• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    To remove carbon dioxide from combustion exhaust gases, the carbon dioxide-containing gas is passed over a porous support material which has been charged with a solution of at least one alkali carbonate, carbon dioxide is bound from the gas by forming alkali bicarbonate, and the carbon dioxide is recovered from the alkali bicarbonate by raising the temperature is released. The heat needed to heat the carbon dioxide is removed from the combustion exhaust gas from which the carbon dioxide is to be removed by means of a heat exchanger.
    公开号:AT512153A4
    申请号:T299/2012
    申请日:2012-03-12
    公开日:2013-06-15
    发明作者:Wolfgang Dipl Ing Mag Wesner
    申请人:Knoch Kern & Co Kg；
    IPC主号:
    专利说明:

    '.ί' ^ '((. ϋΑΐύΜ.'ύΐ • * L «« * * ···························································································· * · · · · «* · · * ·
    The invention relates to a Ver driving of carbon dioxide from gases, in particular from process and combustion exhaust gases, characterized in that carbon dioxide-containing gas is passed over a porous support material which is loaded with a solution of at least one alkali carbonate, that carbon dioxide from the gas is bound to form alkali metal carbonates and carbon dioxide in various proportions, in particular Wegscheidersalze and alkali metal bicarbonates to form chemical compounds from water, and that carbon dioxide by thermal decomposition of the compounds thus obtained, preferably in high concentration, is released again.
    Carbon dioxide accumulates in (combustion) exhaust gases in concentrations of a few percent. In certain processes, such as when producing clinker or burning lime, carbon dioxide accumulates in higher concentrations of about 20%. For economic utilization or storage, however, it is necessary to provide carbon dioxide highly concentrated. Concentrations greater than 99% are preferred.
    The binding of carbon dioxide to alkali metal carbonates, such as sodium carbonate, wherein alkali hydrogen carbonate, in particular sodium bicarbonate (sodium bicarbonate), or other mixed carbonates (Wegscheidersalze) and their hydrates are known. It is further known to release carbon dioxide by decomposing the bicarbonates and mixed carbonates by raising the temperature above the decomposition point to recover the alkali carbonate. This principle is known for sodium carbonates and potassium carbonates in the form of fluidized bed applications of the pure salts, or of salts on support materials.
    Furthermore, the use of solutions of these salts for the absorption of carbon dioxide is known.
    The known methods work, but not very energy-optimized. Against the background of environmental measures for the reduction of carbon dioxide emissions, a ΛΛ · ····· ** ♦ · ····· · · · · · möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst möglichst·············· · · · · · · · · · Energy consumption is critical to the usability and acceptability of such a process.
    Methods for converting ammonium or alkali metal carbonates to bicarbonates are known.
    Thus, US Pat. No. 4,459,272 A describes a process for the dry conversion of ammonium or alkali metal carbonate into bicarbonate, in which case an ammonium and / or alkali metal carbonate is mixed with liquid water in a carbon dioxide-rich atmosphere at a temperature of about 125.degree. 67 * C) to about 240 ° F (= 115.56 ° C) is reacted. In this case, the reaction temperature should be controlled by evaporation of liquid water at the reaction site and removing the water vapor formed thereby from the reaction atmosphere.
    US 4,664,893 A describes converting alkali metal or ammonium carbonate into bicarbonate absorbent for desulfurizing gases. In this process, a carbon dioxide-containing gas stream is to be brought to a humidity of 90% with water vapor, wherein solid carbonate particles in a fluidized bed with the gas stream at a temperature of 100 ° F (= 37.78 ° C) to 200 ° F (= 93.33 ° C), so that an aqueous film is formed on the carbonate particles, whereby carbon dioxide from the gas stream should be able to pass unhindered onto the surface of the carbonate particles and heat from the carbonate particles to the gas stream.
