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Engineering » Environmental Engineering » "CO2 Sequestration and Valorization", book edited by Claudia do Rosario Vaz Morgado and Victor Paulo Pecanha Esteves, ISBN 978-953-51-1225-9, Published: March 12, 2014 under CC BY 3.0 license. © The Author(s).

Chapter 14

Alkaline and Alkaline-Earth Ceramic Oxides for CO2 Capture, Separation and Subsequent Catalytic Chemical Conversion

By Margarita J. Ramírez-Moreno, Issis C. Romero-Ibarra, José Ortiz- Landeros and Heriberto Pfeiffer
DOI: 10.5772/57444

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Theoretical CO2 capture capacities for different alkaline and alkaline-earth ceramics. In the Li8SiO6 (labeled as *) and Li4SiO4 (labeled as +), the maximum capacity can depend on the CO2 moles captured in each different phase formed (Li8SiO6 + CO2 → Li4SiO4 + CO2 → Li2SiO3 + Li2CO3).
Figure 1. Theoretical CO2 capture capacities for different alkaline and alkaline-earth ceramics. In the Li8SiO6 (labeled as *) and Li4SiO4 (labeled as +), the maximum capacity can depend on the CO2 moles captured in each different phase formed (Li8SiO6 + CO2 → Li4SiO4 + CO2 → Li2SiO3 + Li2CO3).
Membrane-based processes for the carbon dioxide separation from flue gases. The concentrated CO2 is obtained in the permeate side.
Figure 2. Membrane-based processes for the carbon dioxide separation from flue gases. The concentrated CO2 is obtained in the permeate side.
Schematic representation of a membrane system for the CO2 separation via a dual-ion conduction mechanism.
Figure 3. Schematic representation of a membrane system for the CO2 separation via a dual-ion conduction mechanism.
CO2/N2 separation factor of different ceramic oxide membranes.
Figure 4. CO2/N2 separation factor of different ceramic oxide membranes.
Schematic representation of a membrane system for the CO2 separation and SEM image of a ceramic oxide-carbonate dual-phase membrane
Figure 5. Schematic representation of a membrane system for the CO2 separation and SEM image of a ceramic oxide-carbonate dual-phase membrane
Schematic representation of the membrane reactor concept using a CO2 permselective ceramic membrane: (a) CO2 dry methane reforming and (b) water-gas shift reaction with hydrogen purification wherein CO2 capture promotes the separation process.
Figure 6. Schematic representation of the membrane reactor concept using a CO2 permselective ceramic membrane: (a) CO2 dry methane reforming and (b) water-gas shift reaction with hydrogen purification wherein CO2 capture promotes the separation process.

Alkaline and Alkaline-Earth Ceramic Oxides for CO2 Capture, Separation and Subsequent Catalytic Chemical Conversion

Margarita J. Ramírez-Moreno1, 2, Issis C. Romero-Ibarra1, José Ortiz-Landeros2 and Heriberto Pfeiffer1

1. Introduction

The amounts of anthropogenic carbon dioxide (CO2) in the atmosphere have been raised dramatically, mainly due to the combustion of different carbonaceous materials used in energy production, transport and other important industries such as cement production, iron and steelmaking. To solve or at least mitigate this environmental problem, several alternatives have been proposed. A promising alternative for reducing the CO2 emissions is the separation and/or capture and concentration of the gas and its subsequent chemical transformation. In that sense, a variety of materials have been tested containing alkaline and/or alkaline-earth oxide ceramics and have been found to be good options.

The aforementioned ceramics are able to selectively trap CO2 under different conditions of temperature, pressure, humidity and gas mixture composition. The influence of those factors on the CO2 capture (physically or chemically) seems to promote different sorption mechanisms, which depend on the material’s chemical composition and the sorption conditions used. Actually, this capture performance suggests the feasibility of these kinds of solid for being used with different capture technologies and processes, such as: pressure swing adsorption (PSA), vacuum swing adsorption (VSP), temperature swing adsorption (TSA) and water gas shift reaction (WGSR). Therefore, the fundamental study regarding this matter can help to elucidate the whole phenomena in order to enhance the sorbents’ properties.

2. CO2 capture by different alkaline and alkaline-earth ceramics

Among the alkaline and/or alkaline-earth oxides, various lithium, sodium, potassium, calcium and magnesium ceramics have been proposed for CO2 capture through adsorption and chemisorption processes [1-20]. These materials can be classified into two large groups: dense and porous ceramics. Dense ceramics mainly trap CO2 chemically: the CO2 is chemisorbed. Among these ceramics, CaO is the most studied one. It presents very interesting sorption capacities at high temperatures (T ≥ 600 °C). In addition to this material, alkaline ceramic oxides have been considered as possible captors, mostly lithium and sodium based ceramics (Li5AlO4 and Na2ZrO3, for example). In these cases, one of the most interesting properties is related to the wide temperature range in which some of these ceramics trap CO2 (between 150 and 800 °C), as well as their high CO2 capture capacity.

In these ceramics, the CO2 capture occurs chemically, through a chemisorption process. At a micrometric scale, a general reaction mechanism has been proposed, where the following steps have been established: Initially, CO2 reacts at the surface of the particles, producing the respective alkaline or alkaline-earth carbonate and in some cases different secondary phases. Some examples are:

Li5AlO4+ 2 CO22Li2CO3+ LiAlO2
Na2ZrO3+ CO2Na2CO3+ ZrO2
CaO + CO2CaCO3

The above reactions show that surface products can be composed of carbonates, but as well they can contain metal oxides or other alkaline/alkaline-earth ceramics. The presence of these secondary phases can modify (improve or reduce) the diffusion processes described below [1].

Once the external carbonate shell is formed, different diffusion mechanisms have to be activated in order to continue the CO2 chemisorption, through the particle bulk. Some of the diffusion processes correspond to the CO2 diffusion through the mesoporous external carbonate shell, and some others such as the intercrystalline and grain boundary diffusion processes [1, 18, 21].

Figure 1 shows the theoretical CO2 chemisorption capacities (mmol of CO2 per gram of ceramic) for the most studied alkaline and alkaline-earth ceramics. As it can be seen, metal oxides (Li2O, MgO and CaO) are among the materials with the best CO2 capture capacities. Nevertheless, Li2O and MgO have not been really considered as possible options due to reactivity and kinetics factors, respectively. On the contrary, CaO is one of the most promising alkaline-earth based materials, with possible real industrial applications. Other interesting materials are ceramics with lithium or sodium phases, which present better thermal stabilities and volume variations than CaO. In addition, the sodium phases may present another advantage if the CO2 capture is produced in the presence of steam. Under these conditions the sodium phases may produce sodium bicarbonate (NaHCO3) as the carbonated phase, which is twice the amount of CO2 could be trapped in comparison to the Na2CO3 product.


Figure 1.

Theoretical CO2 capture capacities for different alkaline and alkaline-earth ceramics. In the Li8SiO6 (labeled as *) and Li4SiO4 (labeled as +), the maximum capacity can depend on the CO2 moles captured in each different phase formed (Li8SiO6 + CO2 → Li4SiO4 + CO2 → Li2SiO3 + Li2CO3).

Other ceramics containing alkaline-earth metals are the layered double hydroxides (LDH) or hydrotalcite-like compounds (HTLc). LDHs, also called anionic clays due to their layered structure and structural resemblance to a kind of naturally-occurring clay mineral. These materials are a family of anionic clays that have received much attention in the past decades because of their numerous applications in many different fields, such as antacids, PVC additives, flame retardants and more recently for drug delivery systems and as solid sorbents of gaseous pollutants [22-24]. The LDH structure is based on positively charged brucite like [Mg(OH)2] layers that consist of divalent cations surrounded octahedrally by hydroxide ions. These octahedral units form infinite layers by edge sharing [25]. Due to the fact that certain fraction of the divalent cations can be substituted by trivalent cations at the centers of octahedral sites, an excess of positive charge is promoted. The excess of positive charge in the main layers of LDHs is compensated by the intercalation of anions in the hydrated interlayer space, to form the three-dimensional structure. These materials have relatively weak bonds between the interlayer and the sheet, so they exhibit excellent ability to capture organic or inorganic anions. The materials are easy to synthesize by several methods such as co-precipitation, rehydration-reconstruction, ion exchange, hydrothermal, urea hydrolysis and sol gel, although not always as a pure phase [26].

