Biogas Upgrading into Renewable Natural Gas: Part I—An Assessment of Available Technologies

Abstract

Energy security is a growing societal and industrial concern that leads research and development toward more sustainable options. Biogas, a bio-alternative to conventional fuels, is a product generated from the anaerobic digestion of organic matter. This source of fuel production is more environmentally friendly compared to traditional fossil fuels, leading to a lower carbon footprint, higher air quality, and the promotion of a circular economy. Impurities of raw biogas, such as carbon dioxide, hydrogen sulfide, and other trace contaminants, make biogas conditioning necessary for most applications. In addition, biogas upgrading, technologies furthering biogas purity, is an important factor in the production of biomethane, a sustainable biofuel known more commonly as renewable natural gas (RNG). Diversifying fuel sources and providing energy sustainability while mitigating negative environmental effects makes RNG an attractive alternative to conventional natural gas. This document, Part I, provides an overview of current technologies related to biogas conditioning, such as sorption, oxidation, and biological treatments aimed at the removal of a wide variety of contaminants. Processes developed for biogas upgrading are also discussed, including physical/chemical absorption, pressure swing adsorption, and membrane separation. The focus of upgrading applies approaches in meeting a higher quality biofuel by further carbon dioxide exclusion to ease pipeline transport and increase combustion efficiency. These technologies present the core foundation of processes in the production of RNG; however, all face inherent challenges that deem further research and development a requirement for global adoption. The biggest challenges are either in the cost of reaching higher purities or the inability to do so without other operations. Thus, in conjunction with this document, emerging and developing technologies are provided in a separate analysis deemed Part II. Together, these documents offer a comprehensive understanding of current practices and growing technological developments.

1. Introduction

Biogas is an attractive renewable energy resource derived from biological raw feedstocks for a carbon-emission-restricted future. It can reduce the world demand for fossil fuel-based natural gas and mitigate the accumulation of greenhouse gases in the atmosphere. Projections to 2050 established in the 2022 Annual Energy Outlook by the Energy Information Administration (EIA) of the USA natural gas production will grow steadily at about a 0.9% rate through the coming years [1]. Natural gas exports and industrial applications drive the current production of natural gas [2]. Additionally, carbon dioxide (CO₂) emissions related to the energy used by the industrial sector are forecast to grow, showing a 0.6% per year increase from 2017 to 2050 in the USA. The EIA also states that natural gas generates most of the energy and CO₂ emissions in the industrial sector during the entire projection period [1]. In fact, the EIA predicts that natural gas-fueled power plants will be, by far, the largest source of electricity within the USA for many years to come, with the use of coal steadily decreasing over time. Currently, electrical power generation is the largest sector contributing to natural gas consumption due to its use as a feedstock in various chemical processes. Due to the demand and considerable benefits, renewable natural gas (RNG) as an additional source or an alternative to natural gas is growing in appeal in global energy markets. An advantage of RNG is its cleaner production, and with costs expected to continue decreasing with further development, RNG can be a promising and more attractive option for industrial processes. Research into biogas production, conditioning, and use will also continue to increase over the coming years. Figure 1 shows an analysis of publications and topics collated from the Web of Science database on “Renewable Natural Gas” from 2014 to 2023. Total yearly publications in RNG research increased from roughly 546 to over 2100 from 2014 to 2023. This trend in publication production shows higher interest in the topic and can be directly correlated to increased energy sustainability efforts and technological advancements. Analysis of citation topics provides the highest discussion of RNG production in the fields of sustainable sciences, energy and fuels, power systems, and electric vehicles. The diversity of applications within the vast research areas of RNG incites further investment into growing generative technologies on a global scale.

Biogas is a gaseous product generated from the complete anaerobic digestion of organic materials. Most biogas produced for use as fuel is generated within artificially constructed anaerobic digesters or landfills. These can be designed using various reactor systems with the resulting product labeled biogas. The majority of biogas produced by volume is primarily composed of methane (CH₄) and carbon dioxide in the range of 40–75% and 25–60%, respectively. A recent trend has been upgrading biogas into a fuel gas product with at least 90% methane through some form of conditioning or removal of CO₂; albeit, for over ten years, this has been a goal of many government agencies [2]. More recently, upgraded biogas is beginning to be utilized on a larger scale. The upgraded product is commonly referred to as “RNG”, “sustainable natural gas”, or “biomethane” with RNG being the most commonly used term [2]. These conversions aim to position biogas as energetically similar to fossil fuel natural gas while capturing renewable fuel funding incentives. Within the USA, RNG is considered by the Environmental Protection Agency (EPA) as a “cellulosic biofuel” under its Renewable Fuels requirements set by its Renewable Fuels Standard portfolio [3,4]. Because of its ease of production, RNG has become the most common alternative to conventional fuel used within the USA, meeting EPA goals (i.e., volume targets, 60% lifecycle greenhouse gas reduction, etc.) [4]. The usage of RNG is expected to increase over the coming years. In 2025, the coupling of the Inflation Reduction Act of 2022 and the One Big Beautiful Bill of 2025, the IRS Tax Code 45V was refined to provide staggered tax credit incentives for the use of RNG to serve as a viable feedstock into the production of clean hydrogen [5]. This amended tax code will opened up new opportunities and markets for RNG for use in the production of clean hydrogen, particularly, RNG converted into hydrogen via several similar commercialized processes such as steam methane reforming and autothermal reforming [6]. Hence, there is an envisioned expansion of RNG markets as clean hydrogen production increases across the USA stimulated by the 45V tax credits.

