Biogas Management: Advanced Utilization for Production of Renewable Energy and Added-value Chemicals

Biogas is widely available as a product of anaerobic digestion of urban, industrial, animal and agricultural wastes. Its indigenous local-base production offers the promise of a dispersed renewable energy source that can significantly contribute to regional economic growth. Biogas composition typically consists of 35–75% methane, 25–65% carbon dioxide, 1–5% hydrogen along with minor quantities of water vapor, ammonia, hydrogen sulfide and halides. Current utilization for heating and lighting is inefficient and polluting, and, in the case of poor quality biogas (CH₄/CO₂ < 1), exacerbated by detrimental venting to the atmosphere. Accordingly, innovative and efficient strategies for improving the management and utilization of biogas for the production of sustainable electrical power or high added-value chemicals are highly desirable. Utilization is the focus of the present review in which the scientific and technological basis underlying alternative routes to the efficient and eco-friendly exploitation of biogas are described and discussed. After concisely reviewing state-of-the-art purification and upgrading methods, in-depth consideration is given to the exploitation of biogas in the renewable energy, liquid fuels, transport and chemicals sectors along with an account of potential impediments to further progress.

Biogas

Efficient management of ever-increasing amounts of municipal, industrial and agricultural wastes in order to minimize their environmental impact is an urgent necessity. Biological treatment of wastes, which can be carried out either aerobically or anaerobically, is widely applied in this area. Due to their several advantages the anaerobic processes are to be preferred because they require considerably smaller installations, produce less sludge, operate at lower temperatures and are suited to periodic operation. Much more importantly, they generate biogas, which is an attractive potential source of renewable energy and/or added-value chemicals due to its high content of methane and CO₂. Anaerobic digestion (AD) can proceed over a wide temperature range, from phychrophilic (ca. 10–20°C) and mesophilic (ca. 20–45°C) up to thermophilic (ca. 45–65°C) and hyperthermophilic (ca. ~70°C) levels, by means of cooperation between anaerobes and facultative anaerobe microorganisms, which successively promote a sequence of hydrolysis-acidogenesis, acetogenesis and finally methanogenesis, that lead to biogas formation (Abatzoglou and Boivin, 2009; Weiland, 2010; Mao et al., 2015; Salihu and Alam, 2015). The quality of biogas, the digestion rate, the process stability, the richness in bacteria and the effectiveness in treating substrates containing lipids, proteins and nonbiodegradable solid matter, are parameters that are in principle influenced by both the pretreatment of the organic feedstocks and the AD operation temperature (Dareioti et al., 2009; Stamatelatou et al., 2010, 2012; Mao et al., 2015; Croce et al., 2016). Therefore, two-stage anaerobic digestion processes are often considered to be the optimal combination, namely thermophilic hydrolysis/acidogenesis and mesophilic methanogenesis.

Depending on the source of raw biomass and the particular treatment process, the biogas composition typically lies within the ranges CH₄ = 35–75%, CO₂ = 25–65%, H₂ = 1-5%, N₂ = 0.3–3% (Table 1) along with traces of water vapor, NH₃, H₂S, and mercaptans (e.g., CH₃SH), halides and siloxanes (Abatzoglou and Boivin, 2009; Petersson and Wellinger, 2009). The amounts of these contaminants strongly depend on the biomass source and its treatment: they play a crucial role in determining biogas quality and its ultimate economic value, due to problems of fouling, corrosion and erosion when used in thermal or catalytic systems. Environmental pollution from hazardous secondary pollutants produced by the use of a raw biogas is another important issue. Accordingly, removal of contaminants is a necessary precursor to biogas utilization, and if it involves the removal of CO₂ as well, the process is referred in the literature as biogas upgrading.

TABLE 1

Table 1. Chemical composition of several origin biogases and natural gases.

The most undesirable biogas impurities are H₂S and other S-containing compounds with a typical concentration in the range 0.0001–1%vol, originating from the anaerobic fermentation of S-bearing proteins (Abatzoglou and Boivin, 2009). Although much research has been carried out to develop H₂S-tolerant materials for the catalytic utilization of biogas, achieving H₂S reduction to the level of 10–100 ppmv remains a highly desirable goal.

Siloxanes, which are a case-sensitive biogas contaminant, are mostly found in gas originating from landfill and composting sites. Failure to remove siloxane impurities causes significant problems in both automotive engines and in catalytic/electrocatalytic systems due to the formation of silica microparticulates. It is therefore of crucial importance to remove siloxanes from biogas intended for energy or added-value chemical vectors.

Less harmful than H₂S and siloxanes, but also corrosive and a health risk, the NH₃ present in biogas results from anaerobic fermentation of N-containing organics. Ammonia itself is readily combusted or catalytically decomposed producing heat and/or electrical power in fuel cell applications of biogas. Therefore, it is not generally an important factor under operating conditions—however NH₃-derived NOx remains a potential pollutant that requires attention. The remaining contaminants in biogas may be considered of much lesser significance for most uses of biogas.

The thermal heating value of biogas varies between 15 and 30 MJ/m³, close to that of natural gas (Table 1); 1 m³ of biogas is equivalent to about 0.6 L of gasoline. It is often described as Renewable Natural Gas (RNG) or Substituted Natural Gas (SNG) or even biomethane, since it is a pipeline-quality gas, which, after upgrading is fully equivalent to and interchangeable with natural gas so that it can partially substitute the latter in transport applications or grid injection. Accordingly, along with natural gas, biogas may be considered as a “bridge fuel” for the twentieth century, enabling the transition to a low-carbon energy economy, currently playing a key role in the emerging market for renewable energy. As a result, biogas purification and upgrading has been a prominent research topic in recent years. A number of comprehensive reviews are available including those provided by Abatzoglou and Boivin (2009), Ryckebosch et al. (2011), Sun et al. (2015); Andriani et al. (2014) and Salihu and Alam (2015). However, although biogas purification and upgrading has been extensively reviewed, its advanced utilization as a renewable energy vector and for the production of added-value chemicals has received much less attention. The latter aspect is the principal focus of the present review: after concisely reviewing state-of-the-art purification and upgrading methods, in-depth consideration is given to the exploitation of biogas in the renewable energy and chemicals sectors. With respect to the former, particular emphasis is given to direct biogas solid oxide fuel cells which currently attract much research effort, although the information dispersed in the primary literature rather in reviews. Concerning the latter, the most promising potentially practical and environmentally benign utilization routes are reviewed here and an informative process sequence network is provided. Although some of the chemical routes are not new, they have not been previously considered for biogas utilization—for example transformation of biogas to ethylene via one-step process.

Biogas Purification

Biogas purification processes comprise mainly physical and chemical methods, but biological techniques capable of being effectively and economically applied even at small scales are also available (Abatzoglou and Boivin, 2009; Osorio and Torres, 2009; Salihu and Alam, 2015). Gas absorption, scrubbing or washing with specific liquid solvents, physical or chemical adsorption on high surface area solids, condensation (cryogenic separation), membrane separation, catalytic conversion, and biofiltration are the methods involved. Biogas upgrading is rapidly spreading all over the word; Petersson and Wellinger (2009) and Salihu and Alam (2015) provide information about current plant operations and distribution in a number of countries.

Here we focus on the principal contaminants that have to be removed in biogas purification processes, i.e., H₂S and siloxanes, and the main methodologies are summarized below.