    WO93 / 1107Q A relates to a process for treating trona (a mineral mixture of sodium carbonate / sodium bicarbonate) to form sodium bicarbonate. It should be carried out with a mixing device, a stirring of the trona particles and a carbon dioxide-containing gas stream with little water to be implemented. The carbon dioxide-containing gas stream is passed through a scrubber where it is saturated with water and returned to the mixer. So shall a new kind of w w. · ♦ · · · ·
    Sodium bicarbonate can be formed "/ * the" * ais "* Abr96rptionsmittel for removing sulfur from exhaust gases can be used.
    In the prior art, the water required for the reaction of alkali metal carbonate / alkali bicarbonate is supplied to the fluid moisture in fluidized bed reactors. Since this amount of water is still not optimal for the reaction rate, large fluidized bed reactors are needed, which require a lot of energy to maintain the fluidized bed. Higher water contents, e.g. could be achieved by injecting water into the fluidized bed, lead to clumping of the carbonates and are therefore not realized.
    When using carbonate solutions, pumping energy is needed to pump the exhaust gas into water. The capacity of solutions is lower than that of the solids and the rate of uptake is better with less concentrated solutions than with the saturated solutions, so that even larger volumes of absorbent are needed. The larger the exchange surface should be, the more pump energy is needed. The most economical way of fixing carbon dioxide with solutions is by spraying the solution in an exhaust scrubber (venturi scrubber). However, here too, in addition to the pumping energy for atomizing the absorption solution in the scrubber, the release of carbon dioxide is more energy-intensive than in processes using moist salts. This results directly from the high heat capacity of water, which must be heated to release the carbon dioxide.
    The object of the invention is to provide an energy-optimized process for removing carbon dioxide from gas, in particular for purifying exhaust gas streams of carbon dioxide, and for the subsequent release of concentrated carbon dioxide.
    The object is achieved according to the invention with a method according to claim 1. 4U ··· «·« * · ** ··· ·· ♦♦ · ♦ ·· «| «· · · · · · · ·
    Advantageous and preferred embodiments of the invention are the subject of the dependent claims.
    The invention provides an energy-saving method for recovering carbon dioxide from gas, primarily from exhaust gases available, at the same time a gas or exhaust gas purification takes place in the sense of reducing the carbon dioxide content of the exhaust gas.
    With the subject invention, it further manages to keep energy consumption low overall, since energy that is needed for the operation of the method can be covered for the most part from waste heat of an industrial operation itself.
    In the method according to the invention, the water management during loading and unloading makes it possible to optimize the method. Since sodium carbonate reacts with water and carbon dioxide to form sodium bicarbonate, the water requirement for the reaction can already be seen from the reaction equation. 2 NaHCO 3 (s) × Na 2 C03 (s) + C03 (g) + H 2 O (g)
    The reaction is reversible, a typical implementation involves "loading". with carbon dioxide at 80 ° C to form sodium bicarbonate. From 120 ° C desorption (calcination) takes place with reformation of sodium carbonate.
    Experiments have shown that a water supply beyond the molar ratio in the process according to the invention leads to a faster conversion of carbon dioxide.
    For example, when carrying out the method according to the invention as described below.
    A porous material, preferably of calcined clay, with a preferred particle size between 2 and 8 mm, is introduced into a reactor. The porous clay material preferably has 40 to 80% pore volume and a pore diameter of 5 to 60pm. f * «+ ··· * ·······························
    Depending on the exhaust gas, the reactor may be executed in any desired form. It is advantageous to have a bulk level inside which is at least 50 cm. At the top, the bed height is limited only by the stability of the porous material, but through intermediate floors, this limitation can be overcome.
    Loading the porous support material with alkali carbonate:
    The porous material is sprinkled with a saturated aqueous solution of an alkali carbonate or a mixture of alkali carbonates (especially sodium and / or potassium carbonate) while blowing air or dry gas from underneath. This results in a supersaturated solution which partially crystallizes out in the capillaries of the support material.
    Loading the alkali carbonate on the carrier material with carbon dioxide: The gas, in particular combustion gas, is blown (preferably at atmospheric pressure or only slightly elevated pressure, usual resistances of the charge amount only a few mbar per meter) through the bulk of the carrier material (regardless of whether from bottom to top , reversed or horizontal), wherein, depending on the flow rate and the length, the flow-through bed, an almost complete absorption of carbon dioxide from the gas to be cleaned.