It is envisioned that by 2050, RNG will be produced as a truly renewable source of methane, applying new and updated technologies from all types of organic wastes, by-products, and other renewable raw materials. RNG derived from biogas will likely provide the green component of the natural gas fuel mixture distributed throughout the European gas network along with increased usage within the USA. This gas will be used to generate electricity, provide heating and refrigeration, and even serve as a biofuel in the transportation sector. The European Biogas Association (EBA) suggested that by 2030 the goal for biogas production could reach 35 billion cubic meters per year in Europe, or about 10 percent of the European Union’s (EU) natural gas consumption [7,8].

Considering these projections and advances in biogas improvement technologies it is necessary to highlight several available technologies for biogas conditioning and upgrading that hold reasonable promise for large-scale application.

Thus, the objectives of this work are:

• Describe biogas, natural gas compositions, and the standard requirements for RNG in five European countries and the USA.
• Describe conditioning methods for typical contaminants present in the biogas matrix that yield higher methane compositions.
• Details on technology options for biogas upgrading that are currently being utilized.
• Discuss case studies and process designs.

As a product that can be an alternative to fossil fuel-based natural gas, biogas provides an attractive renewable energy source, creates local industry, reduces dependence on foreign gas imports, and decreases adverse environmental impacts. This information is intended to emphasize activities regarding biogas production, conditioning, and upgrading while also providing some basis for transitioning toward increasing global use.

2. Composition: Natural Gas and Biomethane

As outlined in Section 1, biogas is an important product of the anaerobic digestion of organic substrates. It is mainly composed of methane, carbon dioxide, and trace compounds like water vapor, hydrogen sulfide, oxygen, nitrogen, ammonium, siloxanes, hydrocarbons, and particles.

The methane content of biogas, and therefore the performance, depends on a wide variety of factors with varying levels of control [9,10,11,12,13]. Most commonly, the contributing factors are the following:

• Type of substrate material used.
• Concentrations of carbon contained in each substrate (see

  Table 1. Biogas Yield and Methane Content for Different Groups of Substances [10,11].

  Substance Group	Digestion Biogas Yield (L/Kg VS)	Methane Content
  (%v) Digestible Fat	1000–1250	70–75
  Digestible Protein	600–700	68–73
  Digestible Carbohydrates	700–800	50–55

  ).
• Weather conditions.
• The location of gas production.
• Type of technology used for production.
• Process conditions (Temperature, Residence Time, etc.).

Currently, the energy potential from biogas is being used on increasing scales; countries like Poland, the United Kingdom, Sweden, France, and Germany are taking advantage of this energy source. The last three (Sweden, France, and Germany) were among the most developed countries for electricity production and the three leading countries in European RNG production in 2016 [14]. The USA is falling behind other countries in its adoption of RNG as a realistic commercial fuel. The quality of biogas can vary significantly by country, as seen in Table 2. Natural Gas quality is shown in Table 3 for comparison. The quality of RNG is increased through two main steps:

• A conditioning process where trace components like water vapor, hydrogen sulfide, oxygen, nitrogen, ammonium, siloxanes, halogenated hydrocarbons, and particles are removed.
• An upgrading process to yield biogas containing the typical values of natural gas.

Table 2. Raw Biogas Composition in Different Countries.

Biogas Component	Units	Poland [15,16]	United Kingdom a [17,18,19]	Germany a,b [16,17,18,19]	France b [17,18,19]	Sweden b [18]	United States [20,21,22]
Methane	v/v%	63.4 ± 1.1	50–70	54.4 ± 0.9	50–75	65	50–70
	v/v%	60.2–67.7	60–70		53–70		60
	v/v%		53–70
Other Hydrocarbons c	mg/Nm3			0–200			Trace
Hydrogen	v/v%			<1			Trace
Carbon Dioxide	v/v%	36.6 ± 1.0	25–45	45.5 ± 0.8	25–45	35	25–50
	v/v%	32.2–39.5	30–47		30–47		36
	v/v%		<2		<2
Nitrogen	v/v%	0.003–0.525	0–3	0.1 ± 0.1	0–3	0.2	0–5
Oxygen	v/v%	0–0.083		<2			Trace
	v/v%			0–1			Trace
Hydrogen Sulfide	ppmv		<1000		<1000		0–7500
	ppmv	0–194	<500	16.0 ± 0.7	<500	<500	1000–1400
Ammonium	ppmv	0–0.84	<1	3.6 ± 1.0	<1	100	0–500
	ppmv		100		100
Min. Heating Valve	Btu/ft3			564			893
	Btu/ft3			617
Water	v/v%			2–7 d			1–5
	v/v%			5–10
Chlorine	ppmv	0–40		0–5
Fluorine	ppmv	0–5
Siloxane	mg/Nm3			0–41

^a Most Developed Electricity Generation, 2016. ^b Most Developed Biomethane Generation, 2016. ^c C₂ through C₅ n and i hydrocarbons. ^d Measured throughout the temperature range of 20–40 °C.