H₂S Removal

H₂S removal via reactive-absorption techniques (passage of biogas through alkaline solutions—NaOH, CaO) is not a feasible method. This is because it is not a selective process; CO₂ also reacts with alkaline solutions and would thus consume the costly alkalis. Moreover, as we shall see, CO₂ is itself an economically valuable biogas component that can be used for cultivation of agricultural plants or for the production of added-value products by means of appropriate upgrading.

Various types of activated carbon have been investigated for H₂S removal mainly by adsorption/oxidation to produce elemental sulfur and to a lesser extent by conversion to SO₂ (Bagreev and Bandosz, 2001; Bashkova et al., 2007; Xiao et al., 2008; Pipatmanomai et al., 2009; Kwansy and Balcerzak, 2016). Pore structure and surface characteristics as well as nitrogen content of the activated carbon affect both H₂S breakthrough capacity and selectivity toward elemental sulfur formation (Bashkova et al., 2007). On the other hand, Bagreev et al. (2001) concluded that the surface chemistry, specifically the surface acidity, of activated carbon seems to be the key factor that plays the dominant role in the H₂S breakthrough capacity, rather than surface area and pore volume characteristics. The relative humidity of the gas stream and alkali-impregnation were also found to be crucial to the performance of activated carbons used for H₂S removal (Xiao et al., 2008; Pipatmanomai et al., 2009). A reaction pathway for H₂S oxidation over activated carbon that involves the participation of all three vapor-liquid-solid phases has been proposed by Bagreev et al. (2001) and Xiao et al. (2008). The liquid phase consists of an extremely thin water film formed on the AC surface via water vapor condensation into which H₂S dissolves prior of its dissociation toward H⁺ and HS⁻ ions. Then a surface reaction occurs between HS⁻ and dissociatively adsorbed oxygen (O_ads*) on the activated carbon active sites (*) forming elemental sulfur and water at the edge of the liquid film. Some of the HS⁻ ions is are also oxidized to H₂SO₄. The net results is

$\begin{array}{ll}{\text{H}}_2\text{S}+{½\text{O}}_2\to \text{S}+{\text{H}}_2\text{O and }{\text{H}}_2\text{S}+{2\text{O}}_2\to {\text{H}}_2{\text{SO}}_4& (\text{R}1)\end{array}$

According to Bagreev et al. (2001) and Xiao et al. (2008) the steps involved are as follows, where * is an active site on the AC surface.

$\begin{array}{ll}{\text{H}}_2\text{S}(\text{g})\to {\text{H}}_2{\text{S}}_{\text{abs}-\text{liquid}}& (\text{R}2)\end{array}$

$\begin{array}{ll}{\text{H}}_2{\text{S}}_{\text{abs}-\text{liquid}}\to {\text{H}}^{+}+{\text{HS}}^{-}& (\text{R}3)\end{array}$

$\begin{array}{ll}{\text{O}}_2(\text{g})+\ast \to {\text{O}}_{\text{ads}}\ast & (\text{R}4)\end{array}$

$\begin{array}{ll}{\text{HS}}^{-}+{\text{O}}_{\text{ads}}\ast \to {\text{S}}_{\text{ads}}\ast +{\text{OH}}^{-}& (\text{R}5)\end{array}$

$\begin{array}{ll}{\text{HS}}^{-}+3{\text{O}}_{\text{ads}}\ast \to {\text{SO}}_{2\text{ads}}\ast +{\text{OH}}^{-}& (\text{R}6)\end{array}$

$\begin{array}{ll}{\text{SO}}_{2\text{ads}}\ast +3{\text{O}}_{\text{ads}}\ast +{\text{H}}_2\text{O }\to {\text{H}}_2{\text{SO}}_4& (\text{R}7)\end{array}$

$\begin{array}{ll}{\text{H}}^{+}+{\text{OH}}^{-}\to {\text{H}}_2\text{O}& (\text{R}8)\end{array}$

The importance of water on the AC surface is clear from the above mechanism and explains why both relative humidity (RH) and the ability of the AC surfaces to adsorb water have a major influence on H₂S removal efficiency. Low RH values or hydrophobic AC surfaces indeed exhibit low H₂S removal efficiencies as shown by Xiao et al. (2008) who showed that impregnation of AC with Na₂CO₃ modifies the chemistry of the AC surface, enhancing water adsorption and promoting dissociation of H₂S and its subsequent removal.

Zeolite-based materials also possess high H₂S breakthrough capacities and therefore present an alternative strategy for H₂S removal (e.g., ion-exchanged zeolites, CuO or ZnO-modified zeolites, etc.; Cosoli et al., 2008; Micoli et al., 2014), mesoporous silica (Belmabkhout et al., 2009) and iron oxide/hydroxide systems (so-called iron sponges) (Abatzoglou and Boivin, 2009). The basicity of these materials induces acid-base or redox reactions that result in efficient removal of H₂S, for example:

$\begin{array}{ll}\text{Na-zeolite }+{\text{H}}_2\text{S }\to \text{ H-zeolite }+\text{ NaHS}& (\text{R}9)\end{array}$

$\begin{array}{ll}\text{CuO }+{\text{H}}_2\text{S }\to \text{ CuS }+{\text{H}}_2\text{O}& (\text{R}10)\end{array}$

$\begin{array}{ll}{\text{Fe}}_2{\text{O}}_3+3{\text{H}}_2\text{S }\to {\text{Fe}}_2{\text{S}}_3+3{\text{H}}_2\text{O}& (\text{R}11)\end{array}$

$\begin{array}{ll}2\text{Fe}{(\text{OH})}_3+3{\text{H}}_2\text{S }\to {\text{Fe}}_2{\text{S}}_3+6{\text{H}}_2\text{O}& (\text{R}12)\end{array}$

Iron sponge can also remove mercaptans

$\begin{array}{ll}{\text{Fe}}_2{\text{O}}_3+6\text{RSH }\to 2\text{Fe}{(\text{RS})}_3+3{\text{H}}_2\text{O}& (\text{R}13)\end{array}$

and are easily regenerated by O₂

$\begin{array}{ll}{\text{Fe}}_2{\text{S}}_3+3\text{/}2{\text{O}}_2\to {\text{Fe}}_2{\text{O}}_3+3\text{S}& (\text{R}14)\end{array}$

Besides the above physical and chemical methods, biological processes are also widely employed for H₂S removal by microorganisms. These can achieve a satisfactory degree of desulfurization without the disadvantages associated with chemical processes. They can transform H₂S into S⁰ or $S{O}_4^{2-}$ (depending on O₂ availability) generating readily separated by-products that could be used for other industrial processes. In addition, they require minimum nutrient input and display high robustness to temperature, pH and moisture fluctuations (Oyarzun et al., 2003; Syed et al., 2006; Abatzoglou and Boivin, 2009; Sun et al., 2015).

