Patent Application
20140360369
The invention relates to a process for absorbing CO2 from a gas mixture.
Gas streams which have an undesirable high content of CO2 which has to be reduced for further processing, for transport or for avoiding CO2 emissions occur in numerous industrial and chemical processes.
On the industrial scale, CO2 is typically absorbed from a gas mixture by using aqueous solutions of alkanolamines as an absorption medium. The loaded absorption medium is regenerated by heating, depressurization to a lower pressure or stripping, and the carbon dioxide is desorbed. After the regeneration process, the absorption medium can be used again. These processes are described for example in Rolker, J.; Arlt, W.; “Abtrennung von Kohlendioxid aus Rauchgasen mittels Absorption” [Removal of carbon dioxide from flue gases by absorption] in Chemie Ingenieur Technik 2006, 78, pages 416 to 424, and also in Kohl, A. L.; Nielsen, R. B., “Gas Purification”, 5th edition, Gulf Publishing, Houston 1997.
A disadvantage of these processes, however, is that the removal of CO2 by absorption and subsequent desorption requires a relatively large amount of energy and that, on desorption, only a part of the absorbed CO2 is desorbed again, with the consequence that, in a cycle of absorption and desorption, the capacity of the absorption medium is not sufficient.
Diamines, oligoamines and polyamines have been proposed as alternatives to alkanolamines in the prior art.
WO 2004/082809 describes absorption of CO2 from gas streams using concentrated aqueous solutions of diamines of formula (R1)2N(CR2R3)nN(R1)2 where R1 may be a C1-C4 alkyl radical and R2 and R3 may each independently be hydrogen or a C1-C4 alkyl radical. For the case where n=4, the diamines tetramethyl-1,4-butanediamine and tetraethyl-1,4-butanediamine are explicitly disclosed. Diamines comprising two tertiary amino groups have the disadvantage that absorption of CO2 proceeds slowly.
WO 2010/012883 describes the absorption of CO2 from gas streams using an aqueous solution of N,N,N′,N′-tetramethyl-1,6-hexanediamine. In order to avoid phase separation into two liquid phases during absorption, it is further necessary, to add a primary or secondary amine to the absorption medium.
WO 2011/080405 describes the absorption of CO2 from gas streams using aqueous solutions of diamines of formula R1R2N(CR4R5)(CR6R7)aNHR3 where R1 and R2 may each independently be a C1-C12 alkyl radical or a C1-C12 alkoxyalkyl radical, R3 to R7 may each independently be hydrogen, a C1-C12 alkyl radical or a C1-C12 alkoxyalkyl radical, a=1 to 11 and R3 is different from R1 and R2. For the case where n=3, the diamine N1,N1-diethyl-1,4-pentanedamine is explicitly disclosed.
WO 2011/080406 describes the absorption of CO2 from gas streams using aqueous solutions of triamines. The triamine N1,N1-diethyl-N4-dimethylaminoethyl-1,4-pentanediamine is disclosed as having an increased absorption capacity compared to ethanolamine and methyldiethanolamine.
It has now been found that, surprisingly, the amines of formula (I) provide an improved CO2 absorption capacity compared to the amines known from WO 2004/082809 and WO 2011/080405 and heating in a subsequent desorption step provides a particularly low residual CO2 content.
The invention accordingly provides a process for absorbing CO2 from a gas mixture by contacting the gas mixture with an absorption medium comprising water and at least one amine of formula (I)
The amines of formula (I) used in the process according to the invention are diamines in which the nitrogen atoms are separated by a chain of 4 carbon atoms which bears on at least one of the carbon atoms adjacent to the nitrogen atoms an alkyl radical having 1 to 4 carbon atoms. Both nitrogen atoms are further substituted with alkyl groups having 1 to 6 carbon atoms, so in each case a secondary or tertiary amino group is present. One of the two nitrogen atoms may also be part of a saturated heterocycle, for example of a pyrrolidine, piperidine, morpholine or piperazine.
The radicals R1 and R2 in formula (I) may be alkyl radicals having 1 to 4 carbon atoms, unbranched n-alkyl radicals being preferred. It is preferable to use amines of formula (I) in which the chain connecting the nitrogen atoms bears only one alkyl substituent, i.e., the radical R1 in formula (I) is hydrogen. It is particularly preferable when the chain connecting the nitrogen atoms is substituted with a methyl group, i.e., the radical R2 in formula (I) is methyl.