Table 2. Raw Biogas Composition in Different Countries.

Biogas Component	Units	Poland [15,16]	United Kingdom a [17,18,19]	Germany a,b [16,17,18,19]	France b [17,18,19]	Sweden b [18]	United States [20,21,22]
Methane	v/v%	63.4 ± 1.1	50–70	54.4 ± 0.9	50–75	65	50–70
	v/v%	60.2–67.7	60–70		53–70		60
	v/v%		53–70
Other Hydrocarbons c	mg/Nm3			0–200			Trace
Hydrogen	v/v%			<1			Trace
Carbon Dioxide	v/v%	36.6 ± 1.0	25–45	45.5 ± 0.8	25–45	35	25–50
	v/v%	32.2–39.5	30–47		30–47		36
	v/v%		<2		<2
Nitrogen	v/v%	0.003–0.525	0–3	0.1 ± 0.1	0–3	0.2	0–5
Oxygen	v/v%	0–0.083		<2			Trace
	v/v%			0–1			Trace
Hydrogen Sulfide	ppmv		<1000		<1000		0–7500
	ppmv	0–194	<500	16.0 ± 0.7	<500	<500	1000–1400
Ammonium	ppmv	0–0.84	<1	3.6 ± 1.0	<1	100	0–500
	ppmv		100		100
Min. Heating Valve	Btu/ft3			564			893
	Btu/ft3			617
Water	v/v%			2–7 d			1–5
	v/v%			5–10
Chlorine	ppmv	0–40		0–5
Fluorine	ppmv	0–5
Siloxane	mg/Nm3			0–41

^a Most Developed Electricity Generation, 2016. ^b Most Developed Biomethane Generation, 2016. ^c C₂ through C₅ n and i hydrocarbons. ^d Measured throughout the temperature range of 20–40 °C.

Table 3. Natural Gas Composition.

Biogas Component	Units	Wet a	Dry a	United Kingdom	Germany [11,23]	France [11]	Sweden [11]	United States [24,25,26]
Methane	v/v%	84.6	96		≥70			87.0–97.0
Other Hydrocarbons	v/v%	0.1–6.4	0.06–2		0			0–9.0
Hydrogen	v/v%							0–0.02
Carbon Dioxide	v/v%	<5	<5	0–1.8	<5	2.5	3	0.05–1.0
Nitrogen	v/v%	<10	<10		<10			0.2–5.5
Oxygen	v/v%			0–0.2	3	1	1	0–0.1
Hydrogen Sulfide	ppmv	<5	<5	5	<6.5	5	10	0.0055
Ammonium	ppmv					3	20
Min. Heating Valve	Btu/ft3	1047	1047	37–47	36.0–45.72	38.5–46.1 H	39.6–43.2	36.0–40.2
	Btu/ft3				30.2–47.2	34.2–37.7 L
Water	mg/Nm3						<32	16–32

^a Typical Composition [17,27]. ^H High Quality Gas. ^L Low Quality Gas.

Table 3. Natural Gas Composition.

Biogas Component	Units	Wet a	Dry a	United Kingdom	Germany [11,23]	France [11]	Sweden [11]	United States [24,25,26]
Methane	v/v%	84.6	96		≥70			87.0–97.0
Other Hydrocarbons	v/v%	0.1–6.4	0.06–2		0			0–9.0
Hydrogen	v/v%							0–0.02
Carbon Dioxide	v/v%	<5	<5	0–1.8	<5	2.5	3	0.05–1.0
Nitrogen	v/v%	<10	<10		<10			0.2–5.5
Oxygen	v/v%			0–0.2	3	1	1	0–0.1
Hydrogen Sulfide	ppmv	<5	<5	5	<6.5	5	10	0.0055
Ammonium	ppmv					3	20
Min. Heating Valve	Btu/ft3	1047	1047	37–47	36.0–45.72	38.5–46.1 H	39.6–43.2	36.0–40.2
	Btu/ft3				30.2–47.2	34.2–37.7 L
Water	mg/Nm3						<32	16–32

^a Typical Composition [17,27]. ^H High Quality Gas. ^L Low Quality Gas.

Many contaminant compounds removed during the conditioning process can cause corrosion and mechanical wear in equipment. For this reason, RNG is almost always treated in a conditioning process, while upgrading depends on the initial gas quality and desired end use. Usually, conditioning is performed to meet standards to allow for RNG injection into the natural gas network or as fuel for power generation or vehicles.

Table 4. Standard Requirements for Renewable Natural Gas by Country.