The LDH materials are represented by the general formula: [M1-xIIMxIII(OH)2]x+[Am]x/mnH2Owhere MII and MIII are divalent (Mg2+, Ni2+, Zn2+, Cu2+, etc.) and trivalent cations (Al3+, Fe3+, Cr3+, etc.), respectively, and Am- is a charge compensating anion such as CO32-, SO42-, NO3-, Cl-, OH-, where x is equal to the molar ratio of [MIII/(MII + MIII)]. Its value is commonly between 0.2 and 0.33, i.e., the MII/MIII molar ratio is in the range of 4 - 2 [25], but this is not a limitation ratio and it depends on the MII and MIII composition [27-29].

Among various CO2 mesoporous adsorbents, LDH-base materials have been identified as suitable materials for CO2 sorption at moderate temperatures (T ≤ 400 °C) [30-46] due to their properties such as large surface area, high anion exchange capacity (2-3 meq/g) and good thermal stability [37-40]. The LDH materials themselves do not possess any basic sites. For that reason, it is preferred to use their derived mixed oxides, formed by the thermal decomposition of LDH, which do exhibit interesting basic properties. Thermal decomposition of the material occurs in three stages, first at temperatures lower than 200 °C, at which the dehydration of superficial and interlayer water molecules takes place on the material. Then the second decomposition stage takes place in the range of 300-400 °C, at which the structure collapses due to a partial dehydroxylation process, typically associated with both the decomposition of Al-OH and the Mg-OH hydroxides. During dehydroxylation, changes occur in the structure. A portion of the trivalent cations of the brucite like layers migrates to the interlaminar region, allowing the preservation of the laminar characteristics of the material [41]. Finally, the total decomposition of the material occurs at temperatures higher than 400 °C, when the decarbonation process is completed [42].

Once the temperature reaches about 400 °C, LDH forms a three-dimensional network of compact oxygen with a disordered distribution of cations in the interstices, where the cations M+3 are tetrahedrally coordinated (interlayer region) and M+2 are octahedrally coordinated. The compressive-expansion stresses associated with the formation of the amorphous three-dimensional networks and their connection to the octahedral layer increases the surface area and pore volume, which can help improve the storage capacity properties, for example for gas sorption related applications, besides decreasing the ability of the Mg+2 cation to favor physisorption instead of chemisorption [30, 42]. For instance, the thermal evolution of the Mg/Al-CO3 LDH structure is considered to be crucial in determining the CO2 adsorption capacity, so there are several studies about this issue [42-44].

Reddy et al. [43] studied the effect of the calcination temperature on the adsorptive capacity of the Mg/Al-CO3 LDH. They found out that the best properties were obtained at calcination temperature of 400 °C, which they attributed to the obtaining of a combination of surface area and the availability of the active basic sites. Actually, at this temperature the material is still amorphous, which allows having a relatively high surface area. Therefore, there is a high number of exposed basic sites, allowing the reversible CO2 adsorption according to the following reaction:

Mg-O + CO2   Mg-O  CO2 (ad)

However, if the LDH is calcined under 500 °C, the material is able to transform back to the original LDH structure when it is exposed to a carbonate solution or another anionic containing solution. Finally, if the sample is heated to temperatures above 500 °C, the structural changes become irreversible because of the spinel phase formation [37].

As mentioned, the mixed oxides derived from the LDH calcination possess some interesting characteristics such as high specific surface area, excess of positive charge that needs to be compensated, basic sites and thermal stability at elevated temperatures (200 – 400 °C). Besides these aspects, it is important to consider the advantage of acid-base interactions on the CO2 sorption applications, where acidic CO2 molecules interact with the basic sites on the derived oxide. These characteristics make the LDH-materials acceptable CO2 captors [43, 45]. However, the CO2 adsorption capacity of this material is low compared with other ceramic sorbents; reaching mean values smaller than 0.1 mmol/g [46]. Nevertheless, many studies suggest that the adsorption capacity of LDH materials can be improved by modifying a factor set such as: composition, improvement of the material’s basicity and contaminant gas stream composition [30-32, 36, 41-45, 47-59].

As previously mentioned, Reddy et al. [43] studied the influence of the calcination temperature of LDHs on their CO2 capture properties. The Mg3/Al1-CO3 material was calcined at different temperatures ranging from 200 to 600 °C. The results showed that when the calcination temperatures are under 400 °C, LDH is considered to be dehydrated and materials still keep the layered structure intact, wherein the CO32- ions are occupying the basic sites. The obtained samples calcined at 400 °C have the maximum BET surface area of 167 m2/g compared with samples calcined at lower temperatures. Moreover, during the calcination of the LDH at higher temperatures (T > 500 °C), most of the CO32- decompose to release some basic sites for CO2 adsorption. However, the final amount of basic sites decreases with the subsequent crystallization of the MgO and spinel (MgAl2O4). Hence, LDH materials obtained at 400 °C have the highest surface area and the maximum quantities of active basic sites exposed. Because of these characteristics, they achieved a total sorption capacity of 0.5 mmol/g [43]. The same researchers observed that 88% of the captured gas can be desorbed and during the material regeneration 98% of the original weight is gained. This is another important property of LDH materials in high temperature CO2 separation applications as described later..

As mentioned, the thermal evolution of the layered structure has a great influence on the CO2 capture. The loss of superficial interlayer water occurs at 200 °C. Then at temperatures between 300 and 400 °C the layer decomposition begins, resulting in an amorphous 3D network with the highest surface area [30], so the adsorption temperature improves the CO2 capture in the order of 400 > 300 > 20 >200 °C [41-42, 47, 52]

Several researchers have investigated a set of different factors to improve the CO2 sorption capacity. Yong et al. [47, 48] studied the factors which influence the CO2 capture in LDH materials, such as aluminum content, water content and heat treatment temperature. Regarding the M/Al-CO3 LDHs (M = Mg, Ni, Co, Cu or Zn), the best CO2 sorption capacity was obtained for the Mg/Al materials degassed at 400 °C and with adsorption conditions of 25 °C. In general, the sorption capacity follows the trend Ni > Mg > Co > Cu = Zn. However, when the degassed temperature is increased, the trend is modified to Mg (400 °C) > Co (300°C) > Ni (350°C) > Cu (300°C) >Zn (200°C). These results show that Mg/Al-CO3 is the best composition at the degassing temperature of 400 °C [47]. At this temperature, the material consists of an amorphous phase with optimal properties for use as CO2 captor [42]. Also, the influence of Al+3 has been studied as a trivalent cation at 25 and 300 °C adsorption temperatures, by Yong [41] and Yamamoto [49] respectively. Both samples were degassed at 300 °C and the results showed that the CO2 capture is influenced by the adsorption temperature. At a temperature of 25 °C, the maximum adsorption was 0.41 mmol/g with an Mg/Al ratio equal to 1.5 (x = 0.375) [41] and at 300 °C the amount of CO2 adsorbed was 1.5 mmol/g for a cation ratio of 1.66 (x = 0.4) [49]. The differences between the two capacities can be attributed to the Al content differences. The Al incorporation in the structure has two functions: 1) to increase the charge density on the brucite-like sheet; and 2) to reduce the interlaminar distance and the number of sites with high resistance to CO2 adsorption [48].

On the other hand, Qian et al. [50] studied the effect of the charge compensation anions (A- = CO3-2, NO3-1, Cl-, SO4-2 and HCO3-1) on the structural properties and CO2 adsorption capacity of Mg/Al-A- (molar ratio equal to 3). Despite all of the prepared LDH materials showed the typical XRD patterns of LDH materials, slight structural and microstructural differences were observed. In fact, the interlayer distance changed by varying the interlayer anions due to their difference in sizes and carried charges. These differences affect the morphology and the BET surface area of both fresh and heat-treated LDH materials. Additionally, thermal treatments were performed in order to optimize the adsorption capacity of these materials. The optimal temperature treatment was established for each Mg/Al-A- based on the surface area of each calcined LDH. Then the CO2 adsorption capacities of calcined LDH were tested at 200 °C. Mg3/Al1–CO3 showed the highest CO2 adsorption capacity (0.53 mmol/g). This value was much higher than those obtained for calcined Mg3/Al1-NO3 > Mg3/Al1-HCO3, Mg3Al1-Cl, and Mg3/Al1-SO4 ( ≈ 0.1 mmol/g). The results indicated that BET surface area of calcined LDHs seems be the main parameter that determines the CO2 adsorption capacity because the Mg-O active basic site [43, 45].