The most common biological technologies for H₂S removal include biofilters (i.e., Chung et al., 1996; Elias et al., 2002; Oyarzun et al., 2003), biotrickling filters (e.g., Kim and Deshusses, 2005; Fortuny et al., 2008; Rodriguez et al., 2014) and bioscrubbers (e.g., Sorokin et al., 2008; Van Den Bosch et al., 2008). These processes are effective and environmentally friendly for the removal of H₂S, in particular at low concentrations of the latter (Fortuny et al., 2008; Tang et al., 2009). Moreover, most biological processes for H₂S removal use sulfide-oxidizing bacteria (SOB), especially chemotropic species (mostly Thiobacillus sp., Thiotrix sp., Beggiato sp., Thermothrix sp.). A number of chemotrophic thiobacteria have been studied and found suitable for H₂S biodegradation and can be used in both aerobic conditions with O₂ and anaerobic conditions (Syed et al., 2006; Abatzoglou and Boivin, 2009). Three patented H₂S purification processes, namely Thiopaq^®, Biopuric^®, and H2SPLUS SYSTEM^®, combining chemical scrubbers and bioreactors have been commercialized for large-scale biogas desulfurization (Fortuny et al., 2008; Sorokin et al., 2008; Abatzoglou and Boivin, 2009).

Chung et al. (2007), based on their previous findings of the behavior of the Thiobmillus thiopurus biofilter (Chung et al., 1996), demonstrating for the first time a two-stage biofilter for sequential treatment of concentrated H₂S and diluted NH₃ mixtures. Their strategy of using a first biofilter of Thiobacillus thioparus for H₂S removal and a second biofilter of Nitrosomonas europaea for NH₃ removal was very effective. Kobayashi et al. (2012) studied microbial mats for desulfurization of biogas in a full-scale anaerobic digester and characterized them in terms of their structure and chemical and microbial properties. Their results indicated that the key players in sulfide oxidation and sulfur production in the bio-desulfurization in the headspace of the digester were likely to be two sulfide-oxidizing bacteria species related to H. neapolitanus and S. denitrificans: the microbial community, cell density, bacterial activity varied depending on the environmental conditions. They also showed that the habitat of the SOB should be confined to the lower part of the headspace so as to improve operating conditions. Lohwacharin and Annachhatre (2010) investigated the successful operation of the biological sulfide oxidation process in an airlift biological reactor under oxygen-limited conditions and showed that up to 90% of sulfide removed was converted to elemental sulfur ($S_2{O}_3^{2-}$ was the main by-product).

Fortuny et al. (2008) studied biotrickling filters with two different packing materials for the removal of ultra-high concentrations of H₂S from oxygen-poor gases as an interesting alternative for the treatment of off-gases containing high concentrations of H₂S. They found that optimization of packing and operating conditions could improve the process. Similarly, Fernandez et al. (2013) tested a biotrickling filter packed with polypropylene Pall rings to remove H₂S from biogas under anoxic conditions and achieved 99% sulfur removal for H₂S inlet loads lower than 120 gSm⁻³h⁻¹.

Ramos et al. (2014a,b) and Diaz et al. (2015) studied microaerobic conditions in order to control H₂S content and showed that the application of such conditions was an efficient method for H₂S control and removal from biogas. Moreover, Jeníček et al. (2017) confirmed the effectiveness of microaeration as a biochemical method of sulfide oxidation to elemental sulfur, obtaining H₂S removal efficiency more than 90% in most cases. An unusual approach is the combination of chemical and biological processes. Ho et al. (2013) proposed a chemical–biological process to remove a high concentration of H₂S in biogas, in which H₂S was first oxidized by ferric iron to generate S⁰ in a chemical reactor and the resulting ferrous iron was then oxidized in a biological reactor by iron-oxidizing bacteria. An H₂S removal efficiency of 98% was achieved indicating the feasibility of the method. Likewise, Lin et al. (2013) developed a pilot-scale chemical–biological H₂S removal process for biogas achieving H₂S removal efficiency up to 95%, further highlighting the chemical-biological approach feasibility for biogas desulfurization.

Siloxanes Removal

Organic compounds that contain Si-C bonds, called organosilicons, are classified into organosilanes and organosiloxanes. The former are polymeric compounds containing Si-Si bonds with organic side-chains, the latter consist of a backbone of alternating Si-O units with organic side-chains attached to each Si atom (de Arespacochaga et al., 2015). Siloxanes have exceptional properties including thermal stability, low flammability, low surface tension and toxicity, hydrophobicity and high compressibility. They are therefore widely used in industry as additives in many products, including pharmaceuticals, detergents, cosmetics, shampoos, shaving foams, textiles, and coatings. Depending on the raw biomass used for biogas production, and in particular from landfill wastes and composts, the resulting biogas can contain significant amount of siloxanes, volatile methyl siloxanes (VMSs) being the most common species found in digester and landfill biogas. The most significant ones are listed in Table 2.

TABLE 2

Table 2. Volatile Methyl Siloxanes commonly found in digester and landfill biogas^a.

When siloxanes-containing biogases are used as an energy vector, silica microparticulates formed at high temperatures can create fouling and abrasion effects that are highly detrimental to the engine components of natural gas-fueled vehicles (Nair et al., 2012, 2013; Jalali et al., 2013; de Arespacochaga et al., 2015), to the anodic side of biogas-fueled solid oxide fuel cells (Haga et al., 2008; Madi et al., 2015) and to the catalysts used for production of added-value chemicals from biogas. Accordingly, together with H₂S, siloxanes are considered as one of the most undesirable contaminant in biogas (Dewil et al., 2006; Ohannessian et al., 2008; Jalali et al., 2013). It is therefore of importance to remove siloxanes from biogas at the first stages of upgrading and also before its use as RNG in energy generation or catalytic production of valuable chemicals. The subject is attracting increasing attention (Abatzoglou and Boivin, 2009; de Arespacochaga et al., 2015) and undergoing rapid development.

Several methods are effective for removal of siloxanes and may be considered as possible strategies for this purpose:

i. selective absorption in organic solvents,

ii. reactive absorption by active liquids (also called extraction or chemical abatement),

iii. adsorption on silica, molecular sieves, activated carbon or polymer particles,

iv. cryogenically.

To this end, Schweigkofler and Niessner (2001) showed that nitric acid and sulfuric acid are especially potent agents for siloxane removal (efficiencies >95%) at moderately elevated temperatures (ca. 60°C) and in concentrated solutions, 65 and 97 wt% respectively, whereas phosphoric acid was ineffective. Countercurrent absorption towers are necessary to ensure sufficient contact and therefore fast mass transfer between gas and liquid, although the high acidity involved is a significant techno-economic drawback for application of the method. The same authors have also researched siloxanes abatement via adsorption on a variety of solids. The adsorption capacity was found to depend strongly on the siloxane type (L2 and D5 siloxanes were tested), relative humidity of the biogas (the higher the humidity the lower the siloxane removal capacity), and of course on the nature of the adsorbent itself (activated charcoal, carbopack B, Tenax TA, XAD II resins, molecular sieve 13X and silica gel were tested). Activated charcoal and silica gel were found to be exceptionally effective sorbents and silica gel showed excellent thermal regeneration properties as well (ca. 250°C).

Regenerable, activated alumina beds operated in continuous mode (double-bed, cyclic; alternately fused or trapping and regeneration) have been proposed for the efficient removal of siloxanes by Higgins (2007).

Montanari et al. (2010) studied D3 adsorption and adsorbent regeneration over three solids (silica gel, faujasite NaX zeolite and pure activated carbon) by means of FT-IR spectroscopy. Only partial regeneration was achieved with all these adsorbents in the temperature range of 20–200°C with either N₂ flow or by applying vacuum. Hydrogen bonding to surface silanol groups is involved in the adsorption of D3 on silica, while with NaX zeolite molecular adsorption as well as chemical adsorption occurs. The authors discussed the advantages of choosing various types of activated carbon as preferred adsorbents for removal of D3 contamination from biogas.