Biogas Component	Units	France [10,28]	Germany [10]	Sweden [10,28]	United States [24,25,26]
Wobble Index	MJ/Nm3	48.2–56.5 H	46.1–56.5	44.7–46.4	43.4–44.4
	MJ/Nm3	42.5–46.8 L	37.8–46.8
Methane	v/v%	≥86	≤70	95–99	87.0–97.0
Carbon Dioxide	v/v%	<2	<6	≤3	0.05–1.0
	v/v%	2.5	<3	≤1	0–0.1
Oxygen (Dry Gas)	v/v%		3
Oxygen (Wet Gas)	v/v%		0.5
Hydrogen	v/v%	<6	≤5	≤0.5	0.0055
CO2 + O2 + N2	v/v%			≤5
Water Dew Point	°C	<5 a	<T c	≤T d–5
Sulfur	mg/Nm3	75 b	<30	≤23
	mg/Nm3	30

^a At Maximum Operating Pressure (MOP) Downstream from Injection Point. ^b Average Content. ^c Ground Temperature. ^d Ambient Temperature. ^H High Quality Gas. ^L Low Quality Gas.

shows some of these standard requirements [13].

3. Conditioning of Typical Contaminants

Biogas is produced from a wide variety of sources, and each can bring unique challenges to the utilization of the resulting product gas.

Table 5. Benefits of Contaminant Removal from Biogas.

Contaminant	Removal Benefit
Water	- Prevents corrosion in compressors, gas storage tanks and engines due to the reactions with H2S, NH3 and/or CO2 to produce acids. - Avoids water accumulation in pipes. - Prevents condensation and/or freezing due to high pressure.
Hydrogen Sulfide	- Prevents corrosion in compressors, gas storage tanks and engines. - Avoids concentrations of toxic H2S (>50 ppm) that remain in biogas. - Prevents formation of SO2 and SO3 due to the combustion of H2S.
Oxygen and Nitrogen	- Avoids explosive mixtures due to high concentrations of O2 in biogas. - Avoids the formation of corrosive compounds such as NH3.
Ammonium	- Avoids corrosion when dissolved in water.
Siloxane	- Avoids the formation of SiO2 and micro-crystalline quartz due to combustion. Prevents deposition in spark plugs, valves and heads embracing the surface.
Hydrocarbons	- Prevents corrosion in engines due to combustion (non-methane volatile organic compounds).
Particles	- Avoids obstruction due to deposition in compressors and gas storage tanks.

shows common contaminants found in biogas as well as the major benefits of their removal. This section deals with technologies that remove and/or reduce these contaminants in preparation for direct end use or further upgrading. In contrast to chemical species covered here, carbon dioxide reduces the heating value of biogas but does not otherwise affect its chemical compatibility or reactivity. Removal of CO₂ by current methods is therefore covered separately in Section 4.

3.1. Water Removal

When biogas is saturated with water vapor flows through a pipe, water condenses and accumulates inside the pipeline, reducing available space for the proper flow of biogas. This biphasic flow of gas–liquid mixtures creates an unstable system and decreases total gas flow. In addition, condensate water and biogas-sourced impurities cause corrosion and clogging of metal pipes, making frequent conditioning a necessity. The removal of water is of concern in many industrial processes and allows for the repurposing of technology from other sectors. All of the water removal methods listed here work more efficiently at low temperatures and elevated pressures.

3.1.1. Condensate Traps

Liquid water can be separated from biogas by increasing pressure and reducing temperature to condense water vapor. This technology is best suited for bulk removal and leaves trace amounts of residual water behind, but it is a cheap and effective first step. If total water vapor elimination is desired, the biogas can then be treated with further cooling, compression, absorption, and adsorption processes.

3.1.2. Absorption and Adsorption

Contacting biogas with a liquid that exhibits a high affinity for water and a low affinity for methane can absorb water out of the gas phase. Absorption is commonly performed in a counter-current liquid–vapor contactor where a liquid phase, such as glycol, falls down through biogas as water vapor rises to the top. The water vapor is then absorbed into the liquid phase and exits the apparatus, where it can be regenerated for reuse.Contacting biogas with a solid that traps water vapor via chemical or physical interaction is known as adsorption. Gas is pushed through a pipe or bed where water is trapped on the surface of a chosen adsorbent allowing dewatered gas to exit the process. Unlike absorption, adsorption equipment can be mounted in any orientation and does not require liquid handling. Silicon dioxide, aluminum oxide (alumina), activated coal, hygroscopic salts, and molecular sieves are commonly used adsorbents in industrial processes. The absorption and adsorption materials can be regenerated by increasing the temperature or lowering the pressure [10,13,29].

3.2. Hydrogen Sulfide Removal

Hydrogen sulfide (H₂S) is an extremely toxic and flammable gas, harmful to human health and the environment. The Occupational Safety and Health Administration (OSHA) limits long-term exposure to 20 ppm of H₂S during an 8 h shift, with 100 ppm listed as immediately threatening to life and health [30]. It is commonly found in anaerobic digesters resulting from a microbiological reduction of sulfur-containing compounds (peptides, amino acids, etc.). The concentration of H₂S gas can be reduced within the biogas reactor by precipitation within the liquid of the digester. Biogas can be de-sulfured using multiple processes, including physical, chemical, and biological sulfate reduction. Removal limits are normally dependent on application, examples of which can include: 100 ppm concentration for internal combustion engines, 3–4 ppm for most applications as a substitute for natural gas applications, and less than 1 ppm for gas grid injection and transport [31]. Selection of the best process for each digester depends on gas composition, the H₂S levels to be treated, and the mass flow of treated gas [10,29,32,33].