It has been demonstrated that the quasi-amorphous phase obtained by the thermal treatment of LDH at the lowest possible temperature has the highest CO2 capture capacity. This finding is in line with the fact that high calcination temperature can decrease the number of active Mg–O sites due to the formation of crystal MgO [51].

Yong [41] and Yamamoto [49] investigated the influence of the several types of anions. The results suggested that the amounts CO2 capture decrease as a function of the anion size, which promotes a larger interlayer spacing and the higher charge: Fe(CN)64-(1.5 mmol/g) > CO32- (0.5 mmol/g) > NO3- (0.4 mmol/g) > OH- (0.4-0.25 mmol/g). The reason is that Fe(CN)64- and CO32-, because they have more void space in the interlayer due size, and are able to accommodate higher CO2 quantities. Calcined layered double hydroxide derivatives have shown great potential for high temperature CO2 separation from flue gases. However, the presence of SOx and H2O from flue gases can strongly affect CO2 adsorption capacity and regeneration of hydrotalcite-like compounds. Flue gases emitted from power stations contain considerable amounts of water in the form of steam. The percentage of water found in the flue gas emitted from different sources varies between 7 and 22%, with the emissions from brown coal combustion having the highest water content [45]. For many other gas adsorption sorbents, steam generally has a negative effect on the adsorption performance because of competition for basic sites between CO2 and H2O. However, the presence of water or steam seems to be favorable for the adsorption capacity onto LDH [31,43,53,54]. This fact is the result of the increasing potential energy that is able to further activate basic sites, possibly by maintaining the hydroxyl concentration of the surface material and/or preventing site poisoning through carbonate or coke deposition [31]. An example of the above was reported by Yong et al. [47], who found that water or steam can increase the adsorption capacity of CO2 by about 25%, from 0.4 mmol/g to 0.5 mmol/g.

Ding et al. [31] studied CO2 adsorption at higher temperatures (480 °C) under conditions for steam reforming of methane. They found an adsorption capacity of 0.58 mmol/g, which was independent of water vapor content in the feed. In turn, Reddy et al. [45] investigated calcined LDHs’ sorption performance influenced by CO2 wet-gas streams. LDH samples were calcined at 400 °C [43] before measuring CO2 sorption at 200 °C. The gas streams used were CO2, CO2 + H2O, flue gas (14% CO2, 4% O2 and 82 % N2) +12% H2O.

For a pure CO2 dry sorption, the maximum weight gain was 2.72% (~0.61 mmol/g) after 60 min, whereas the wet adsorption increased the weight of the calcined LDHs to 4.81%, showing an additional 2.09%, where He and He + H2O were used to remove the H2O water capture. The results showed that the helium has virtually no significant sorption affinity for the material, whereas the water-sorption profile of it clearly indicates a water weight gain of 1.67%, i.e., the gain was 0.1mmol/g due to steam presence, showing that water has a positive effect, shifting the CO2 sorption by 0.42% as compared to dry CO2 sorption. Also, these results revealed that in all cases about 70% sorption occurs during the first 5 min and reaches equilibrium after around 30 min.

To determine the influence of CO2, Reddy et al. [43] tested a sample in both, wet and dry CO2 stream conditions. The experiments showed that the same quantity of CO2 can be trapped for the solid sorbent after two hours. The presence of water in the stream only affects the kinetics of the process. This result is in agreement with that reported by Ding et al. [31]. On the other hand, the results of the material tested suggest that the fact the CO2 capture from flue gas was higher than in a pure stream of CO2 might have been because the polluted gas was diluted in the stream. The presence of the water does not enhance de CO2 capture; the maximum CO2 adsorbed was 0.9 mmol/g. The differences between Reddy et al. results and the previously mentioned studies can be caused by the use of uncalcined LDHs, which already contain an -OH network.

To apply these materials in industrial processes, it is important to know the times during which each sorbent material can be used. Tests of the cyclability in LDH materials disclose that as function of the temperature the CO2 capture time can vary. This can be attributed to CO2 chemisorbed during each cycle [54] and/or to the formation of spinel-based aluminas, such as γ-Al2O3 (at temperatures higher than 400 °C). Hibino et al. [52] found that the carbonate content, acting as charge-compensating anion, continuously decreases in subsequent calcination – rehydration cycles. Reddy et al. tested LDH materials during six CO2 adsorption (200 °C)-desorption (300 °C) cycles. The average amount gained was 0.58 mmol/g, whereas 75% of this value is desorbed, reaching desorption equilibrium after the third cycle. This can be attributed to the stabilization of the material phase and basic sites during the temperature swing.

Hufton et al. [54] studied a LDH material during several cycles in dry and wet CO2 flows. As previously discussed, the presence of steam in the flow gas improves the CO2 adsorption. However, after 10 adsorption cycles, the capture decreased 45%. The same behavior was observed in the dry gas flow. However, the final capture was similar to the wet gas stream, in agreement with Reddy et al. [43].

Recent studies have demonstrated that K-impregnated LDH or K-impregnated mixed oxides have a better CO2 capture capacity due to the addition of K alkaline-earth element that improves the chemical affinity between the acidic CO2 and alkaline surface of the sorbent material [32, 36, 55-56]. Additionally, it has been proposed that K-impregnation reduces the CO2 diffusion resistance in the material. [57]. Hufton et al. [58] showed that the K-impregnation increases the CO2 capture, but there is an optimal quantity of K to reach the maximum capture. Qiang et al. [50] tested an Mg3/Al1-CO3 (pH = 10) impregnated with 20 wt.% K2CO3. The CO2 adsorption capacity was increased between 0.81 and 0.85 mmol/g in the temperature range of 300 - 350 °C. This adsorption capacity is adequate for application in water gas shift reactions (WGS).

Lee et al. [59] tested the behavior of three commercial LDHs impregnated with K (K2CO3/LDH ratio between 0 and 1). Three Mg/Al-CO3 LDH with different contents of magnesium were used. Results indicated that the sorption capacity of the LDH is improved by about 10 times with the optimal K2CO3 additions. Additionally, it was observed that impregnation is not the only factor that influences the adsorption but the composition too. The best value was obtained when the content of divalent cation was reduced and therefore, the material had a composition with the maximum trivalent cation content. The CO2 adsorption capacity improved from 0.1mmol/g to 0.95mmol/g with K2CO3/LDH weight ratio equal to 0.35 at 400 °C. After determining the optimal alkaline source/LDH ratio, a set of samples was evaluated as a function of the temperature and the results showed a maximum of 1.35 mmol/g, at 50 °C. In the impregnated materials, CO2 chemisorption can occur and the sorbed CO2 can be further stored as metal carbonate forms.

Other alkaline elements can be used to improve the sorption capacity of materials. Martunus et al. [46] studied the impregnation of LDH with Na and K. The LDH samples were thermally treated at 450 °C for 5 min then calcined samples were re-crystallized in K2CO3 and Na2CO3 (1 M) solutions. The re-crystallized materials were tested as CO2 captors and the capture was maximum with LDH-Na (0.688 mmol/g) > LDH- K (0.575 mmol/g) at 350 °C after five cycles. Finally, the re-crystallized material with the highest capture was calcined at 650 °C for 4 h and re-crystallized with a solution containing the appropriate quantities of K and Na to achieve alkaline metal loading up to 20%. When the sample was Impregnated with additional K and Na at 18.4% and 1.6%, respectively, the adsorption capacity rose from 0.688 to 1.21 mmol/g. This capacity increase was achievable despite the relatively low BET surface area, equal to 124 m2/g.

Other alkaline elements such as cesium have been studied as reinforcement. Oliveira et al. [55] tested commercial Mg1/Al1-CO3 and Mg6Al1-CO3 impregnated with K and Cs carbonates. The materials were evaluated in the presence of steam (26% v/v water content) gas at different temperatures (306, 403 and 510 °C) at 0.4 bar of CO2 partial pressure (total pressure 2 bar). The LDH with the highest sorption capacity was Mg1/Al1-CO3–K with 0.76 mmol/g at 403 °C. Among the Cs impregnated samples, the Mg6Al1-CO3-Cs presented the highest capacity with 0.41 mmol/g, while the commercial LDH samples presented CO2 sorption capacities around 0.1 mmol/g.