    Discharging the alkali carbonate:
    The discharge of the alkali carbonate is carried out according to the invention by preheated carbon dioxide (T> 100 ° C preferably 120 to 140 ° C) is circulated through the bed of the support material, wherein the carbon dioxide is heated outside the bed in a heat exchanger.
    The heat on the primary side of the heat exchanger is preferably removed from the combustion exhaust gas before the carbon dioxide removal. The entire circulation preferably remains closed until the decomposition of sodium carbonate builds up a pressure which is higher than the water vapor pressure at the corresponding point 9 ♦ ······································ I
    The temperature is (for example, l, 3t at l2t) e * S) «i» Büfx5K * eiivt) pressure relief valve is drained with water vapor saturated carbon dioxide. After cooling the product gas and condensation of the water is highly concentrated carbon dioxide available for further use.
    Decisive for the advantageous energy balance of a preferred embodiment of the method according to the invention is that no additional water vapor escapes and remains saturated with alkali carbonate water and also undissolved carbonate in the pores of the carrier material. This saves not only water but, above all, the amount of heat that would be needed to evaporate water. Loss of water due to the discharge of saturated carbon dioxide can be compensated by adding condensed water to the reactor head.
    As an alternative to introducing heat via heated carbon dioxide, the release of carbon dioxide can also be achieved by blowing in superheated steam, which condenses in the bed with release of the heat of condensation. The condensate replaced in this variant of the method according to the invention the loss of water as a result of the discharge of moist carbon dioxide. In addition, introduced steam causes an advantageous for purifying the absorbent water excess. Water and alkali carbonate solution, which drips down to the bottom of the reactor, can be re-applied from above into the reactor after a process-like purification of the solution.
    Purification of the absorbent and the carrier material:
    Since exhaust gas (combustion exhaust gas) not only contains pure carbon dioxide and nitrogen, but also contains dusts and sulfur compounds which would reduce the performance of the absorption process over time, in one embodiment of the process according to the invention it is provided that the bed is regularly treated with a concentrated solution of alkali carbonate is sprinkled. This solution is pumped through a purge in the circulation, and only the losses as a result of the ························································································ · * * · * · ♦ · * * β
    Cleaning will be replaced. Dusts are removed by mechanical filters. Alkali sulphates have a lower solubility than the alkali metal carbonates and bicarbonates, whereby they precipitate in the saturated alkali carbonate solution and can be filtered off. If, after a long period of operation, larger amounts of sulphates accumulate in the capillaries of the carrier material, this can be washed out with water. A replacement of the carrier material is therefore not required over many years of operation.
    Abrasion of the carrier material can also be disposed of by treating the solution. The loss of substrate due to abrasion can be supplemented regularly to maintain the original capacity of the plant.
    The regular cleaning of the bed by the facilities described above is advantageous in order to obtain the permeability of the bed even with coarser dust input and prevent sludge. If the entire water required for the binding has to be evaporated again during the release of carbon dioxide in conventional processes, then the process according to the invention has a comparatively small amount of heat.
    External pumps and blower for pressure build-up, which would have to be operated with electrical energy, are not necessary.
    The enriched carbon dioxide is already available with a pre-pressure of approx.
    Using an excess of water with a large contact surface between the gas phase and the liquid phase allows a particularly effective binding of the carbon dioxide and thus reduces the plant costs.
    The fact that only low pressures must be built is an advantage of the method according to the invention.
    In order to be able to operate continuously, at least two reactors with the bed of porous material may be provided, which are alternately loaded and unloaded.
    In the drawing, an example of a system in which the method according to the invention can be performed is shown schematically.