Cabrera-Codony et al. (2014) investigated 12 commercial types of activated carbon as D4 siloxane adsorbents. They found a strong correlation between the textural properties of the ACs (in particular the total pore volume) and their D4 adsorption capacities, with a wood-based H₃PO₄-activated carbon offering the optimum adsorption capacity (D4 ~1750 mg/g) with dry N₂ as carrier. This value was reduced by >50% under typical biogas concentrations of D4 and in the presence of the major biogas components CH₄, CO₂ and water vapor. However, polymerization of siloxane on the adsorbent surface, promoted by oxygeated functional groups (phenolic and carboxylic) that occur on these wood-based types of AC, inhibits their thermal regeneration. The authors concluded that the activated carbons with high pore volume and low carboxylic and phenolic content may be very promising materials with both high siloxane capacities and good thermal regeneration characteristics.

Sigot et al. (2014) investigated the D4 adsorbing capacity of three materials: a coconut-based activated carbon (930 m²/g BET surface area), a 13X zeolite (700 m²/g BET surface area) and a Chameleon^® silica gel (690 m²/g BET surface area). The silica gel exhibited the highest D4 adsorbing capacity: ~250 mg/g at room temperature and 0% relative humidity (RH). At a temperature ~20°C higher, only a 15% decrease in capacity was found; however RH of the order of 70% catastrophically decreased D4 adsorption at both temperatures. The surface chemistry of silica gel is dominated by siloxane Si-O-Si and silanol Si-O-H groups which show an affinity for compounds similar to D4: these are considered to play a key role in the superior capacity of silica gel compared to the other materials tested.

Jiang et al. (2016) explored D4 siloxane adsorption over mesoporous aluminosilicate (UCT-15), a zeolite-type material developed at the University of Connecticut, which offers tuneable textural properties via variations in aluminum content and calcination ramp rate. The best D4 adsorption capacity (105 mg/g) was shown by UCT-15 with Si:Al = 5 and a 10°C/min ramp rate, a value that is almost twice that of commercial ZSM-5, which has similar BET surface area and total pore volume. The as-prepared UCT-15 had a larger BET surface area, external surface area, mesopore volume and total pore volume. External surface area and mesopore volume were the key parameters governing the adsorption capacity. Hydroxyl groups on the surface of the aluminosilicates were found to promote the undesirable polymerization of D4, which is detrimental to adsorbent regeneration. In a more recent report Jafari et al. (2016) modified the textural properties of the mesoporous silica UCT-14, by tuning the temperature of gelation, calcination temperature and the heating rate to produce a material with high D4 adsorbing capacity (686 mg/g). This high value is comparable to that achieved with commercial silica gel under both dry and humid conditions. The modified UCT-14 (designated Si-Syn120) was more stable under consecutive use-regeneration cycles and somewhat more resistant to humidity in regard to performance deterioration, compared to commercial silica gel.

Cryogenic methods may also be considered for biogas purification from siloxanes. Although siloxanes can be fully removed (>99%) at very low temperatures, ca. −70°C, Abatzoglou and Boivin (2009) pointed out the energy-intensive character of the method and the need for relevant techno-economic analysis to demonstrate its sustainability.

Comprehensive reviews of biogas purification processes have been provided by Abatzoglou and Boivin (2009) and Ryckebosch et al. (2011).

Biogas Upgrading

This term is typically used to describe processes that remove all impurities from biogas (i.e., desulfurization, siloxanes removal, drying, elimination of trace compounds) in addition to CO₂ removal in order to achieve upgrading to natural gas with a high Wobbe Index (MJ/m³) as fuel for transport applications or grid injection, minimizing adverse effects associated with acid emissions (Abatzoglou and Boivin, 2009; Salihu and Alam, 2015). Upgrading strategies are mostly based on physical and/or chemical absorption in water or in active aqueous solutions (Cebula, 2009; Petersson and Wellinger, 2009; Kismurtono, 2011; Ryckebosch et al., 2011; Bansal et al., 2013; Khalil et al., 2014; Kohl and Nielsen, 1997) or adsorption on solid surfaces (Pandey and Fabian, 1989; Dabrowski, 2001; Jee et al., 2001; Yang, 2003; Himeno et al., 2005; Grande and Rodrigues, 2007; Ma et al., 2007; Cavenati et al., 2008; Das et al., 2008; Alonso-Vicario et al., 2010; Tippayawong and Thanompongchart, 2010; Grande, 2011, 2012; Yuan et al., 2013; Andriani et al., 2014), membrane separation methods (Wellinger and Lindberg, 2005; Favre et al., 2009; Petersson and Wellinger, 2009; Simons et al., 2009; Deng and Hagg, 2010; Makaruk et al., 2010; Ryckebosch et al., 2011; Andriani et al., 2014; Salihu and Alam, 2015), and biological methods (Ryckebosch et al., 2011; Andriani et al., 2014; Salihu and Alam, 2015) or even combinations of the above (Bansal et al., 2013).

On the other hand, the CO₂ content of biogas may not be considered as an undesirable component; it is a raw material, which potentially could be used for enhanced oil recovery, and for augmenting the growth and production of algae and plants (as a carbon source for autotrophic microorganisms), and for the production of added-value chemicals, e.g., via hydrogenation—see below. Therefore, its regeneration during biogas upgrading is of substantial importance.

Absorption Processes

CO₂ separation from a gas stream via absorption is a classical method, based either on physical or preferably on chemically-driven absorption of CO₂ in liquids or liquid solutions, taking place in bubble cap trays or in randomly packed towers (containing inert solid elements) where a countercurrent flow of gas mixture and liquid absorbent is applied; spray contactors of absorbent and gas mixture may also be possible in practical applications (Kohl and Nielsen, 1997). Countercurrent flow in randomly packed columns is well suited to absorption applications due to their more reliable design and generally superior performance. Based on the significantly higher solubility of CO₂ in water compared to methane, particularly at lower temperatures (Figure 1), so-called water or physical scrubbing may be used for CH₄-CO₂ separation of biogas. The CO₂-rich water leaving the absorption tower is regenerated by flashing followed by recycling. Biogas upgrading plants using water scrubbing with yield capacities of the order of 30–100 m³/h are in current use.

FIGURE 1

Figure 1. Solubility of CO₂ and CH₄ in water. Data Source: Perry et al. (1984).