3.2.1. Precipitation

When absorbed into water, hydrogen sulfide disassociates into ions, as seen in Equations (1) and (2). One proven method of H₂S removal is treatment with compounds that disassociate into iron ions, such as ferrous and ferric chloride (Fe₂⁺ & Fe₃⁺). These react with sulfide ions to precipitate iron sulfide, shown in Equations (3) and (4), thus removing it from the digester before it can be released as a gas. This process is mainly used when hydrogen sulfide concentrations in the biogas are high, often 1000 ppm or higher [10,34].

$${\mathrm{H}}_2\mathrm{S}\iff \mathrm{H}\mathrm{S}+{\mathrm{H}}^{+}$$

(1)

$$\mathrm{H}\mathrm{S}\iff {\mathrm{S}}^{=}+{\mathrm{H}}^{+}$$

(2)

$$\mathrm{F}{\mathrm{e}}_2^{+}+\mathrm{H}{\mathrm{S}}^{-}\to \mathrm{F}\mathrm{e}\mathrm{S}+{\mathrm{H}}^{+}$$

(3)

$$2\mathrm{F}{\mathrm{e}}_3^{+}+3\mathrm{H}{\mathrm{S}}^{-}\to \mathrm{F}{\mathrm{e}}_2{\mathrm{S}}_3+{\mathrm{H}}^{+}$$

(4)

3.2.2. Adsorption Technologies

Similarly to water vapor removal, the adsorption of hydrogen sulfide gas onto solid substrates removes the H₂S from biogas. The use of granular activated carbon (GAC) and iron oxide as adsorbents is effective, operationally simple, and has a long history of implementation in industry. As demonstrated in Equation (5), iron oxide reacts with hydrogen sulfide to produce ferric sulfide. However, these adsorbents are generally suited for treating lower concentrations of H₂S (<300 ppm) and mostly operated as a batch process due to the spent bed requiring regeneration for continuous processes [35]. Treating a 100 L per minute gas stream with 300 ppm H₂S would have an estimated annual media cost of $59 for iron sponge units, $272 for GAC, and $590 for activated carbon [36]. Further, the spent adsorbent can be regenerated by treatment with oxygen but only recovers about 60% of the original removal capacity [37].

$$2\mathrm{F}{\mathrm{e}}_2{\mathrm{S}}_3+6{\mathrm{H}}_2\mathrm{S}\to 2\mathrm{F}{\mathrm{e}}_2{\mathrm{S}}_3+6{\mathrm{H}}_2\mathrm{O}$$

(5)

Activated carbon can treat significantly higher levels of H₂S but at a substantial increase in cost. For example, reference studies on a hog farm treated hydrogen sulfide at 2400 ppm over a projected installation lifetime. The economic analysis revealed that activated carbon usage caused an increase in the payback period from 4.3 to 7.9 years versus the baseline option [38]. While regeneration of activated carbon is possible, the recovery is poor. Coppola & Papurello (2018) used data from a municipal wastewater treatment plant and found their maximum activated carbon regeneration to be 30% [39]. The calculated savings in this case study equated to 16% over the projected 4-year lifetime. Without increases in adsorption capacity, higher regeneration limits, or lowered cost, activated carbon is generally inferior to iron oxide in small biogas operations [40].

One removal method commonly under consideration is the use of low-cost alternative adsorbents produced from natural materials such as wood, peat, coal, lignite, or agricultural waste [41,42]. Domestic and industrial waste treatment operations by-products such as slag, sludge, and other solid wastes have also been considered [43]. As seen in

Table 6. Surface Area of Various Adsorbents [41,43].

Material	Surface Area (m2/g)
Industrial Carbonate Waste	3.6
Garden Grass	21.28
Slag	107
Sewage Sludge a	390
Sugarcane Bagasse	606.8
Pinewood a	902
Corncob a	943
Sugarcane Bagasse a	1433
Commercial Carbon a	2000

^a Activated.

these low-cost alternatives have significantly lower surface areas and a correspondingly small adsorption capacity versus commercially produced GAC. Enhancing adsorption capacity by chemically conditioning the material is one way to increase economic value. The carbon in these alternatives can be doped with catalysts by the addition of permanganate reactive species, potassium iodide, potassium carbonate, zinc oxide, sodium hydroxide, or ferric oxide, increasing reaction kinetics, total adsorption capacity, and sulfide-reduction [44]. Even though carbon impregnated with zinc oxide is expensive, it effectively removes hydrogen sulfide at concentrations higher than 1 ppm [10,42,45]. Makaruk et al. used water hyacinth biomass modified via carbonization and achieved H₂S removal of 31.85 g per 100 g of biomass [46].