    A warm, carbon dioxide-containing exhaust stream is withdrawn heat in the first heat exchanger 1 at a high Temperat.urniveau. With this heat, steam is generated in the container 6, or steam heated in the container 7 at a lower temperature level is heated, or humid carbon dioxide heating the bed for desorption in the cycle is heated. If there is no sufficient amount of heat available from the exhaust gas, process waste heat or simply heat (preferably from regenerative sources) can be made available via a further heat exchanger 11.
    The already cooled exhaust gas 2 further heat is removed at a lower temperature level in a second heat exchanger. This heat is utilized in the vessel 7 to generate steam or to heat steam / carbon dioxide to preheat the bed after switching from absorption to desorption. About the Kühlwasser.der capacitors 8 and 9, the container 7, the heat of condensation of the water can be supplied from the product gas stream again.
    The third heat exchanger 3 cools the exhaust gas to the absorption temperature, preferably 80 ° C from. This waste heat can still be used to preheat water or feed solutions.
    The exhaust gas stream is then passed through an optional pre-cleaning 10 consisting of a bed of alkali bicarbonates. This bed is not regenerated but replaced intermittently or continuously. 9 • · · * · · · «· ·
    Sulfur oxides bind here and dust mechanically arrives.
    Thereafter, the exhaust gas is passed through the valves A or B in one of the absorption reactors 4 or 5, while the other is desorbed. In the top of the column or thereafter, capacitors 8 and 9 are attached, which condense the water out of the product during desorption. During absorption, capacitors 8 and 9 have no function.
    Thereafter, the purified exhaust gas flow through the valves G and D is released. Valves E and F are used to release the product gas during desorption. Draining takes place according to the invention at a pressure which is above the boiling point of the water at the corresponding reactor temperature. The valves E and F therefore have a corresponding pressure control, which only clears the path for the carbon dioxide when the pressure is exceeded by the decomposition of the alkali metal bicarbonates. If the release were to take place at lower pressures and lower temperatures, the heat requirement would increase sharply due to the large amounts of water which evaporate, which is less advantageous.
    The plant parts 12a to 12c serve to treat the solution of the alkali bicarbonates. Dust, abrasion and precipitated salts are removed by means of filter devices and separators. The resulting loss of solution or alkali carbonates is compensated for by addition after the purification.
    Optionally, circulation pumps I, J, K, L, N, 0 are provided, which can be saved with optimized plant planning. The energy for pressure build-up in the desorption is provided by heat according to the invention, by evaporation of water and the decomposition of the alkali bicarbonates results in a sufficient pressure build-up, so that no compressor or compressors are required.
    In summary, an embodiment of the invention may be described as follows.
    To remove carbon dioxide from combustion exhaust gases, the carbon dioxide-containing gas is passed over a porous support material which has been charged with a solution of at least one alkali carbonate, carbon dioxide is bound from the gas by forming alkali bicarbonate, and the carbon dioxide is recovered from the alkali bicarbonate by raising the temperature is released. The heat needed to heat the carbon dioxide is removed from the combustion exhaust gas from which the carbon dioxide is to be removed by means of a heat exchanger. 11 11
    REFERENCE SIGNS LIST 1 First heat exchanger for heat recovery from the exhaust gas 2 Second heat exchanger for heat recovery from the exhaust gas 3 Third heat exchanger for cooling the exhaust gas 4 First absorption tank filled with a bed of porous support material loaded with alkali carbonate 5 Second absorption tank filled with a bed of porous support material loaded with alkali carbonate 6 evaporator and / or storage tank for Dampf.oder
    Steam / carbon dioxide for heat input for the release of the bound carbon dioxide 7 Storage tank for carbon dioxide and / or steam for preheating the bed after loading 8 First condenser for condensing the water in the product gas stream 9 Second condenser for condensing the water in the product gas stream 10 Flue gas scrubbing, replaceable bed a bicarbonate for mechanical filtering and for the binding of sulfur oxides in the form of their alkali metal salts. 11 heat exchangers for the provision of process waste heat and or additional heat, preferably from renewable energy sources. 12a, b, c Preparation of the alkali carbonate solution, removal of dust, abrasion, poorly soluble salts by various filtration methods. A, B, C, D valves for the deflection of the exhaust gas flow to realize a batch operation of the reactors. E, F Pressure valves which allow the withdrawal of carbon dioxide during discharge. G, H heat input valves for desorption,