On the other hand, with the most effective chemically-based absorption of CO₂ (often called chemical scrubbing), efficiencies up to 99.5% can be reached (Ryckebosch et al., 2011), with alkalis (e.g., NaOH; Ca(OH)₂) or alkanolamines (RNH₂; R is the organic component of the amine whose identity is not critical to the absorption reaction). Aqueous solutions of these bases are generally used, where CO₂ trapping occurs according to the following reactions:

$\begin{array}{l}{\text{CO}}_2+2{\text{OH}}^{-}\to {\text{CO}}_3^{2-}+{\text{H}}_2\text{O}\stackrel{C{O}_2}{\to }2{\text{HCO}}_3^{-}\\ (\text{in alkaline solutions})& (\text{R}15)\end{array}$

$\begin{array}{l}{\text{CO}}_2+{\text{RNH}}_2+{\text{H}}_2\text{O }\to {\text{RNH}}_3^{+}+{\text{HCO}}_3^{-}\\ (\text{in alkanolamine solutions})& (\text{R}16)\end{array}$

The most common alkalolamines used include monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA), di-methylethanolamine (DMEA), methyldiethanolamine (MDEA), mixtures of glycol and monomethylamine, diglycolamine (DGA), diisopropanolamine (DIPA) and amine mixtures (Cebula, 2009; Petersson and Wellinger, 2009; Ryckebosch et al., 2011). After absorption, the consumed alkalolamine is regenerated by heating, and then recycled. During this process the following reaction takes place:

$\begin{array}{ll}{\text{RNH}}_3^{+}+{\text{HCO}}_3^{-}\to {\text{RNH}}_2+{\text{H}}_2\text{O }+{\text{CO}}_2& (\text{R}17)\end{array}$

It is possible for chemical scrubbing to be applied for the simultaneous removal of CO₂ and H₂S, in which case higher temperature is required for amine regeneration (Petersson and Wellinger, 2009). It is therefore preferable to remove H₂S from biogas before CO₂ absorption as this is cheaper overall and generates clean CO₂ for possible subsequent use.

Adsorption Processes

Adsorption, often referred to as chemisorption, the driving force behind heterogeneous catalytic reactions, is also widely applied for the selective separation of molecules from a fluid phase (Dabrowski, 2001). It is the spontaneous exothermic chemical reaction that occurs when a molecule (referred to as adsorbate), initially present in fluid phase, encounters the surface of an active solid (referred to as adsorbent). Adsorbents are porous solids with large surface areas per unit mass (typically 100–2,000 m²/g), such as activated carbons, molecular carbon sieves, fullerenes, carbonaceous nanomaterials, silica gels, activated alumina and other metal oxides, metal hydroxides, zeolites, clay minerals and pillared clays, etc. They are effective for the selective adsorption of specific species from a fluid (gas or liquid) phase, thus removing them from the mixture. The adsorption isotherms of adsorbate species, often described by the Langmuir equilibrium equation, are of critical importance for the design of an adsorption-based separation process and enable determination of the solid surface capacity of the adsorbent for a specific adsorbed molecule. On the other hand, the kinetics and dynamics of adsorption, described by the more general term “adsorption dynamics,” is affected by external, internal and surface diffusion characteristics of the adsorbed molecule, and, as described by Fick's second law, give the evolution with time of industrial adsorption processes used in separations (Kohl and Nielsen, 1997; Dabrowski, 2001).

Regeneration of the adsorbent, a key step in any separation process based on adsorption, can be performed by reducing the total pressure or by applying vacuum conditions on the saturated adsorbent: these processes are therefore termed pressure swing adsorption (PSA) or vacuum swing adsorption (VSA) respectively. Alternatively, regeneration may be achieved by increasing the temperature of the saturated adsorbent so as to desorb the adsorbate (temperature swing adsorption, (TSA)).

Adsoprtion-based removal of CO₂ from biogas is widely practiced and commercially applied at both pilot and demonstration plant levels and is still an active research subject (Cavenati et al., 2008; Cebula, 2009; Petersson and Wellinger, 2009; Alonso-Vicario et al., 2010; Tippayawong and Thanompongchart, 2010; Grande, 2011; Montanari et al., 2010; Grande, 2012; Ryckebosch et al., 2011; Yuan et al., 2013; Andriani et al., 2014). The techniques used include PSA and TSA, both involving two packed-bed columns in a swing-type arrangement employing appropriate valve sequencing, as shown schematically in Figure 2. The operating principal is similar in the two cases, the main difference being the method used for adsorbent regeneration, i.e., either pressure or temperature variation. This two-column arrangement allows continuous-flow steady-state operation of the process, although the operation of individual columns is of course discontinuous and involves a multistep cycle. The simplest case uses a two-step cycle. One column is maintained at low temperature to continuously trap CO₂ from the biogas flow (allowing free passage of CH₄ through the packed bed) whilst the other is heated (TSA) or evacuated (PSA) to release previously adsorbed CO₂. Note that the temperature of the bed determines its adsorption capacity—the lower the temperature, the greater the adsorption capacity of an adsorbent for a given molecule. A CO₂ collection vessel is typically used, as well as a small portion of the purified methane stream (or an inert gas) in order to assist CO₂ flow into the collection vessel and to purge the column, preparing it for the next cycle. In the second step, the two 4-port valves are synchronous turned to a second position such that the role of each column is reversed: the cleaned column #2 now traps CO₂, whilst the previously CO₂-saturated column #1 commences regeneration. The duration of the two-step cycle is a crucial design parameter that depends on the CO₂ capacity of the columns. This must be appropriately determined in order to allow continuous utilization of the feedstream with continuous production of CH₄ in the system's exhaust. The basic concept can be varied, especially in regard to the number of steps required for a complete cycle, and with respect to the operating sequence of the valves during each step (Grande, 2012). In addition to CH₄-CO₂ separation, the concept has been successfully applied in a number of other separations, for example in the purification of H₂-containing streams for fuel cell applications (Nikolaidou et al., 2015); for C₂H₄ separation from CH₄ and O₂ in the oxidative coupling of methane, thus providing a one-step transformation of methane to ethylene with extremely high yields (Jiang et al., 1994); for air separation (Jee et al., 2001); for noble gas purification (Das et al., 2008); for n-paraffin/iso-paraffin separation (Yang, 2003), and others. The simplicity of PSA and its low capital and operational costs makes it very attractive in comparison to other fluid separation technologies.

FIGURE 2

Figure 2. Schematic representation of a two-columns temperature (or pressure) swing adsorption unit. Under the indicated stage of operation, column#1 is unsaturated and operates for CO₂ trapping, whilst the saturated column#2 is regenerating (CO₂ desorption).

Adsorbent characteristics are crucially important in adsorption-based biogas upgrading units. Their CO₂ capacity and the temperatures required for sufficient CO₂ adsorption and desorption are critical parameters that determine the economics and engineering aspects of the separation process. A wide variety of porous materials, including many kinds of zeolites, mesoporous materials, activated carbons and more recently high-surface area coordination polymers can be effectively applied in PSA and TSA. Yet other materials for this purpose are continuously under development, although only a few are used in current commercial PSA units. New research avenues are aimed at the simultaneous removal of CO₂ and H₂S from biogas (Belmabkhout et al., 2009; Tippayawong and Thanompongchart, 2010). A significant cost-effectiveness parameter for potential adsorbents is their ease of regeneration, rather than their ultimate CO₂-capacity. Accordingly, materials that exhibit quasi-linear CO₂ adsorption isotherms at low pressures, as opposed to very steep ones that rapidly flatten above a certain pressure, are far preferable in PSA applications, even if the latter offer much higher ultimate capacities (Grande, 2012). Materials which meet the requirements for effective, low-cost CH₄-CO₂ separation are zeolites, carbon molecular sieves and activated carbons (Pandey and Fabian, 1989; Cebula, 2009; Montanari et al., 2010; Ryckebosch et al., 2011; Alonso-Vicario et al., 2010).

Compact PSA plants for CH₄-CO₂ separation with yields of the order of 250 m³/h have been already commercialized. They involve low capital and installation costs and are well suited to small scale applications. A comprehensive overview of the fundamentals of the PSA process and its evolution with time, with emphasis on CH₄-CO₂ separation, has recently been published by Grande (2012).