The radicals R3 to R6 in formula (I) may be cyclic or acyclic alkyl radicals having 1 to 6 carbon atoms, unbranched n-alkyl radicals being preferred. In a preferred embodiment, one of the two nitrogen atoms of the amine of formula (I) is a tertiary amine, i.e., the radical R4 in formula (I) is not a hydrogen atom. It is particularly preferable for the amine of formula(I) to comprise both a secondary and a tertiary amino group, i.e., the radical R6 in formula (I) is a hydrogen atom and the radical R4 in formula (I) is not a hydrogen atom. The tertiary nitrogen atom preferably bears two identical radicals R3 and R4, which, more preferably, are methyl or ethyl groups or combine with the nitrogen atom to form a morpholine ring i.e., R3 and R4 form the bridging radical —CH2CH2OCH2CH2—.
Particularly preferred amines of formula(I) are N1,N1,N4-trimethyl-1,4-diaminopentane, N1,N1-dimethyl-N4-ethyl-1,4-diaminopentane, N1,N1-dimethyl-N4-propyl-1,4-diaminopentane, N1,N1-diethyl-N4-methyl-1,4-diaminopentane, N1,N1,N4-triethyl-1,4-diaminopentane, N1,N1-diethyl-N4-propyl-1,4-diaminopentane, N-(4-methylamino)pentylmorpholine, N-(4-ethylamino)pentylmorpholine and N-(4-propylamino)pentylmorpholine.
Amines of formula(I) may be prepared according to known processes. In a first step, in accordance with equation (1), a nitroalkane is reacted with an α,β-unsaturated carbonyl compound in a Michael addition, as described in J. Am. Chem. Soc. 74 (1952) 3664-3668.
In a further step, in accordance with equation (2), a reductive amination with an alkylamine is carried out at the carbonyl group of the product from the first step, followed by reduction of the nitro group, for example as described in U.S. Pat. No. 4,910,343.
Substituents R5 and R6 may subsequently be introduced by further reductive amination, as shown in equation (3) for the introduction of R5=ethyl by reductive amination.
The working medium used in the process according to the invention comprises water and at least one amine of formula (I). The content of amines of formula (I) in the absorption medium is preferably 10 to 60 wt %, more preferably 20 to 50 wt %. The content of water in the absorption medium is preferably 40 to 80 wt %.
The absorption medium may, in addition to water and amines of formula (I), further comprise at least one sterically unhindered primary or secondary amine as an activator. A sterically unhindered primary amine for the purposes of the invention is a primary amine in which the amino group is bonded to a carbon atom which has at least one hydrogen atom bonded to it. A sterically unhindered secondary amine for the purposes of the invention is a secondary amine in which the amino group is bonded to carbon atoms each having at least two hydrogen atoms bonded to them. The content of sterically unhindered primary or secondary amines is preferably 0.1 to 10 wt %, more preferably 0.5 to 8 wt %. Suitable activators include activators known from the prior art, such as monoethanolamine, piperazine and 3-(methylamino)propylamine. The addition of an activator brings about an increase in the rate of absorption of CO2 from the gas mixture without a loss of absorption capacity.
In addition to water and amines, the absorption medium may further comprise one or more physical solvents. The proportion of physical solvents in this case may be up to 50% by weight. Suitable physical solvents include sulfolane, aliphatic acid amides, such as N-formyl-morpholine, N-acetylmorpholine, N-alkylpyrrolidones, more particularly N-methyl-2-pyrrolidone, or N-alkylpiperidones, and also diethylene glycol, triethylene glycol and polyethylene glycols and alkyl ethers thereof, more particularly diethylene glycol monobutyl ether. Preferably, however, the absorption medium contains no physical solvent.
The absorption medium may additionally comprise further additives, such as corrosion inhibitors, wetting-promoting additives and defoamers.
All compounds known to the skilled person as suitable corrosion inhibitors for the absorption of CO2 using alkanolamines can be used as corrosion inhibitors in the absorption medium of the invention, in particular the corrosion inhibitors described in U.S. Pat. No. 4,714,597. In the process of the invention, a significantly lower amount of corrosion inhibitors can be chosen than in the case of a customary absorption medium containing ethanolamine, since the absorption medium used in the method of the invention is significantly less corrosive towards metallic materials than the customarily used absorption media that contain ethanolamine.