    Control of carbon dioxide and / or steam. M valve for recovery of condensation heat. I, J, K, L, N, 0 Circulation pumps optional
    权利要求:
    Claims (19)
    [1]
    12 • * Patentanäjfififeh'e » *. Process for the recovery of carbon dioxide from gases, in particular from process and combustion exhaust gases, characterized in that carbon dioxide-containing gas is passed over a porous carrier material which is loaded with a solution of at least one alkali carbonate in that carbon dioxide from the gas is bound to form chemical compounds of water alkali carbonates and carbon dioxide, in particular Wegscheidersalze and alkali bicarbonates, and that carbon dioxide by thermal decomposition of the compounds thus obtained, preferably in high concentration, is released again. A method according to claim 1, characterized in that the heat required for the thermal decomposition amount of heat is supplied by supplying heated carbon dioxide and / or water vapor. A method according to claim 1 or 2, characterized in that the heat required for the thermal decomposition to heat carbon dioxide and / or water vapor, and / or the heat required for generating water vapor from water, at least partially combustion exhaust gases is withdrawn and / or from Process waste heat and / or from renewable energy sources is provided. Method according to one of claims 1 to 3, characterized in that the thermal decomposition to release carbon dioxide, at a pressure which is higher than the vapor pressure of water at the prevailing temperature. Method according to one of claims 1 to 4, characterized in that water vapor is condensed from the deducted carbon dioxide before relaxing by cooling the gas stream. 13
    [2]
    6. Method according to one of the claims, characterized in that the boiling point of the water is increased by addition of substances not participating in the binding of CO 2, in particular of readily soluble salts so that the evaporation of water in the release of carbon dioxide is reduced.
    [3]
    7. The method according to any one of claims 1 to 6, characterized in that as a porous carrier material fired clay is used.
    [4]
    8. The method according to claim 7, characterized in that burnt clay with a grain size of 0.5 to 100 mm, preferably 2 to 8 mm is used.
    [5]
    9. The method according to claim 7 and 8, characterized in that fired clay is used with a pore volume of 10 to 90%, preferably 40% to 80%.
    [6]
    10. The method according to any one of claims 7 to 9, characterized in that porous, fired clay whose pores. predominantly have a pore diameter less than 100 pm, preferably less than 10 μπι and that alkali carbonate solution in the capillaries and increasing the boiling point of located in the capillaries takes place water.
    [7]
    11. The method according to any one of claims 1 to 10, characterized in that the gas is passed through a reactor which is filled with a bed of porous carrier material.
    [8]
    12. The method according to any one of claims 1 to 11, characterized in that for discharging carbon dioxide through the porous support material to a temperature of more than 100 ° C, preferably more than 120 ° C, heated, moist carbon dioxide, is passed. 14 »*
    [9]
    13. A method according to one of the Ans] Jeilefee'.l.bfts * 1 * 1 * characterized in that for discharging carbon dioxide steam is introduced into the reactor, that the steam cooled as a result of the endothermic decomposition of the alkali carbonate carbon dioxide compounds and then under further heat output is condensed.
    [10]
    14. The method according to any one of claims 1 to 13, characterized in that the heat required for heating the carbon dioxide is partially or completely removed from combustion exhaust gases from which the carbon dioxide is to be removed, or from process waste heat of an upstream production process or optionally downstream carbon dioxide processing processes is won.
    [11]
    15. The method according to any one of claims 2 to 14, characterized in that the steam, which is required for the release of carbon dioxide, at a temperature and a pressure which are smaller than those in the reactor, where the decomposition takes place, from waste heat is produced at a temperature level between 60 and 120 ° C, and that the steam thus obtained is heated to a temperature above the decomposition temperature only for introduction into the reactor.
    [12]
    16. The method according to any one of claims 1 to 15, characterized in that combustion exhaust gases and / or waste water and / or process media heat is removed by means of a heat exchanger.