The results suggest the existence of a sorption mechanism combining physical adsorption and chemical reaction. First the maximum physical adsorption is reached, then the chemisorption begins, but there is an optimal temperature. If the temperature is too low, the chemisorption does not happen, but with higher temperatures the loss of porosity impedes the contact of CO2 molecules with active basic sites promoted by the alkaline element addition.

These results suggest there is an optimum amount of K2CO3 to impregnate the LDH that achieves a balance between the increase in the basicity of the sorbent material and its reduction of surface area, associated with CO2 capture capacity. The influence of potassium is currently not clear and the relevant research is still ongoing. Finally, CO2 adsorption capacity on the synthesized 20 wt.%K2CO3/Mg3/Al1–CO3 (pH = 10) probably could be further increased in the presence of steam.

3. Ceramic oxide membranes as an alternative for CO2 separation

Membrane-based processes, related to gas separation and purification, have achieved an important level of development for a variety of industrial applications [60]. Therefore, the use of separation membranes is one of the promising technologies for reducing the emissions of greenhouse gases such as CO2. The term membrane is defined as a permselective barrier between two phases, the feed or upstream and permeate or downstream side [61]. This permselective barrier has the property to control the rate of transport of different species from the upstream to the downstream side, causing the concentration or purification of one of the species present in the feed gas mixture.

Membrane-based processes offer the advantage of large scale application to separate CO2 from a gas mixture. Figure 2 schematizes the process where concentrated CO2 is selectively separated from flue gas that is mainly composed of nitrogen and carbon dioxide along with other gases such as water vapor, SOx, NOx and methane. Subsequent to the membrane process, concentrated CO2 obtained at the permeate side can be disposed or used as raw material for the synthesis of several chemicals such as fuel and value-added products [62].


Figure 2.

Membrane-based processes for the carbon dioxide separation from flue gases. The concentrated CO2 is obtained in the permeate side.

Of course, the rate of transport or permeation properties of a particular gas through a given membrane depend on the nature of the permeant gas, as well as the physical and chemical properties of the membrane.

Inorganic membranes are more thermally and chemically stable and have better mechanical properties than organic polymer membranes; ceramic membranes offer both the advantage of large scale application and potential for pre- and post-combustion CO2 separation applications, where membranes systems would be operating at elevated temperatures of 300-1000 °C [63].

Inorganic ceramic membranes can be classified as porous and nonporous or dense. These differ from each other not only in their structures but also in the mechanism of permeation. In porous membranes, the transport of species is explained with the pore-flow model, in which permeants are transported by pressure-driven convective flow through the pore network. Separation occurs because one of the permeants is excluded (molecular filtration or sieving) from the pores in the membrane and remains in the retentate while the other permeants move towards the downstream side. On the other hand, in nonporous membranes, separation occurs by solution-diffusion, in which permeants dissolve in the membrane material and then diffuse through the bulk membrane by a concentration gradient [60].

3.1. Porous membranes based on alkaline and alkaline-earth ceramic oxides for CO2 separation

Among the porous systems for CO2 separation, both microporous (carbon, silica and zeolite membranes) and modified mesoporous membranes have been reported [63-64].

Zeolites are hydrous crystalline aluminosilicates that exhibit an intracrystalline microporous structure as a result of the particular three-dimensional arrangement of their TO4 tetrahedral units (T=Si or Al) [65]. Zeolite membranes are commonly prepared as thin films grown on porous alumina supports via hydrothermal synthesis and dry gel conversion methods [66]. Zeolite membranes of different structures have been developed to separate CO2 from other gases via molecular sieving [67-69]. For example, membranes prepared with the 12-member ring faujasite (FAU)-type zeolite show high separation factors of 20-100 for binary gas mixtures of CO2/N2 [69]. In the same sense, T zeolite membranes exhibited very high selectivity, of about 400, for CO2/CH4 and 104 for CO2/N2. The high selectivity of CO2/CH4 exhibited by T zeolites is due to the small pore size of about 0.41 nm, which is similar in size to the CH4 molecule but larger than CO2 [69]. Table 1 shows the kinetic diameter of various molecules that are present in CO2 containing gas mixtures such as flue and natural gas [70].

MoleculeKinetic diameter (Ǻ)
H2 2.69
CO2 3.3
O2 3.46
N2 3.64
CH4 3.80

Table 1.

Kinetic diameter of various molecules based on the Lennard Jhones relationship.

Deca-dodecasil 3R (DDR) (0.36 nm x 0.44 nm), and pseudo-zeolite materials like silicoaluminophosphate (SAPO)-34 (0.38 nm) also show high CO2/CH4 selectivities due to narrow molecular sieving, which controls molecular transport into this material [69, 71-73]. For example, Tomita et al. [74] obtained a CO2/CH4 separation factor of 220 and CO2 permeance values of 7 x 10-8 mol m-2 s-1 Pa-1 at 28 °C on a DDR membrane [75].

As discussed, one of the most important factors controlling permeation through microporous membranes is the restriction imposed by the molecular size of the permeant. However, the transport mechanism in microporous systems is more complex than just size exclusion and the permeation and selectivity properties are also affected by competitive adsorption among perment species that produce differences in mobility [76].

Thus, the diffusion mechanism for gas permeation through microporous membranes can be characterized by two modes: one controlled by adsorption and a second one where diffusion dominates [63]. In the case of adsorption-controlled mode with permeating gases having strong affinity with the membrane, a gas permeation flux equation is obtained by assuming steady-state single gas permeation, a constant diffusivity and a single gas adsorption described by a Langmuir-type adsorption isotherm, as in Eq. (5).

J=ϕqsDcL1+bPf1+bPp or J=ϕqsDcL1-θp1+θf

where J is the permeation flux, ϕ is a geometric correction factor that involves both membrane porosity and tortuosity, Dc is the corrected diffusivity of the permeating species, L is the membrane thickness, Pf and Pp represent the feed and permeate pressure respectively and θf and θp represent the relative occupancies.

Furthermore, if the adsorption isotherm of the permeating gas is linear (1 >> bP), then flux permeation is described by Eq. (6).

where F is the permeance and K = qsb is the adsorption equilibrium constant. Therefore, from Eq. (5) it can be concluded that permeance is determined by both diffusivity (Dc) and adsorption (K). Based on the above, an interesting option to enhance membrane properties is to intercalate zeolite membranes with alkaline and alkaline-earth cations. Zeolite intercalation can enhance the separation between CO2 and other molecules such as N2 by promoting preferential CO2 adsorption [63, 77]. It is well known that zeolites show affinity for polar molecules, like CO2, due to the strong interaction of their quadrupole moment with the electric field of the zeolite framework. In this sense, the adsorption properties of zeolites can be enhanced by the inclusion of exchangeable cations within the cavities of zeolites where the adsorbent-adsorbate interactions are influenced by the basicity and electric field of the adsorbent cavities [78-80]. Lara-Medina et al. [77] carried out separation studies of CO2 and N2 with a silicalite-1 zeolite membrane prepared via hydrothermal synthesis and subsequently modified by using lithium solutions in order to promote preferential CO2 adsorption and diffusion. CO2/N2 separation factor increases from 1.46 up to 6 at 25 psi and 400 ◦C after lithium modification. An et al. [79] studied a series of membranes prepared starting from natural Clinoptilolite zeolite rocks. Disk membranes were obtained by cutting and polishing of the original minerals, which were subsequently chemically treated with aqueous solutions containing Li, Na, Sr or Ba ions. Ionic exchanged membranes showed better permeation properties due to the presence of the extra framework cations.

Although zeolite membranes offer certain advantages in comparison with polymer membranes, such as chemical stability, the main issues are related to the selectivity decrease as a function of the permeation temperature. This is explained in terms of the contribution of the adsorption to the separation, which decreases sharply as temperature increases. At high temperature, physical adsorption becomes negligible and permeation is mainly controlled by diffusion [63, 76]. Additionally, due to the fact that CO2 and N2 molecules have similar sizes (Table 1), the difference in diffusivity is not a strong controlling factor in determining selectivity.