The cationic surfactants, zwitterionic surfactants and nonionic surfactants known from WO 2010/089257 page 11, line 18 to page 13, line 7 are preferably used as wetting-promoting additive.
Defoamers that may be used in the absorption medium include any substances known to those skilled in the art as suitable defoamers for absorption of CO2 using alkanolamines.
In the process according to the invention, the gas mixture may be a natural gas, a methane-containing biogas from a fermentation, composting or a sewage treatment plant, a combustion off-gas, an off-gas from a calcination reaction, such as the burning of lime or the production of cement, a residual gas from a blast-furnace operation for producing iron, or a gas mixture resulting from a chemical reaction, such as, for example, a synthesis gas containing carbon monoxide and hydrogen, or a reaction gas from a steam-reforming hydrogen production process. The gas mixture is preferably a combustion off-gas, a natural gas or a biogas, particularly preferably a combustion off-gas, for example from a power station.
The gas mixture can contain further acid gases, for example COS, H2S, CH3SH or SO2, in addition to CO2. In a preferred embodiment, the gas mixture contains H2S in addition to CO2. A combustion off-gas is preferably desulphurized beforehand, i.e. SO2 is removed from the gas mixture by means of a desulphurization method known from the prior art, preferably by means of a gas scrub using milk of lime, before the absorption process of the invention is carried out.
Before being brought into contact with the absorption medium, the gas mixture preferably has a CO2 content in the range from 0.1 to 50% by volume, particularly preferably in the range from 1 to 20% by volume, and most preferably in the range from 10 to 20% by volume.
The gas mixture can contain oxygen, preferably in a proportion of from 0.1 to 25% by volume and particularly preferably in a proportion of from 0.1 to 10% by volume, in addition to CO2.
For the process of the invention, all apparatus suitable for contacting a gas phase with a liquid phase can be used to contact the gas mixture with the absorption medium. Preferably, absorption columns or gas scrubbers known from the prior art are used, for example membrane contactors, radial flow scrubbers, jet scrubbers, venturi scrubbers, rotary spray scrubbers, random packing columns, ordered packing columns or tray columns. With particular preference, absorption columns are used in countercurrent flow mode.
In the process of the invention, the absorption of CO2 is carried out preferably at a temperature of the absorption medium in the range from 0 to 80° C., more preferably 20 to 70° C. When using an absorption column in countercurrent flow mode, the temperature of the absorption medium is more preferably 30 to 60° C. on entry into the column, and 35 to 70° C. on exit from the column.
The CO2-containing gas mixture is preferably contacted with the absorption medium at an initial CO2 partial pressure of from 0.01 to 4 bar. It is particularly preferable when the initial partial pressure of CO2 in the gas mixture is from 0.05 to 3 bar. The total pressure of the gas mixture is preferably in the range from 0.8 to 50 bar, more preferably 0.9 to 30 bar.
In a preferred embodiment of the process of the invention, CO2 absorbed in the absorption medium is desorbed again by increasing the temperature and/or reducing the pressure and the absorption medium after this desorption of CO2 is used again for absorbing CO2. The desorption is preferably carried out by increasing the temperature. By such cyclic operation of absorption and desorption, CO2 can be entirely or partially separated from the gas mixture and obtained separately from other components of the gas mixture.
As an alternative to the increase in temperature or the reduction in pressure, or in addition to an increase in temperature and/or a reduction in pressure, it is also possible to carry out a desorption by stripping the absorption medium loaded with CO2 by means of an inert gas, such as air or nitrogen.
If, in the desorption of CO2, water is also removed from the absorption medium, water may be added as necessary to the absorption medium before reuse for absorption.
All apparatus known from the prior art for desorbing a gas from a liquid can be used for the desorption. The desorption is preferably carried out in a desorption column. Alternatively, the desorption of CO2 may also be carried out in one or more flash evaporation stages.