    [13]
    17. The method according to any one of claims 1 to 16, characterized in that combustion exhaust heat is removed before the exhaust gases are passed through the porous support material, in particular the reactor.
    [14]
    18. The method according to any one of claims 1 to 17, characterized in that at least * ea- * nlAL * ka * Li # käi: i * 5nat on a porous support material in the form of a concentrated to supersaturated solution, optionally at least partially crystallized present.
    [15]
    19. The method according to any one of claims 1 to 18, characterized in that the porous support is loaded with a solution 'of at least one alkali carbonate by the porous carrier is sprinkled with the solution.
    [16]
    20. The method according to claim 19, characterized in that steam-supersaturated air or other undersaturated gas is passed through the porous support material, while the porous support material is sprinkled with the solution of at least one alkali carbonate.
    [17]
    21. The method according to any one of claims 1 to 20, characterized in that for regeneration at least a portion of the support material, with a detergent, preferably water or aqueous solutions, is washed and this support material is then loaded again with alkali carbonate.
    [18]
    22. Process according to claims 1 to 20, characterized in that at least part of the support material is regenerated by washing with saturated solutions of the salts applied to the support material in order to remove dust, adhering impurities and unwanted reaction products, such as alkali metal sulphates.
    [19]
    23. The method according to claim 21 or 22, characterized in that a regeneration of the solution of leached alkali metal carbonate by filtration and / or ion exchange and / or precipitation takes place and the solution or salts of this solution is purified by the carbon dioxide-containing exhaust gas supplied impurities. 24. 16 * ················································································································································································································································· is in the form of a bed, which is divided into individual parallel or series connected areas that these areas are sprinkled independently with washing solution and that the support material, optionally during operation, can be washed and loaded independently of other areas in the individual areas , Process according to any one of Claims 1 to 24, characterized in that the bulk of support material is conveyed by means of transport such as e.g. Conveyor belts, screws or vibrating systems, is moved from the gas outlet to the gas inlet of the reactor containing the bed, that fresh or regenerated carrier material is added to the gas outlet side and that on the gas inlet side, the escaping carrier material is removed.
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    同族专利:
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    EP2638953A2|2013-09-18|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3660023A|1970-02-02|1972-05-02|Dow Chemical Co|Process for recovering carbon dioxide from stack gas|
    JP2001232148A|2000-02-25|2001-08-28|Toshiba Corp|Carbon dioxide absorbent and its manufacturing method|
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    WO2008061958A1|2006-11-24|2008-05-29|Basf Se|Method for the separation of carbon dioxide using a porous metal-organic framework material|
    US3527618A|1968-05-13|1970-09-08|United Aircraft Corp|Fuel cell with carbon dioxide gas stripper and method of operation|
    DE3520671C2|1985-06-08|1988-11-17|Kernforschungsanlage Juelich Gmbh, 5170 Juelich, De|
    JP3853398B2|1994-05-23|2006-12-06|株式会社四国総合研究所|Carbon dioxide recovery method and carbon dioxide adsorbent|
    US6387337B1|2000-07-14|2002-05-14|The United States Of America As Represented By The United States Department Of Energy|Carbon dioxide capture process with regenerable sorbents|
    JP2007526822A|2004-01-28|2007-09-20|マイクロポアーインコーポレイテッド|Improved carbon dioxide adsorption|EP3077080B1|2013-12-03|2019-02-20|Antecy B.V.|Moisture swing carbon dioxide enrichment process|
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    法律状态:
    2018-11-15| MM01| Lapse because of not paying annual fees|Effective date: 20180312 |
    优先权:
    申请号 | 申请日 | 专利标题
    ATA299/2012A|AT512153B1|2012-03-12|2012-03-12|Process for recovering carbon dioxide|ATA299/2012A| AT512153B1|2012-03-12|2012-03-12|Process for recovering carbon dioxide|
    EP13450012.3A| EP2638953A3|2012-03-12|2013-03-12|Method for the recovery of carbon dioxide|
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