Membrane Separation Processes

The selective permeation of a molecule through a solid renders it as a potential membrane for the separation of that molecule from a gas mixture (Bernardo et al., 2009). Gas-gas and gas-liquid membrane separation processes have been developed for practical applications (for example, in the latter case CO₂ is extracted from a CO₂+CH₄ gas mixture into a liquid phase from which it is subsequently extracted by a second gas-liquid membrane thus achieving separation of the two components, Figure 3; Simons et al., 2009).

FIGURE 3

Figure 3. Separation of CH₄ and CO₂ in a combined double gas-liquid membrane process. [Reproduced with permission of Elsevier from Simons et al. (2009)].

For biogas upgrading, membranes typically consist of materials that are permeable to CO₂, water and NH₃, partially permeable to H₂S and O₂ and essentially non-permeable to CH₄ and N₂ (Favre et al., 2009; Petersson and Wellinger, 2009; Deng and Hagg, 2010; Makaruk et al., 2010; Ryckebosch et al., 2011; Andriani et al., 2014). However, water and H₂S are usually removed from biogas before CO₂ separation as they can adversely affect membrane performance and efficiency. Due to the less than ideal efficiency of practical membranes, multi-stage separators are commonly used for efficient CH₄-CO₂ separation (Wellinger and Lindberg, 2005; Makaruk et al., 2010) and such biogas upgrading units with yield capacities >200 m³/h are in current use.

New Technologies

Recent developments in biogas upgrading technology include cryogenic separation, in situ biological methane enrichment and the so-called ecological lung (Petersson and Wellinger, 2009; Ryckebosch et al., 2011; Kao et al., 2012). These methods, although promising and providing better performance than traditional well-established technologies already operating in micro-, meso-, and macro-scale biomethane production plants, are still under development. Both traditional and more recent biogas upgrading methods are being continuously improved and developed, so that the subject is a very active area of applied technology research. It is worth noting that all biogas upgrading technologies are capable of producing RNG for vehicle applications containing >97% CH₄, which purity is superior to that of all globally produced natural gases. Ryckebosch et al. (2011) and Andriani et al. (2014) have reviewed biogas upgrading techniques currently in use or under development, providing comprehensive comparative technical and operational details, advantages/disadvantages, energy and technical requirements, maintenance and operational costs and other techno-economic information. More recently, Sun et al. (2015) published a comprehensive review covering biogas-upgrading technologies. As these authors point out, upgrading technology is site-specific, case-sensitive, and dependent on utilization requirements and local circumstances. They have critically evaluated state-of-the-art purification and upgrading processes, providing much useful information in regard to product purity, methane recovery and loss, process efficiency, as well as the investment and operating costs of the various alternatives.

Advanced Biogas Utilization

This topic is the principal focus of the present review. Most biogas sources linked to anthropogenic activities (urban wastewater sludge, agricultural food industry sludge and animal farm manure anaerobic fermentation, landfill and commercial composting) yield gas that currently is used in specialized burners for heat production—a route for energy recovery that is not the most desirable one. Indeed, heat is a low quality form of energy that can be transformed to other high quality forms only with a very low efficiency. Even worse, low-grade biogas (i.e., minimal CH₄ content) is inappropriate for direct heat production because at low methane levels the operation of biogas burners is inefficient. In such cases, large quantities of poor-quality biogases are instead wasted by highly detrimental venting to atmosphere, seriously contributing to environmental pollution. Biogas is widely available as a product of the decomposition of all living matter, it is therefore cheap and is a potential renewable carbon source for energy and chemicals production. Moreover, its usage addresses the imperative need for attaining sustainable development and eco-friendly production of energy and added-value chemicals. The increasing value of petroleum, combined with extensive use of fossil fuels and the associated greenhouse emissions have prompted researchers to focus on generating energy from low-carbon sources by means of eco-friendly modern technology. Biogas is a viable alternative to fossil fuels and its valorization is now a field of intense activity: research and development, technology and implementation are currently given high priority.

In this section, the major R&D avenues for biogas valorization will be presented and discussed, regardless of their status of development, i.e., application, commercialization, pilot, demonstration or laboratory research. The presentation is based on the flow sheet shown in Figure 4, which depicts possible advanced routes for obtaining energy or added-value chemicals based on rational management and utilization of biogas.

FIGURE 4

Figure 4. Schematic representation of the possible routes for biogas utilization as a renewable carbon vector (i.e., power generation and/or added-value chemicals production).

The first step in Figure 4 concerns purification, i.e., removal of H₂S, siloxanes, water vapor and other possible case-sensitive traces, in order to produce a pure CH₄-CO₂ mixture. Two alternative avenues may then be considered: avenue#1, involves biogas external (route#1-1) or internal (route#1-2) reforming and also other more traditional methods (route#1-3: combined heat and power engines, CHP, or route#1-4: heat production burners); the latter lie outside the scope of this review. Avenue#2 concerns upgrading of the purified biogas, i.e., separation of CH₄ and CO₂.

Methane (external) reforming (route#1-1, Figure 4) is a well-established technology for synthesis gas (H₂+CO) or H₂ production (e.g., Ashcroft et al., 1991; Bradford and Vannice, 1999; Verykios, 2003; Papadopoulou et al., 2012; Yentekakis et al., 2015). Practically, any composition (poor, equimolar, or rich in CH₄) of the purified biogas itself is a suitable feed for the dry reforming of methane (DRM) process, which occurs through the reaction (R18):

$\begin{array}{ll}{\text{CH}}_4+{\text{CO}}_2\to 2\text{CO }+2{\text{H}}_2& (\text{R}18)\end{array}$

producing H₂ and CO, so-called syngas, since it can be fed to Fischer-Tropsch synthesis technology (path#1-1-1, Figure 4) to produce liquid energy carriers (e.g., Schulz, 1999; Selvatico et al., 2016). This probably represents one of the most attractive routes for biogas valorization as a renewable carbon source.

Dry reforming of methane has been investigated over a variety of metal catalysts (e.g., Ni, Pt, Rh, Ir, Ru, Pd, Co) supported on oxide or mixed oxide supports (e.g. Al₂O₃, La₂O₃, CeO₂, SiO₂, TiO₂, La₂O₃-SiO₂, ZrO₂-SiO₂, PrO₂–Al₂O₃). Most of these catalysts are very active for the DRM reaction. A major problem that concerns especially nickel-based catalysts (the cheapest) is coke deposition, which eventually results in catalyst deactivation; some very recent studies are focused on Ni-based bimetallic catalysts which exhibit reduced carbon deposition (Niakolas et al., 2015). This drawback does not affect noble metal catalysts which show similar activity but are very resistant to carbon deposition, and hence attractive candidates for use in practical applications of DRM. Recently, it was shown that Ir is an extremely stable catalyst at high temperatures under oxidative conditions; it therefore fulfil1s all the necessary requirements for practical DRM applications (Yentekakis et al., 2015).

It is beyond the scope of the present review to consider DRM in any detail. It has been well studied for many years and several comprehensive reviews are available (e.g., Rostrup-Nielsen and Hansen, 1993; Bradford and Vannice, 1999; Verykios, 2003).

As an alternative to the Fischer-Tropsch synthesis route, syngas (CO+H₂) can be utilized as an efficient fuel in high temperature solid oxide fuel cells for electrical power generation (path#1-1-2, Figure 4), although the aforementioned internal reforming process offers some engineering and economic advantages as schematically shown in Figure 5.