Modified γ-Al2O3 mesoporous membranes have been also reported as a means for CO2 separation [64]. Transport mechanisms in porous membranes have the contribution of different regimes. An overview of the different mechanisms is given in Table 2.

Transport TypePore diameterCharacteristics
Viscous flow>20 μmNon selective.
Affects the total flow resistance of the membrane system.
Molecular diffusion>10 μm
Knudsen diffusion2 – 100 nmOccurs when the mean free path of the molecule is much larger than pore radius of the membrane.
Shows selectivity based on molecular weights.
Surface diffusionShows selectivity due to interaction of molecules with membrane walls.
Capillary condensation
Micropore diffusion (Configurational diffusion)< 1.5 nm

Table 2.

Transport mechanisms in porous membranes.

Depending on the particular system, permeability of a membrane can involve several transport mechanisms that take place simultaneously. Considering no membrane defects and pore sizes in the range of 2.5-5 nm, γ-Al2O3 based membranes theoretically have two transport regimes: Knudsen diffusion and surface diffusion. Eq. (7) describes the permeability of a membrane by taking into consideration the Knudsen and surface diffusion.

F=2εμr3RTL8RTπM0.5+ 2εμDsrA0NavdxsdP

where r is the mean pore radius, μ is a shape factor, R is the universal gas constant, T is the temperature, P is the mean pressure, M is molar mass of the gas, Ao is the surface area occupied by a molecule, Ds is the surface diffusion coefficient, Nav is Avogadro's constant and Xs is the percentage of occupied surface compared with a monolayer [81].

For the cases when Knudsen diffusion dominates, selectivity can be correlated to the molecular weights of the permeating gases by the so called Graham’s law of diffusion, which establishes that the transport rate of any gas is inversely proportional to the square root of its molecular weight. The CO2/N2 separation factor considering pure Knudsen diffusion is given by Eq. (8) and has a value of just 0.8. Therefore, Eq. (8) clearly shows that separation via Knudsen is limited for systems where species are of similar molecular weight.

Based on the aforesaid, CO2/N2 separation factor can be better enhanced by promoting the surface diffusion mechanism (second term on the right hand side of Eq. (7)). Surface diffusion involves the adsorption of gas molecules on the surface of the pore and subsequent diffusion of the adsorbed species along the surface by a concentration gradient. Then separation properties of a membrane can be improved by generating such an interaction between one component of the feed gas mixture with the membrane; one option being via a chemical modification.

Cho et al [81] prepared a series of thin (2-5 μm thickness) γ-Al2O3 and CaO- or SiO2-modified γ-Al2O3 membranes for CO2 separation at temperatures between 25 and 400 °C. Impregnation of membranes with SiO2 or alkaline CaO was done in order to improve the CO2/N2 selectivity by promoting adsorption between CO2 gas molecules and the membrane pore wall. Although this kind of chemical modification of the membrane surface and the pore walls is able to activate the surface diffusion mechanism, an interesting behavior was observed. The CO2/N2 separation factor increased from 1.0 to 1.38 at 25 °C after modification of the γ-Al2O3 with SiO2. On the other hand, CaO impregnated membranes showed a separation factor of 0.98, which is even lower than that of the unmodified γ-Al2O3. The same behavior has been reported by Uhlhorn et al. [82-83]. They reported MgO modified γ-Al2O3 membranes which did not show significant enhancement in the permeation and selectivity properties as a result of the modification process. This fact was explained in terms of the surface diffusion mechanisms. As discussed, it is expected that physicochemical modifications of the membrane can enhance preferential adsorption of the gas species in the feed. Impregnations with alkaline oxide such as calcium oxide or magnesia on the γ-alumina surface give more strong base sites than those promoted by silica. Therefore, it promotes a strong bonding of CO2 on the alumina surface, causing CO2 molecules to lose mobility, resulting in a smaller contribution of surface diffusion to the total transport mechanism.

There is another kind of membrane where alkaline and alkaline-earth ceramic oxides have been used for the fabrication of CO2 permselective membranes. In these cases ceramic materials were chosen because of their well-known properties of physisorption of CO2 at low and intermediated temperatures.

Kusakabe et al. [84] prepared both pure and modified BaTiO3 CO2 permselective membranes via the alkoxide based sol-gel method; impregnation and calcination at 600 °C. In order to establish the effects of CO2 partial pressure, temperature and influence of the secondary oxide presence (CuO, MgO or La2O) on the CO2 adsorption properties of the membranes, pure and modified barium titanate powders were first evaluated by thermogravimetry and chromatography techniques. Dynamic CO2 absorption was evaluated by applying the impulse response method, wherein the BaTiO3 powder was packed in a separation column. The results suggested that the CO2 molecules adsorbed on the BaTiO3 powder are mobile at temperatures about 500 °C. Therefore, this membrane exhibits CO2 permeation due to surface diffusion mechanism. Even though the prepared membranes showed selectivity, the Knudsen diffusion still has an important contribution to the gas transport due to the presence of membrane defects. The maximum separation factor of CO2/N2 through the membranes was estimated as 1.2. Therefore, further improvement of the permeation properties of this kind of membrane requires obtaining pinhole-free membranes.

Based on the same criteria, Nomura et al. [85] prepared Li4SiO4-based thin membranes on porous alumina supports. Membranes were obtained by the thermal treatment of different silica containing porous materials (Silicalite-1 and mesoporous silica) impregnated with lithium compounds. The authors called this method solid conversion. The use of different silica porous sources was proposed in order to enhance the reaction rate of Si and Li on the porous support at relatively low temperature, avoiding the reaction between the Li and alumina support itself. In the case of Silicalite-1 (MFI zeolite), a zeolite thin film was first prepared on the support by following the dry gel conversion technique. Then, the prepared Silicalite-1 layer was impregnated via dipping into a slurry containing lithium and silica fumed reactants (Li:Si = 4:1) and subsequently into a Li2CO3-K2CO3 slurry. The membrane was finally calcined at 600 °C for 2 h. It is believed that carbonate melts to fill the cracks and the pinholes of the Li4SiO4 formed membrane. A similar procedure of coating and calcination was carried out to prepare high quality membranes starting from mesoporous silica sources with pore sizes of 1.8-12.8 nm. Precursors react to form a Li4SiO4 membrane of 2-5 μm thickness that exhibits an N2 permeance of 1.8 x 10-9 mol m-2 s-1 Pa-1 at 400 °C. This suggests there are no big defects after impregnation of the membrane with the binary mixture of Li2CO3-K2CO3carbonate. Due to the fact that the membrane operates in a rich CO2 atmosphere, carbonates do not decompose even at temperatures of 600 °C. The maximum CO2/N2 permeance ratio was 0.85. The separation factor was higher than that for the Knudsen diffusion. Therefore, it can be conclude that Li4SiO4 layer was selective to CO2 over N2 at high temperature of 600 °C.

Nomura [86] reported a two -stage approach for the preparation of Li4SiO4-CO2 selective membranes that involves the fabrication of a supported Li4SiO4 membrane and its subsequent modification by using a chemical vapor deposition (CVD) method. First, for the preparation of a thin Li4SiO4 membrane the so called solid conversion method described before was used, which is based on the reaction between a porous silica source and a lithium containing solution coated on a porous alumina membrane support. Although the formed membranes showed certain selectivity due to the preferential adsorption of CO2 over N2, the presence of pinholes and cracks caused low separation factors. Therefore, the membrane defects were fixed by using the counter diffusion CVD method to form a silica coating that fills the gaps between the lithium orthosilicate particles that make up the membrane. N2 permeance was reduced about three orders of magnitude after CVD modification. Nitrogen permeance before and after the CVD treatment was 3.4 x 10-6 mol m-2 s-1 Pa-1 and 1.2 x 10-9 mol m-2 s-1 Pa-1 respectively. In the same sense, the CO2/N2 permeance rate increased from 0.7 to 1.2 at 600 °C. Some issues related with this system are the chemical and structural stability of the membranes observed during the permeation tests at elevated temperature. The membranes were broken when permeation tests were carried out at temperatures higher than 700 °C, with the consequent decrease in the CO2/N2 selectivity. The aforesaid is the result of the CO2 chemisorption on the membrane. Lithium orthosilicate reacts with CO2 to form lithium carbonate and lithium metasilicate (Li2SiO3) as products, as indicated by Eq. (9).