The desorption is carried out preferably at a temperature in the range from 50 to 200° C. In a desorption by an increase in temperature, the desorption of CO2 is carried out preferably at a temperature of the absorption medium in the range from 50 to 180° C., more preferably 80 to 150° C. The temperature during desorption is then preferably at least 20° C., more preferably at least 30° C., above the temperature during absorption. When desorption is effected by increasing the temperature, it is preferable to carry out stripping using steam generated by evaporating part of the absorbtion medium.
When desorption is effected by reducing the pressure, the desorption is preferably carried out at a pressure in the range from 0.01 to 10 bar.
Since the absorption medium used in the process according to the invention has a high CO2 absorption capacity and is present in the processes according to the invention as a homogeneous solution, with no precipitation of a solid occurring on absorption of CO2, the process according to the invention can be used in plants of a simple construction and, if so used, achieves an improved CO2 absorption performance compared to the amines known from the prior art. At the same time, compared to ethanolamine, substantially less energy is required to desorb CO2.
In a preferred embodiment of the process of the invention, the desorption is carried out by stripping with an inert gas such as air or nitrogen in a desorption column. The stripping in the desorption column is preferably carried out at a temperature of the absorption medium in the range from 60 to 100° C. Stripping enables a low residual content of CO2 in the absorption medium to be achieved after desorption with a low energy consumption.
The following examples illustrate the invention without, however, limiting the subject matter of the invention.
Into a stirred autoclave were charged 52.9 g (1.20 mol) of acetaldehyde and 50 ml of methanol. Subsequently, 2.90 g of 10% palladium on activated carbon (water-moist), 130 ml of methanol and 196 g of N1,N1-diethyl-1,4-diaminopentane (1.20 mol) were added. The autoclave was sealed and pressurized to 40 bar with hydrogen. The mixture was heated from 40° C. to 100° C. over 5 h under a hydrogen atmosphere, further hydrogen being introduced to re-establish a pressure of 40 bar when the pressure in the autoclave fell below 20 bar. Subsequently, the catalyst was filtered off and, following distillative removal of the solvent, the residue was distilled. 135 g (0.724 mol, 60%) of N1,N1,N4-triethyl-1,4-diaminopentane were obtained as a colourless liquid.
Example 1 was repeated except that 74.7g (1.26 mol) of propionaldehyde and 100 ml of methanol were charged, and 100 ml of methanol were subsequently added instead of 130 ml of methanol. 143 g (0.714 mol, 59%) of N1,N1-diethyl-N4-propyl-1,4-diaminopentane were obtained as a colourless liquid.
Into a stirred autoclave were charged 105 g (1.80 mol) of acetone. Subsequently, 3.60 g of 10% palladium on activated carbon (water-moist), 180 ml of methanol and 245 g of N1,N1-diethyl-1,4-diaminopentane (1.50 mol) were added. The autoclave was sealed and pressurized to 40 bar with hydrogen. The mixture was heated from 40° C. to 120° C. over 8 h under a hydrogen atmosphere, further hydrogen being introduced to re-establish a pressure of 40 bar when the pressure in the autoclave fell below 20 bar. Subsequently, the catalyst was filtered off and, following distillative removal of the solvent, the residue was distilled. 260 g (1.30 mol, 87%) of N1,N1-diethyl-N4-isopropyl-1,4-diaminopentane were obtained as a colourless liquid.
For determining the CO2 loading and the CO2 uptake, 150 g of absorption medium composed of 30 wt % of amine and 70 wt % of water were charged to a thermostatable container with a top-mounted reflux condenser cooled at 3° C. After heating to 40° C. or 100° C., a gas mixture of 14% CO2, 80% nitrogen and 6% oxygen by volume was passed at a flow rate of 59 l/h through the absorption medium, via a frit at the bottom of the container, and the CO2 concentration in the gas stream exiting the reflux condenser was determined by IR absorption using a CO2 analyser. The difference between the CO2 content in the gas stream introduced and in the exiting gas stream was integrated to give the amount of CO2 taken up, and the equilibrium CO2 loading of the absorption medium was calculated. The CO2 uptake was calculated as the difference in the amounts of CO2 taken up at 40° C. and at 100° C. The equilibrium loadings determined in this way at 40° C. and 100° C., in mol CO2/mol amine, and the CO2 uptake in mol CO2/kg absorption medium are given in Table 1.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10 2012 200 566.8 | Jan 2012 | DE | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2012/074019 | 11/30/2012 | WO | 00 | 7/15/2014 |