FIGURE 5

Figure 5. Schematic of the differences between external (A) and internal (B) reforming concepts for SOFC-added electrical power generation from biogas.

A further alternative is the use of syngas for H₂ production via the water-gas-shift reaction (R19) which converts CO to CO₂ and simultaneously enriches the H₂ content of the effluent gas (path#1-1-3):

$\begin{array}{ll}\text{CO }+{\text{H}}_2\text{O }\leftrightarrow {\text{CO}}_2+{\text{H}}_2& (\text{R}19)\end{array}$

After CO₂ removal, the product (pure H₂ with very low levels of CO) can either be used for electrical power generation in polymeric membrane low temperature (~80°C) fuel cells (PEM-FCs) or can be stored for fueling zero emission vehicles. It is well known, however, that low temperature PEM-FCs are very sensitive to CO impurities in the H₂ fuel. The technology for rigorous CO removal (<20 ppm) has been developed, is commercially available, and has been applied in micro- and meso-scale units (Helbio). It is also worth noting that high performance polymer electrolytes for PEM fuel cells have been discovered by Neophytides, Kallitsis and coworkers (Geormezi et al., 2011, 2012). These operate at 150–200°C and are insensitive to CO impurities (up to ~1%). This avenue for biogas utilization has been successfully applied (Nikolaidou et al., 2015) in a demonstration (pilot) scale process in which, starting from wine-waste sludge, an ~500 W electrical power pilot unit with a stack of 17 elevated temperature (180°C) PEM unit cells was successfully constructed and tested.

As shown in Figure 4, an alternative route for biogas utilization is its use in intermediate- or high-temperature fuel cells that use internal reforming for renewable energy production (route#1-2, Figure 4). This concept, also called direct-biogas solid oxide fuel cell (DB-SOFC), offers several advantages in comparison to the previously discussed method of external reforming (Figure 5), has currently received much attention in both experimental (Goula et al., 2006; Yentekakis, 2006; Shiratori et al., 2008, 2010; Yentekakis et al., 2008; Lanzini and Leone, 2010; Papadam et al., 2012; Takahashi et al., 2012; Lanzini et al., 2013; Ma et al., 2015; and references therein) and modeling studies (Lanzini et al., 2011; Ni, 2013; Janardhanan, 2015a,b). Most of these studies made use of Ni-based cermet anodes, doped with additives in some cases in order to prevent carbon deposition (e.g., Yentekakis, 2006; Ma et al., 2015; Niakolas et al., 2015). Table 3 summarizes some direct biogas fuel cells studies that are worthy of particular note.

TABLE 3

Table 3. Direct biogas fuel cell studies.

The main findings of these works were as follows:

i. Internal dry reforming of CH₄ in solid oxide fuel cells is possible even with traditional inexpensive Ni-based cermet anode, without deterioration of cell performance during operation (Goula et al., 2006; Papadam et al., 2012), independently of the biogas quality (low to high CH₄ biogas content). This is because the current flux through the cell prevents carbon accumulation on the anode via the reactions:

$\begin{array}{ll}\text{C }+{\text{O}}^{2-}\to \text{ CO }+2{\text{e}}^{-}& (\text{R}20)\end{array}$

$\begin{array}{ll}\text{C }+2{\text{O}}^{2-}\to {\text{CO}}_2+4{\text{e}}^{-}& (\text{R}21)\end{array}$

These charge transfer reactions occur in parallel with the principal electro-productive reactions between O²⁻ and the reformates (H₂, CO), also taking place on the anode, i.e.,

$\begin{array}{ll}{\text{H}}_2+{\text{O}}^{2-}\to {\text{H}}_2\text{O }+2{\text{e}}^{-}& (\text{R}22)\end{array}$

$\begin{array}{ll}\text{CO }+{\text{O}}^{2-}\to {\text{CO}}_2+2{\text{e}}^{-}& (\text{R}23)\end{array}$

further contributing to the cell's electrical power generation (Goula et al., 2006; Papadam et al., 2012). Recall that the reactions responsible for carbon deposition on the anodes of direct hydrocarbon fuel cells are the methane pyrolysis reaction (R24) and Boudouard reaction (R25)

$\begin{array}{ll}{\text{CH}}_4\to \text{ C }+2{\text{H}}_2& (\text{R}24)\end{array}$

$\begin{array}{ll}2\text{CO }\to \text{ C }+{\text{CO}}_2& (\text{R}25)\end{array}$

which together with the reforming reaction (R18) and the water gas shift (WGS) reaction (R19)

$\begin{array}{ll}\text{CO }+{\text{H}}_2\text{O }\leftrightarrow {\text{CO}}_2+{\text{H}}_2& (\text{R}19)\end{array}$

are the principal chemical and electrochemical reactions taking place in an internal methane reforming fuel cell (Wang et al., 2013; Gur, 2016).

ii. Although the best cell output characteristics (power density) are obtained at around equimolar biogas composition (CH₄/CO₂ ~1), it is also the case that even poor (low CH₄ content) biogas is suitable feed for stable and productive fuel cell operation (Yentekakis et al., 2008; Guerra et al., 2013, 2014).

iii. Both intermediate (600–800°C) and high temperature (800–1,000°C) fuel cells operate successfully under direct biogas feed (Yentekakis, 2006; Yentekakis et al., 2008; Papadam et al., 2012). In regard to this, fast O²⁻-ionic conduction in the solid electrolyte at the required cell operating temperature is the key factor—rather than the kinetics of the anodic chemical and electrochemical reactions; the latter appear to be fast at temperatures > ~600°C.

iv. Electrical power output characteristics of direct biogas FCs were found to compare favorably with those obtained with the same cell under H₂ feed (Fuerte et al., 2014; Ma et al., 2015). This probably implies that reaction (R22) dominates cell performance. Promotion of reaction (R23) is expected to enhance cell performance, as shown by theoretical studies (Ni, 2013). This can be achieved by developing selective electrocatalysts for reaction (R23).

v. Early studies mainly focused on the feasibility of the process with respect to the anodic electrocatalysts employed, which showed the appropriateness of Ni-based composites as active and durable anodic materials. Recent trends also involve optimization of fuel cell compartments and characteristics, aimed at minimizing ohmic overpotential of the cell (found to be the main source of cell polarization) so as to increase power output and efficiency. With this aim, anode- or cathode-supported fuel cell designs with very thin solid electrolytes (ca. 3–20 μm) were successfully applied, delivering as expected superior power generation (Wang et al., 2011a; Takahashi et al., 2012; Ma et al., 2015). Further development of anodic materials together with advanced fuel cell designs that minimize cell overpotentials (of which there is much expertise in solid oxide fuel cell technology) in combination with optimal operational conditions (information provided by direct biogas fuel cell modeling studies) are expected to lead to the development of highly efficient and cost-effective direct biogas fuel cells in the near future.