Li4SiO4+ CO2 Li2CO3+ Li2SiO3

Thermodynamically, this reaction is prone to occur at temperatures between room temperature and about 700 °C. However, experimentally it has been observed that reaction kinetics sharply increase above 550 °C. At these temperatures, the formation of carbonates involves an important change in volume that ends in the membrane’s rupture.

Therefore, one of the issues related to the development of this kind of inorganic membrane is the thermochemical stability. Due to reactivity of alkaline and alkaline-earth ceramic oxides with CO2 to form carbonates, not only preferential adsorption of CO2 molecules over N2 occurs, but CO2 chemisorption and reaction.. Therefore, it is mandatory to establish the operational temperature within a range where CO2 selective adsorption on the membrane layer promotes the separation process without reaction.

3.2. Nonporous membranes based on alkaline and alkaline-earth ceramic oxides for CO2 separation

Some researchers have proposed the use of alkaline and alkaline-earth ceramic oxides to prepare membranes that are able to separate CO2 at high temperatures via a different transport mechanism than those observed on porous membranes. Li2ZrO3 and Li4SiO4 based membranes are examples of the aforesaid. Permselectivity of CO2 through these membranes takes place not only due to the selective CO2 adsorption properties of ceramic phases but also via a mechanism of gas separation that involves the transport of CO32- and O2- ionic species through the electrolytes (carbonate-metal oxide) phases formed by the reaction of the membrane with the CO2 [87-89].

Kawamura et al. [87] fabricated and characterized a membrane for CO2 separation at high temperatures. The membrane was made of lithium zirconate (Li2ZrO3), an alkaline ceramic oxide that reacts with CO2 to produced Li2CO3 and ZrO2. These two reaction products are electrolyte materials produced in-situ when the membrane is exposed to the rich carbon dioxide atmosphere. The electrolytes formed thus are capable to transport both CO2 and O2 across the membrane via a dual ion conduction mechanism. The prepared membrane exhibited a separation factor of 4.9 between CO2 and CH4 gas molecules at a temperature of 600 °C. The obtained separation factor is higher than the Knudsen diffusion limit, 0.6. Therefore, the results clearly suggest the potential use of this kind of membrane system for CO2 separation such as the case of CO2 removal from natural gas.

Yamaguchi et al. [88] investigated the concept of the dual-ion conduction facilitated mechanism previously observed for the case of Li2ZrO3 membranes by focusing their efforts on the preparation of a CO2 permselective membrane based on lithium orthosilicate (Li4SiO4). The supported membrane was prepared via a dip coating technique by using Li4SiO4 suspensions. The coating process was repeated several times before impregnation of the membrane with a Li2CO3/K2CO3 carbonate mixture and final sintering at 750 °C. In this membrane system, Li4SiO4 reacts in-situ with CO2 to form Li2CO3 and Li2SiO3.

Gas separation studies were performed by using CO2/N2 mixtures as feed gas. The observed CO2 permeance values were about 1 x 10-8 mol m-2s-1Pa-1 in the temperature range of 525-625 °C. The CO2/N2 separation factor was estimated between four and six. Figure 3 shows a scheme of the dual-ion conduction mechanism explained as follows. In the feed side, carbon dioxide dissolves in the material and diffuses as carbonate ions through the molten carbonate electrolyte due to a concentration gradient. Then, in the downstream side of the membrane, the formation of gaseous CO2 implies the formation of oxygen ions which must diffuse back to the feed side across the membrane and apparently through the formed Li2SiO3 skeleton to obtain the charge balance.


Figure 3.

Schematic representation of a membrane system for the CO2 separation via a dual-ion conduction mechanism.

The proposed transport mechanisms supports the higher selectivity values observed in the permeation test for both systems, Li2ZrO3 and Li4SiO4. Figure 4 shows the separation factor values (CO2/N2) obtained for different ceramic membranes described in the present report. The pure Knudsen value is written as baseline and separation factor of nonporous Li4SiO4 for comparison purposes. However, it is important to mention that the oxygen ion diffusion process is not totally clear. Indeed, there is no experimental study regarding the oxygen ionic conductivity properties of Li2SiO3 phase. On the other hand, pure ZrO2 exhibits poor bulk oxygen ion conductivity. In fact, good conduction properties are observed only in acceptor-doped ZrO2 based materials with oxygen vacancies being the predominant charge carriers [90]. Therefore, oxygen ion conduction through the membrane must be related to different transport paths, such as grain boundaries and interfacial regions formed between the ceramic and molten carbonate on the membrane.


Figure 4.

CO2/N2 separation factor of different ceramic oxide membranes.

More recently, the promising concept of ceramic oxide-carbonate dual-phase membranes has been proposed for carbon dioxide selective separation at intermediate and high temperatures (450-900 °C) [91-97].

This concept involves the fabrication of nonporous membranes capable of selectively separating CO2 via its transport, as carbonate ions. Dual phase membranes are made of an oxygen ion conductive porous ceramic phase that hosts a molten carbonate phase. Rui et al. [98] proposed the CO2 separation by the electrochemical conversion of CO2 molecules to carbonate ions (CO32-), which are subsequently transported across the membrane. Carbonate ionic species (CO32-) are formed by the surface reaction between CO2 and oxygen that comes from the ceramic oxide phase (feed side, Eq.(10)) and then transport of CO32- takes place through the molten carbonate.

CO2+ OOx CO32-+ VO¨

Once carbonate ions have reached the permeate side, molecular CO2 is released to the gas phase, delivering OOx species back to the ceramic oxide solid phase. This process takes place due to a chemical gradient of CO2 in the system (Figure 5). Here, it is important to emphasize that dual-phase membranes are nonporous and therefore exhibit high separation selectivity as a result of the transport mechanism. Figure 5 also shows the SEM image of the cross section of a ceramic oxide-carbonate membrane prepared by pressing La0.6Sr0.4Co0.8Fe0.2O3-δ powders and subsequent infiltration of the obtained porous ceramic (bright phase) with carbonate (dark phase).


Figure 5.

Schematic representation of a membrane system for the CO2 separation and SEM image of a ceramic oxide-carbonate dual-phase membrane

Table 3 summarizes the different studies reported and certain advances that have been achieved so far regarding the dual-phase membrane concept. This table also includes the Li2ZrO3 and Li4SiO4 nonporous membranes previously described. Although the original reports do not clearly explain the operational mechanism [26-27], the dual-phase membrane concept gives a much better idea of the possible phenomenology involved [30,33,36].

Ceramic Oxide phaseMolten Carbonate phaseMembrane featuresPreparation methodPermeance (mol.s.-1m.-2Pa.-1)Separation Factor (CO2/N2)Ref.
Li2ZrO3 Li2CO3 Thick membrane In situ by exposing Li2ZrO3 to CO2 atmosphere1 x10-8 4.9
(CO2/CH4 at 600°C)
Li4SiO4/Li2SiO3 K2- Li2CO3 Thin supported membraneImpregnation of carbonate2x10-8 5.5
(at 525°C)
La0.6Sr0.4Co0.8Fe0.2O3-δ Li-Na-K2CO3 Thick membrane
(0.35-1.5 mm)
Pressing and direct infiltration4.77 x 10-8 225
(at 900°C)
8 mol% Yttria doped zirconia (YZS)
10 mol% Gadolinia doped ceria (GDC)

Thin freestanding membranes
(200-400 μm)
Tape casting and in situ infiltration2.0 x10-8 (YSZ)
3.0 x10-8 (GDC)
> 2
(at 800 °C)
Ce0.8Sm0.2O1.9 Na2- Li2CO3 Thick membrane
(1.2 mm)
Pressing of SDC-NiO powders where NiO is a sacrificial template~1.2 x 10-6 155-255
(at 700°C)
Bi1.5Y0.3Sm0.2O3 Li-Na-K2CO3 Thin supported membrane
(50 μm)
Dip coating of modified thick support and infiltration1.1 x 10-8 2
(at 650°C)
8 mol% Yttria doped zirconia (YZS)
Li-Na-K2CO3 Thin supported membrane
(10 μm)
Dip coating of YSZ on nonwettable thick support and infiltration~ 7.8×10−8 ---[95]
Ce0.8Sm0.2O1.9 Li-Na-K2CO3 Thin tubular membraneCentrifugal casting and direct infiltration[96]
La0.6Sr0.4Co0.8Fe0.2O3-δ Li-Na-K2CO3 Thick disk-shaped membranePressing and direct infiltration[97]

Table 3.

