, linearity of the amine and the amine having at least one hydrogen atom bound to nitrogen of the amine helps ensure that the nitrogen remains sterically free and available for carbamate formation. Further, noncyclical formulas of the amine lack sites where the metal ion complexes for carbonate formation preferential to the carbamate formation during the carbon dioxide absorption. In operation, complexes formed by absorption of the carbon dioxide may thus not include carbonate groups.
In some embodiments, the metal ions used to form the solution include at least one of copper, zinc, cobalt, nickel, aluminum and magnesium and may be di-cationic species. The complexes formed from the amine, the metal ions and the carbon dioxide provide ionic charged species that are influenced by the electrical potential such that reduction is achieved at the working electrode 112 of the electrolysis cell 108. Experiments utilizing amine, such as MEA, without the metal ion proved inability for electrolytic release from the amine of the carbon dioxide absorbed. While possible to separate conductive mixtures like sodium hydroxide, the amine alone cannot achieve recovery of the carbon dioxide using electrolysis.
For some embodiments, adding a metal salt to a reagent containing the amine forms the solution with the metal ions from the metal salt. Selection of the metal salt depends on solubility of the metal salt and avoidance of anion interference with electrochemistry. Examples of the metal salt include copper sulfate (CuSO4) or copper perchlorate (Cu(ClO4)2). In some embodiments, a metal electrode, such as the counter electrode 110 or a different disposable anode, within a reagent containing the amine supplies a source of the metal ions to form the solution upon electric current dissolving the metal electrode. Copper ions can for example come from use of the working electrode 110 if made from copper.
Various factors influence amount of the metal ions and the amine added to form the solution. Addition of either the amine or the metal ions enables adjusting levels of the amine and the metal ions independent of one another in the solution at any time as needed. Reaction efficiency increases with amount of the metal ions added to make the solution. Even with stabilization of the metal ions by the amine, potential for formation of metal carbonate that is not able to be regenerated limits increasing concentration of the metal ions. Corrosion issues also limit increasing concentration of the amine.
The solution is formed on a mole basis from less of the metal ions than the amine such that there is not a 1:1 stoichiometric quantity of the metal ions to the amine. Each of the metal ions thus reacts with different molecules containing the amine throughout regeneration of the solution while applying the electric potential. In an exemplary embodiment, the forming of the solution includes mixing reagent of between about 10 percent and about 20 percent MEA in water with copper sulfate such that copper ions added are between about 1 mole percent and about 5 mole percent relative to the MEA.
A solution for absorbing carbon dioxide was prepared by adding copper sulfate to a 15 percent aqueous solution of MEA such that copper was 3 mole percent relative to the MEA. The solution was enriched with carbon dioxide through sparging. An electric potential was then applied to the solution utilizing a carbon working electrode and a stainless steel counter electrode. Effluent gasses from the solution during application of the electric potential were collected and passed through a mass spectrometer for analysis.
The preferred embodiment of the present invention has been disclosed and illustrated. However, the invention is intended to be as broad as defined in the claims below. Those skilled in the art may be able to study the preferred embodiments and identify other ways to practice the invention that are not exactly as described herein. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims below and the description, abstract and drawings are not to be used to limit the scope of the invention.
This application is a non-provisional application which claims the benefit of and priority to U.S. Provisional Application Ser. No. 61/299,775 filed Jan. 29, 2010, entitled “Electrolytic Recovery of Retained Carbon Dioxide,” which is hereby incorporated by reference in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 61299775 | Jan 2010 | US |