The second basic avenue#2 of Figure 4 is now considered. It concerns biogas upgrading after purification. Upgrading leads into two separated products: pure CH₄ and pure CO₂. The former can be directly supplied to the national natural gas grid for transport use, as RNG or as a substitute natural gas (SNG), so-called biomethane (route#2-1). An alternative and more attractive route to biomethane valorization (route #2-2) would be its utilization for ethylene (C₂H₄) production, as proposed by Vayenas, Yentekakis and Jiang (VYJ process) (Jiang et al., 1994; Vayenas et al., 1995; Yentekakis et al., 1995, 1996; Makri et al., 1996) by means of the one-step oxidative coupling of methane (OCM) reaction (Keller and Bhasin, 1982; Ito and Lunsford, 1985; Lunsford, 1990):

$\begin{array}{ll}{\text{CH}}_4\stackrel{+{\text{O}}_2}{\to }{\text{C}}_2{\text{H}}_2+C_2{H}_4+{\text{C}}_2{\text{H}}_6+{\text{H}}_2\text{O}& (\text{R}26)\end{array}$

The VYJ process is an one-step method for oxidatively coupling methane to ethylene with yields up to 85% and total C₂ hydrocarbons (C₂H₄ and C₂H₆) up to 88% (Jiang et al., 1994). Such performance is achievable in a gas recycle electrocatalytic or catalytic reactor-separator where the recycled gas continuously passes through a molecular sieve trap in the recycle loop. The outputs of this process are ethylene selectivity up to 88% at methane conversion up to 97%, with a C₂H₄ yield of the order of 85% (Jiang et al., 1994). These values are economically very attractive for development on an industrial scale of this one-step method for production of ethylene from biogas. Ethylene is one of the most important raw materials of the petrochemical industry, used for the production of a wide range of added-value chemicals and plastics (Austin, 1984). For a country with well-established petrochemical industry, such utilization of biogas would represent the most attractive way of its valorization (Chemistry and industry, 1994) and should be considered a high priority.

In regard to the CO₂ product from the upgrading unit (see Figure 4), the following pathways may be proposed. A CO₂-reduction (hydrogenation) process (route#2-3; paths #2-3-1 and #2-3-2), transforming CO₂ to CH₄ through the so-called Sabatier reaction (R27) or to methanol (R28),

$\begin{array}{ll}{\text{CO}}_2+4{\text{H}}_2\to {\text{CH}}_4+2{\text{H}}_2\text{O }\Delta \text{H}°=-165\text{kJ/mol}& (\text{R}27)\end{array}$

$\begin{array}{ll}{\text{CO}}_2+3{\text{H}}_2\to {\text{CH}}_3\text{OH }+{\text{H}}_2\text{O }\Delta \text{H}°=-53.3\text{kJ/mol}& (\text{R}28)\end{array}$

including the formation of other carbonaceous products, such as CO, higher hydrocarbons, dimethyl ether, higher alcohols or formic species (Wang et al., 2011b; Jadhav et al., 2014; Saeidi et al., 2014; Puga, 2016). Ru is an active catalysts for CO₂ methanation, followed by Ni, Fe and Co (Wang et al., 2011b; Puga, 2016), while for formation of methanol and formaldehyde, Cu, Cu-Zn and Ni-Co based supported catalysts are effective (Wang et al., 2011b; Jadhav et al., 2014). There are however both chemical and engineering problems to be solved in regard to these reactions. Both (R27) and (R28) are exothermic and involve a reduction in volume and are therefore thermodynamically favored at low temperatures and elevated pressures. But low temperatures decrease reaction rates, whereas typical catalytic systems are active at moderate temperatures ca. 200–400°C (Wang et al., 2011b; Saeidi et al., 2014; Puga, 2016). The goal therefore is to develop catalysts that are sufficiently active and selective at low temperatures and, if possible, at atmospheric pressure. This is currently a priority research area where surface- or support-induced promotion of the active phases nano-structured catalyst architectures can play a key role. For example, TiO₂-supported Ru nanoparticles are a very promising catalysts for CO₂ methanation (Abe et al., 2009).

CO₂ reduction may also be achieved photochemically and/or electrochemically either with H₂ or with H₂O (Roy et al., 2010; Hoffmann et al., 2011; Habisreutinger et al., 2013; Ganesh, 2014; Jadhav et al., 2014; Puga, 2016). The photochemical reduction is also called “energy-to-power” (P2G) technology or even “artificial photosynthesis” in which H₂ produced via a solar-driven water splitting system by means of electrolysis can drive CO₂ hydrogenation to yield biomethane or liquid biofuels.

Nowadays, conversion of CO₂ into value added chemicals, especially using photocatalysis, is an important world-wide research priority. Progress, challenges and perspectives have been documented in a number of comprehensive reviews, such as those by Wang et al. (2011b), Ganesh (2014), Roy et al. (2010), Saeidi et al. (2014), Hoffmann et al. (2011).

Returning to Figure 4, following the path#2-3-1, biomethane may be fed into the natural gas grid (path#2-3-1-1) or further upgraded to be transformed to ethylene (path#2-3-1-2) by means of Vayenas-Yentekakis-Jiang (VYJ) process (Vayenas et al., 1995), similar to route#2-2. In other words, should it be desired, it is possible to transform all the carbon content of biogas to ethylene by means of combining path#2-3-1-2 and route#2-2 (Figure 4). This scenario would transform wastewater treatment plants and other biogas-producing sites into small-scale ethylene production units.

A synopsis of the above analysis of biogas management as a renewable carbon source in terms of the final product is given below in Table 4. Note that the possible advanced alternative uses that could be applied in practice are subject to the amount of available biogas and to local, regional or global (national) eco- or economic targets.

TABLE 4

Table 4. Synopsis of specific process sequences leading to specific desired products from a biogas feedstock.

The significance in respect to the above discussion is that all the necessary technology for complete valorization of biogas (both CH₄ and CO₂ content) is currently available and/or rapidly developing. This accounts for the major R&D and technology interest in biogas valorization, since it represents a unique, widely available and cheap renewable carbon source, providing the opportunity for eco-friendly and economic energy generation and production of value added chemicals.

Conclusions

Biogas, produced from the decomposition (anaerobic digestion) of all living matter, consists mainly of CH₄ and CO₂. Major efforts in research & development technology are currently devoted to biogas valorization as it represents a suitable, widely available and cheap renewable carbon source, providing the opportunity for eco-friendly and economic energy generation and production of value added chemicals.

This review has focused on the exploitation of the main constituents of biogas (CH₄ and CO₂) as potential raw materials for advanced management and exploitation of this resource, including the principal technologies available and pathways for power generation and value added chemical production.

Analysis has been provided of biogas utilization for renewable and eco-friendly electrical power generation by means of (i) low and higher temperature polymeric membrane fuel cells and (ii) intermediate and high temperature solid oxide fuel cells. In addition, processes for the conversion of biogas to (i) RNG, (ii) clean hydrogen, (iii) ethylene, and (iv) biomethanol or other Fischer-Tropsch liquid biofuels production have been examined.

A final word is in order in regard to economic evaluation of the various existing and emerging strategies for biogas exploitation, which is of course a key issue. This important subject which merits detailed discussion lies beyond the scope of our technically-oriented review, not least because most current approaches to biogas utilization are still at the research and development stage. Accordingly, there is a pressing need for comprehensive economic evaluation of alternative routes for the efficient use of biogas in the energy and chemicals sectors, including identification of bottlenecks, in order to guide policy making and future research and development in this field.

Author Contributions

IY designed the review study and wrote the manuscript. GG assisted with literature searching and in discussion of the fuel cell literature data.

Conflict of Interest Statement

The authors declare that the research was conducted in the absence of any commercial or financial relationships that could be construed as a potential conflict of interest.

Acknowledgments

The authors thank the Technical University of Crete-Research Committee, Special Research Funds Account, TUC, Chania, Crete, Greece, for partial financial support under the project PostDoc2016.

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