Reported studies on dual-phase and related membranes for CO2 separation.

3.3. Applications of CO2 permselective ceramic oxide membranes for the design of membrane reactors.

As mentioned, CO2 can be used as raw material for the synthesis of several chemicals [99]. Moreover, if CO2 is concentrated or separated by a membrane system exhibiting high CO2 permeation and permselectivity, this open up the possibility to develop a continuous process of membrane reaction to simultaneously capture and chemically convert CO2. For example, if the membrane is able to separate CO2 at intermediate and even high temperatures, it can be used for the design of a membrane reactor for the production and purification of hydrogen and syngas. Syngas is a gaseous fuel with a main chemical composition of CO, H2, CO2, and CH4. Syngas can be used as feedstock for the synthesis of several other clean fuels such as H2, methanol, ethanol, diesel and other hydrocarbons synthesized via the Fischer-Tropsch process [100-104].

Among the different processes for the synthesis of syngas and hydrogen, CO2 methane reforming Eq. (11) and the water-gas shift reaction (WGS) Eq. (12) are the most promising options.

CH4+ CO2 2CO + 2H2
CO + H2 CO2+ H2

Figure 6 schematizes the membrane reactor concept considering the two reactions described above. Figure 6A shows a membrane reactor for dry reforming of methane to produce syngas at temperatures between 700 and 800 °C. Figure 6B illustrates the use of ceramic oxide membranes for hydrogen purification by separating the CO2 from water-gas shift products at about 550 °C. Additionally, Figure 6B shows the possibility of using a ceramic sorbent to chemically trap the permeate CO2 and therefore enhance the CO2 permeation process by reducing the concentration of CO2 in the permeate side.


Figure 6.

Schematic representation of the membrane reactor concept using a CO2 permselective ceramic membrane: (a) CO2 dry methane reforming and (b) water-gas shift reaction with hydrogen purification wherein CO2 capture promotes the separation process.

4. Chemical transformation of CO2 catalyzed by ceramic materials: the use of new alternatives.

One of the most widely used chemical absorption techniques for carbon capture and storage/sequestration (CCS) is CO2 adsorption by ceramic materials. Once CO2 has been captured-fixed, it can be converted into value-added products such as precursors in chemical transformation reactions. CO2 is extensively used for enhanced oil recovery, as a monomer feedstock for urea and polymer synthesis, in the food and beverage industry as a propellant, and in production of chemicals. Therefore, the capture-fixation of CO2 would make a system suitable for accomplishing chemical transformation of CO2. The utilization of carbon dioxide is also very attractive because it is environmentally benign [105-115]. CO2 conversion to fuel and value-added products is an ideal route for CO2 utilization due to the simultaneous disposal of CO2 and the benefit that many products can be used as alternate transportation fuels [116]. CO2 chemical transformation methods include (i) reverse water-gas shift, (ii) hydrogenation to hydrocarbons, alcohols, dimethyl ether and formic acid, (iii) reaction with hydrocarbons to syngas, (iv) photo- and electrochemical/catalytic conversion, and (v) thermo-chemical conversion [100-122].

CO2 can be catalyzed to valuable organic or inorganic compounds, where some basic catalytic materials (containing alkaline or alkaline-earth elements) are used. The activation of CO2 by alkali metals has received considerable attention in various surface science studies, which have demonstrated the formation of intermediate CO2, dissociation of CO2 and formation of oxalate and carbonate alkali compounds [118-121]. Carbon dioxide has been identified as one such potential vector molecule (through reduction to syngas, methanol, methane, formic acid, formaldehyde, dimethylether (DME) and short-chain olefins) [117-118, 120-122]. CO2 is a kinetically and thermodynamically stable molecule, so CO2 conversion reactions are endothermic and need efficient catalysts to obtain high yield. CO2 conversion to carbon monoxide (CO) looks like the simplest route for CO2 reduction [121]. CO is a feedstock or intermediate product for the production of methanol and hydrocarbon fuels via Fischer-Tropsch synthesis of CH4/CO2 reforming to form syngas (CO/H2) [122]. CO2 reforming with CH4 is an example of CO2 being used as a soft oxidant, where the dioxide is dissociated into CO and surface oxygen, and oxygen abstracts hydrogen from methane to form water via the water-gas shift reaction (WGS) (Eqs. 11 and 12) [100-103, 121]. The catalytic chemistry of the reverse water-gas shift reaction and the following transformation to methanol/DME (or hydrocarbons via Fischer-Tropsch synthesis), and the subsequent production of gasoline (methanol-to-gasoline or diesel via hydrocracking of the alkanes produced in the Fisher-Tropsch process) are well established [102, 117-122]. On the other hand, methanol can be produced directly from carbon dioxide sources by catalytic hydrogenation and photo-assisted electrochemical reduction. A wide variety of CO2 photo-reduction methods have been performed to oxygenate products, including formic acid (HCOOH) and formaldehyde (HCHO). HCOOH and HCHO are the simplest oxygenates produced from the reduction of CO2 with H2O (or proton solvents) [121]. Furthermore, CO2 can be utilized as a monomeric building block to synthesize various value-added oxygen-rich compounds and polymers under mild conditions. As an example, chemical conversion of CO2 through C–N bond formation can produce value-added chemicals such as oxazolidinones, quinazolines, carbamates, isocyanates and polyurethanes [105]. These commodity chemicals have been synthesized from green methods and have important applications in the pharmaceutical and plastic industries. The chemisorption of CO2 based on C–N bond formation could be one of the most efficient strategies, utilizing liquid absorbents such as conventional aqueous amine solutions, chilled ammonia, amino-functionalized ionic liquids, and solid absorbents including amino-functionalized silica, carbon, polymers and resins. The processes by which chemicals for CO2 capture are manufactured should also be considered in terms of their energy requirements, efficiencies, waste products, and CO2 emissions [105, 123]. In that sense, dimethyl carbonate (DMC) is a promising target molecule derived from CO2 catalyzed by inorganic dehydrating agents such as molecular sieves [107]. Dimethyl carbonate has received much attention as a safe, non-corrosive, and environmentally friendly building block for the production of polycarbonates and other chemicals, an additive to fuel oil owing to its high octane number and an electrolyte in lithium batteries due to its high dielectric constant. It can be synthesized through a two-step transesterification process utilizing CO2 as raw material [105, 107].

As a complementary technology to carbon sequestration and storage (CSS), the chemical recycling of carbon dioxide to fuels is an interesting opportunity. Chemical compounds such as alkane products (CnH(2n+2)) are un-branched hydrocarbons suitable for diesel fuel and jet fuel [121]. In this regard, biofuels or biodiesel, catalyzed using ceramic materials, can provide a significant contribution in energy independence and mitigation of climate change [109-127]. Today the main renewable biofuels are bioethanol and biodiesel. Biodiesel is a liquid fuel consisting of mono alkyl esters (methyl or ethyl) of long-chain fatty acids derived from vegetable oils, animal fats or micro and macro algal oils [127]. Biodiesel is a sustainable, renewable, non-toxic, biodegradable diesel fuel substitute that can be employed in current diesel engines without major modification, offering an interesting alternative to petroleum-based diesel [106, 111-115, 124-128]. Besides this, it is free from sulfur and aromatic components, making it cleaner burning than petroleum diesel. Biodiesel has a high flash point, better viscosity and caloric power similar to fossil fuels. It can be mixed with petroleum fossil fuel at any weight ratio or percentage, and it can be used without blending with fossil fuel (B100) as a successful fuel [127, 128]. It has similar properties (physical and chemical) to petroleum diesel fuel. Recently, transesterification (also called alcoholysis) has been reported as the most common way to produce biodiesel with lipid feedstock (such as vegetable oil or algal oil) and alcohol (usually methanol or ethanol), in presence of an acid or base catalyst. Transesterification is the best method for producing higher-quality biodiesel and glycerol [108, 110-115, 124-132]. The reaction is facilitated with a suitable catalyst [129-131]. The catalyst presence is necessary to increase both, the reaction rate and the transesterification reaction conversion yield. The catalysts are classified as homogeneous or heterogeneous. Homogeneous catalysts act in the same liquid phase as the reaction mixture. Conversely, if the catalyst remains in a different phase, the process is called heterogeneous catalytic transesterification [113, 127-131]. Heterogeneous catalysts are mostly applied in transesterification reaction due to many advantages such as easy catalyst separation and reusability, improved selectivity, fewer process stages, no water formation or saponification reaction, including in green technology, and cost effectiveness [127, 132]. The heterogeneous catalysts increase the mass transfer rate during the transesterification reaction [127, 131]. Various ceramic materials have been investigated for the production of biodiesel [106, 109-115, 124-179]. Some of these solid catalysts include alkali and alkaline-earth metal carbonates and oxides such as magnesium oxide (MgO), calcium oxide (CaO), barium oxide (BaO), strontium oxide (SrO) [124-131, 133-143]; lithium base ceramics (Li4SiO4 and Li2SiO3 [144-146]); sodium silicate (Na2SiO3 [147]); transition metal oxides and derivatives (titanium oxide, zinc oxide, mixed oxides catalysts [148-149]); ion exchange resin type acid heterogeneous catalysts [150]; MCM-metal impregnated materials [114]; layered double hydroxides (hydrotalcite-like hydroxides) [151-154]; hydrocalumite-like compounds [110,155]; supported bases [156-163]; and zeolites [164-165].