3.2.3. Photocatalytic Oxidation

Another alternative method for desulfurization is photocatalytic oxidation. Xiaoyan Hao et al. found promising results by using zeolite/TiO₂ granules within a photocatalytic reactor, achieving an H₂S removal rate of 98.1%. However, this process contained issues with the regeneration of the oxidizing granules due to performance depletion [47]. Jung-Jeng Su et al. proposed a photocatalytic biogas desulfurizing reactor system that oxidizes biogas with TiO₂-coated clay aggregate carriers in conjunction with U.V. irradiation [48]. A proposed mechanism for converting H₂S to SO₂ is below in Equations (6)–(11).

$${\mathrm{H}}_2\mathrm{S}+8·\mathrm{O}\mathrm{H}\to \mathrm{S}{\mathrm{O}}_4^{2-}+2{\mathrm{H}}^{+}+4{\mathrm{H}}_2\mathrm{O}$$

(6)

$$\mathrm{T}\mathrm{i}{\mathrm{O}}_2+\mathrm{h}\surd \to {\mathrm{h}}^{+}+\mathrm{e}$$

(7)

$${\mathrm{h}}^{+}+{\mathrm{H}}_2{\mathrm{O}}_{\mathrm{a}\mathrm{d}\mathrm{s}\cdot }\to \cdot \mathrm{O}\mathrm{H}+{\mathrm{H}}^{+}$$

(8)

$${{{\mathrm{h}}^{+}+\mathrm{O}\mathrm{H}}^{-}}_{\mathrm{s}\mathrm{u}\mathrm{p}\mathrm{e}\mathrm{r}\mathrm{f}.}\to \cdot \mathrm{O}\mathrm{H}+{\mathrm{H}}^{+}$$

(9)

$${\mathrm{O}}_2+2{\mathrm{e}}^{-}+2{\mathrm{H}}_2\mathrm{O}\to {\mathrm{H}}_2{\mathrm{O}}_2$$

(10)

$${\mathrm{H}}_2\mathrm{S}+4{\mathrm{H}}_2{\mathrm{O}}_2\to {\mathrm{S}\mathrm{O}}_4^{2-}+2{\mathrm{H}}^{+}+4{\mathrm{H}}_{2}0$$

(11)

All experimental results from this study provided >99% removal of H₂S from biogas in the presence of sufficient oxygen. However, at H₂S concentrations higher than 836 mg/m³, oxidation of H₂S on the surface of TiO₂ and the lightweight expanded clay aggregate was hindered due to sulfate absorbance [48]. Costs associated with this technology are low in installation, operation, and maintenance compared with conventional methods [47,48]. This process negates expensive or timely carrier or sorbent replacement.

3.2.4. Chemical Absorption

Several commercial processes use chemical absorption to remove hydrogen sulfide from raw biogas. One of the most established systems handling large volumes and high concentrations of H₂S is washing with sodium hydroxide solutions (NaOH) [49]. However, it has drawbacks in biogas use due to the high carbon dioxide content interfering with and consuming hydroxide reagents more rapidly. Other forms of absorption may be utilized, such as chelating solutions with iron/ethylenediaminetetraecetic acid (EDTA), which converts the hydrogen sulfide into elemental sulfur [50]. These processes can eliminate up to 2000 ppm of hydrogen sulfide of the gas at 40 °C, atmospheric pressure, and with a capacity of 1000 Nm³ of crude gas per hour. When the absorbent material becomes saturated, it is necessary to regenerate or replace it. An important point is the recovery and reuse of the spent material. For example, the metal ion can be regenerated by oxidation, converting sulfur dioxide into sulfur to produce sulfuric acid or gypsum [10,51].

3.2.5. Biological Treatment

The biological treatment of biogas with sulfur-oxidizing bacteria (SOB) allows for hydrogen sulfide conversion into elemental sulfur or sulfate within the liquid phase. Hydrogen sulfide can be oxidized by Sulfolobus and Thiobacillus species, among others [10]. Cheng et al. detail a commercial pilot study involving multi-stage removal of H₂S from biogas [32]. An inlet biogas stream with high H₂S concentrations is contacted in a counter-current spray tower where the sulfide is absorbed into a slightly alkaline liquid solution. This sulfide-rich liquid stream continues into a controlled aeration tank where SOB converts the dissolved sulfide into elemental sulfur. The effluent from this tank passes through a settling process to remove the clarified, low-sulfide liquid, where it can then be recycled back to absorb more H₂S. Stable sulfide removal rates of up to 95% were seen during the two-month operation [32]. The transformation performance depends on several operating conditions, including the composition of the substrate, pH of the culture medium, hydrogen sulfide loading, suspended or immobilized conditions of SOB, level of adaptation to changes of H₂S content in biogas, and the dissolved oxygen (D.O.) in solution. Dissolved oxygen levels are critical to the production of elemental sulfur. Excess oxygen can lead to sulfite production and will remain as a contaminant in the solution. Separating the H₂S absorption step from the oxidation step is advantageous since it does not add additional oxygen to the clean biogas effluent. Some advantages of this treatment are its low operating cost, high efficiency toward sulfur separation, minimal sludge production, and no secondary pollution [10,32].

3.3. Oxygen and Nitrogen Removal

During anaerobic digestion, it can be difficult to prevent the introduction of oxygen into the digester. However, Methanogenic Archaea are resilient microorganisms that can tolerate small changes in digester conditions. Introducing relatively low oxygen concentrations will not cause a complete collapse of the microbial community. The digester environment will also contain some facultative anaerobic bacteria capable of consuming oxygen at low levels and avoiding significant methane production interruptions. Any air added into the digester due to poor operation or equipment design will result in the presence of nitrogen in the biogas. For example, oxygen and nitrogen may be present in landfill gas if the gas is collected using vacuum systems. These gases can be removed by adsorption with activated carbon, molecular sieves, or membranes [52]. They can also be eliminated to some extent via sulfate-reduction processes. Using biogas as RNG necessitates removing both nitrogen and oxygen gases to achieve the required purity. The most utilized processing method for removal is catalytic elimination with palladium–platinum catalysts and chemisorption with copper contacts [10,11]. Another method that Ming Xu et al. presented involves co-culturing microalgae with endophytic bacteria to increase nitrogen and oxygen removal efficiency for biogas purification [53].

3.4. Ammonium Removal

Ammonium (NH₄⁺) can serve as an inhibitor of the anaerobic digestion process and is formed naturally during protein degradation. Equation (12) presents that dissolved ammonium is in equilibrium with an ammonia (NH₃) concentration, which is dependent on the temperature and pH of the digester. Aqueous solutions with a basic pH will create higher concentrations of aqueous ammonia, which is in balance with gaseous NH₃ in the digester’s headspace.

$$\mathrm{N}{\mathrm{H}}_{3\left(\mathrm{a}\mathrm{q}\right)}+{{\mathrm{H}}_2\mathrm{O}}_{\left(\mathrm{l}\right)}\iff \mathrm{N}{\mathrm{H}}_{4\left(\mathrm{a}\mathrm{q}\right)}^{+}+{\mathrm{O}\mathrm{H}}_{\left(\mathrm{a}\mathrm{q}\right)}^{-}$$

(12)

Absolute limits cannot be placed on aqueous NH₃ concentrations as even low amounts of ammonia can have a harmful impact on bacteria. For example, an increase in the pH value from 6.5 to 8.0 causes a 30× increase in ammonium concentrations. Digester temperature also positively correlates with the equilibrium between ammonium and ammonia, with increasing temperatures driving higher ammonia concentrations. The ammonium can be separated when biogas is dried or upgraded. Therefore, a separate conditioning step is not usually necessary [10,11].

3.5. Siloxane Removal

Siloxanes are a family of compounds containing silicon, oxygen, and methyl groups commonly called Volatile Organic Silicon Compounds (VOSCs). These compounds can be found in the biogas generated in municipal wastewater treatment plants and landfill gas since they are commonly used to manufacture personal hygiene, health care, and industrial products [54]. When burned, siloxane-containing biogas is converted into silicon dioxide (SiO₂). Power production equipment such as gas turbines, boilers, and internal combustion engines can experience deposition of SiO₂ as a white powder in their combustion and exhaust stages, resulting in significant maintenance costs and downtime. Buildups of SiO₂ also occur in heat exchangers and as a coating on post-combustion catalysts. The maximum allowable level for siloxane concentration in biogas is generally given as 5 mg/Nm³ or lower for internal combustion and 0.1 mg/Nm³ or lower for turbines [54,55,56]. These limits are significant given that VOSCs from most sources range well above the recommended limits, necessitating conditioning or processing of the gas. An overview of different biogas sources can be seen in

Table 7. Reported Values of Siloxane by Process.

Source	(mg/Nm3) a
European Union [57]
- Municipal Sewage Sludge Digesters	3.4–15.4 (10)
- Food Waste Digesters	t—12.4 (1.3)
- Manure Digesters	t—0.6
- Energy Crop Digesters	t—25.3 (10)
United States [58,59]
- Municipal Landfills	4.5–161
- Municipal Landfills	9.6–15.6
- Municipal Sewage Sludge Digesters	5.2–8.2

^a Average Value denoted by ( ). t—Trace amounts VOSCs.

in both the USA and EU. The biogas from manure digesters contain very few VOSCs due to the lack of siloxanes in the feedstock.

Several methods can eliminate these siloxanes depending on the facilities available and the desired treatment level. Bio-trickling filtration is typically cheaper than other methods. However, this process removes less than half of the siloxanes and often requires a subsequent treatment with other high-cost methods [60]. Cooling the gas to condense VOSCs, adsorption (on GAC, alumina, or silica gel), degrading with a mineral acid, biological removal, or absorption into liquid hydrocarbon mixtures are all able to provide removal efficiencies of greater than 95% [54]. Comparing treatment options to that of H₂S, there is significant overlap. Adsorption and absorption can provide simultaneous H₂S and VOSCs removal which leads to a lower overall treatment cost [10,11,29]. As a low-cost commercial precursor, silicon dioxide is not valuable enough to offset removal costs during processing; therefore, it is unnecessary to remove unless needed to meet vendor or regulatory requirements.