Among the alkaline earth metal oxides, CaO is a promising basic heterogeneous catalyst for synthesizing biodiesel at mild temperatures (below the boiling point of methanol, MeOH) and at atmospheric pressure due to its plentiful availability and low cost, but it is rapidly hydrated and carbonated upon contact with room temperature air. CaO is the most widely used catalyst for transesterification and produces a high yield of 98% of fatty acid methyl esters (FAME) during the first cycle of reaction [130]. Granados et al. [142] used activated CaO as a solid base catalyst in the transesterification of sunflower oil to investigate the role of water and carbon dioxide on the deterioration of the catalytic performance upon contact with air for different periods. The study showed that CaO was rapidly hydrated and carbonated in air. Consequently, the reusability of the catalyst for subsequent steps is a big question mark. Di Serio et al. [170] reported a 92% biodiesel yield with MgO catalyst, using 12:1 methanol to oil molar ratio with 5.0wt% of the catalyst at methanol supercritical condition for 1 h. Wen et al. [171] carried out transesterification from waste cooking oil with methanol at 170 °C for 6 h with 10wt% of MgO/TiO2 and 50:1 M ratio of MeOH and oil. Guo et al. [172] studied the methyl ester yield produced via transesterification of soybean oil using sodium silicate as a catalyst. Sodium silicate was an effective catalyst for the microwave-irradiated production of biodiesel and hydrothermal production of hydrogen from by-product glycerol combined with Ni catalyst. The optimum reaction conditions obtained were 7.5:1 M ratio of alcohol/oil, 3wt% catalyst amount, 1 h reaction time and 60 °C reaction temperature. The FAME yield was ~100%. On the other hand, microwave-assisted transesterification of vegetable oil with sodium silicate is an effective and economical method for the rapid production of biodiesel. The reused catalyst after transesterification process for four cycles was recovered. Overall, sodium silicate was fully used in biodiesel production and glycerol gasification, and this co-production process provided a novel green method for biodiesel production and glycerol utilization [172].

Several techniques have been investigated for the transesterification reaction using heterogeneous catalysts for biodiesel production, as follows: transesterification via radio frequency microwaves, alcohol reflex temperature, alcohol supercritical temperature and ultrasonication [127, 173-177]. Recently, the use of ultrasonic irradiation has gained interest in biodiesel production [173-177]. Ultrasonic energy can emulsify the reactants to reduce the catalyst requirement, methanol-oil ratio, reaction time and reaction temperature and also provides the mechanical energy for mixing and the required activation energy for initiating the transesterification reaction [173-176]. The ultrasound phenomenon has its own physical and chemical effects on the liquid-liquid heterogeneous reaction system through cavitation bubbles, according to the following principles [175]: (1) the chemical effect, in which radicals such as H+ and OH- are produced during a transient implosive collapse of bubbles (in a liquid irradiated with ultrasound), which accelerates chemical reaction in the bulk medium; and (2) the physical effect of emulsification, in which the microturbulence generated due to radial motion of bubbles leads to intimate mixing (homogenizing the mixture) of the immiscible reactants. Accordingly, the interfacial region between the oil and alcohol increases sharply, resulting in faster reaction kinetics and higher conversion of oil and biodiesel yield [127]. In 2000, the ultrasonication reactor was first introduced by Hielscher Ultrasonic GmbH for biodiesel production. Nishimura et al. [175] studied the transesterification of vegetable oil using low-frequency ultrasound (28-40kHz). An excellent yield (~98%) was obtained at a 28 kHz ultrasound while a significant reduction of reaction time was obtained by using 40 kHz ultrasound. Salamatinia et al. [176] used ultrasonic assisted transesterification to improve the reaction rate. In this study, they used SrO and BaO as heterogeneous catalysts in the production of biodiesel from palm oil. The results showed that the basic properties of the catalyst were the main cause for their high activity. The low-frequency ultrasonic assisted transesterification process had no significant mechanical effects on SrO, but BaO catalyst study confirmed that the ultrasound treatment significantly improved the process by reducing the reaction time to less than 50 min at a catalyst loading of 2.8wt% to achieve biodiesel yield higher than 95%. Another study of alkali earth metals was carried out by Mootabadi et al. [177]. They reported the effect of ultrasonic waves at 20 kHz and 200W on the regenerated catalyst and compared mechanical stirring and ultrasonic irradiation. They investigated the optimum conditions, using palm oil for biodiesel production with catalysts such as CaO, SrO and BaO. They concluded that catalyst leaching was the main cause for the catalyst inactivity in the case of the re-used catalyst. BaO catalyst was found to be stable during the leaching. At the optimized condition, 95.2% yield was achieved with 60 min of reaction time for both BaO and SrO catalysts. For CaO catalyst, 77.3% yield was achieved with the same conditions. The use of ultrasound showed great enhancement of the reaction parameters in terms of the obtained yield and reaction time. The obtained yields were 30 to 40% higher in comparison to the corresponding results obtained using a conventional stirring reactor system without ultrasonication. Deng et al. [178] prepared nano-sized mixed Mg/Al oxides. Due to their strong basicity, the nanoparticles were further used as catalyst for biodiesel production from jatropha oil. Experiments were conducted with the solid basic catalyst in an ultrasonic transesterification reaction. Under the optimum conditions, biodiesel yield was 95.2%. After removing the glycerol on the catalyst surface, the nano-sized mixed Mg/Al oxides were reused eight times. The authors concluded that calcination of hydrotalcite nanocatalyst under ultrasonic radiation is an effective method for the production of biodiesel from jatropha oil. The activity of base solid catalysts is associated to their basic strength, such that the most basic catalyst showed the highest conversion. In another work, Deng et al. [179] reported optimum conditions for biodiesel production in the presence of base solid catalysts. They studied BaO and Ca–Mg–Al hydrotalcite (the most effective). The 95% biodiesel yield from jatropha oils and Ca–Mg–Al hydrotalcite was established with 30 min of reaction time. Ca–Mg–Al hydrotalcite could be reused twelve times after washing of the adsorbed glycerol from the catalyst surface with ethanol. Other types of heterogeneous catalysts under ultrasonic irradiation were used for transesterification by Georgogianni et al. [114]. They studied a wide range of catalysts including Mg-MCM-41, Mg–Al hydrotalcite and K+-impregnated zirconium oxide. They mixed frying oils, methanol and the catalyst in a batch reactor with mechanical stirring for 24 h and with ultrasonication for 5 h. The results suggested that the basic strength was the cause of the good activity of the catalysts. Mg–Al hydrotalcite achieved the highest reaction conversion of 87% at a reaction temperature of 60 °C. Overall, ultrasonic irradiation significantly enhanced the reaction rate, causing a reduction in reaction time, and the biodiesel yield increased [114]. Consequently, a better understanding of the use of ultrasonic sound waves to accelerate the transesterification process could lead to substantial future improvement of both batch and continuous production systems, to obtain a more sustainable biodiesel production process [127].


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