3.6. Hydrocarbon Removal

Heavy hydrocarbon removal from biogas may be required depending on the end use case, including transportation or 3rd-party sale. The target regulations include a hydrocarbon dew point specification of −10 °C [61]. This helps ensure no liquid species condenses in pipelines or equipment. Specifications for halogenated hydrocarbons depend on the end-use type but fall in the ppm range. For example, fuel cells are limited to 0.1–1 ppm of halogenated compounds [62].

Pressure swing adsorption (PSA) and temperature swing adsorption (TSA) are commonly used methods for reducing the hydrocarbon dew point and removing contaminants. Carbon dioxide and heavy hydrocarbons are adsorbed on a solid bed at either high pressure (PSA) or high temperature (TSA). Depending on processing time and other operating conditions, the effluent gas can contain less than 50 ppm CO₂ and have a hydrocarbon point of less than −10 °C [61]. After purification, the beds are regenerated by lowering the pressure or raising the temperature.

Halogenated hydrocarbons (HHCs), particularly chlorine and fluorine compounds, are not common in agricultural or commercial digester biogas. However, the compounds are often found in landfill gas as a by-product of waste decomposition. Ong et al. collated reported sources and determined that MWTPs and agricultural digesters contained between 0 and 2 mg/Nm³ while landfill sources contained 0.3–2900 mg/NmHHCs³ [63]. When halogens combine with water, they cause corrosion in combined heat and power (CHP) engines and related piping, resulting in costly maintenance [64]. In comparison to other impurities covered above, removal can be easily accomplished via washing. In one such study by Rasi et al., 96% of halogenated hydrocarbon compounds were removed from a target gas stream with counter-current water washing under 20 bar pressure [65]. This process has the beneficial side effect of simultaneously removing CO₂ as well, thus increasing the value of effluent biogas. Gas-to-water volumetric flow ratios across the range of 5–20:1 all showed removal exceeding 85% CO₂ at 20 bar.

Activated carbon can be used to adsorb hydrocarbons at atmospheric pressure and is more efficient at removal than absorption into liquid. However, doing so will not remove significant amounts of carbon dioxide, nitrogen, oxygen, or other gases. Activated carbon can also not regenerate to its original adsorption capacity and must, therefore, be replaced regularly [39].

3.7. Particle Removal

Production of biogas often entrains small particles in the vapor stream as it leaves digestion systems. Depending on the targeted use of the biogas generated, particles must be removed to avoid mechanical wear in internal combustion engines and gas turbines. The most common method of removal is separation, which employs mechanical filters that physically trap particles as gas flows through them. Removal requirements vary by manufacturer but can range from a maximum particle loading of 10–50 mg/Nm³ of gas with sizes no larger than 0.3–10 µm [29]. Stirling engine burners have a high tolerance for siloxanes and other particles, so it may not be necessary to pretreat the gas if this applies [29,66]. Particles are also produced during combustion itself, but with a much smaller diameter on the nanometer scale. While these may pose a health risk similar to particulate matter from other combustion engines, they are not mechanical concerns or are limited only to biogas [67].

4. Current Technologies for Biogas Upgrading

Biogas upgrading technologies have traditionally focused on removing carbon dioxide to improve the heating value of raw gas. While some of the conditioning processes covered previously reduce CO₂ as a side effect, their removal efficiency is too low for producing pipeline-quality biogas. As detailed in

Table 8. Technologies Available for the Improvement of Clean Biogas.

Available Technologies	Objective	Benefits
Physical Absorption with Water	CO2 Removal	Simple process, non-toxic
Physical Absorption with Organic Solvents	CO2 Removal	High capacity, low regeneration energy
Chemical Absorption with Amines	CO2 Removal	High CH4 purity
Pressure Swing Adsorption	CO2 Removal	No reagent disposal issues
Membrane Separation	CO2 Removal	Compact equipment, long life

, several commercial processes are currently used to further condition raw biogas to meet a specified use. These processes are based on physical/chemical absorption, adsorption, and membrane separation [68].

The main objective of each process is removing carbon dioxide while retaining the maximum amount of methane. However, each treatment has specific drawbacks related to its use. In 2018, five technologies were reported to be successfully used at reasonable scales for biogas upgrading in Europe [68]. At their core, each is based on water purification, chemical absorption, adsorption by oscillation pressure, membrane separation, or physical absorption. The landscape of regulatory requirements, public support, investor willingness, biogas source, clean gas target, and many other unknown factors contribute to the particular technologies utilized at treatment plants. A snapshot of historical plant populations in Europe and Asia can be seen in

Table 9. Upgrading Technology Plant Type by Year.

	2009	2015	2016	2017	2020	2024
Total Number of Upgrading Plants	127	428	480	532	606	795
Physical Absorption with Water	34%	34%	34%	30%	30%	18%
Physical Absorption with Organic Solvents	9%	5%	4%	4%	3%	3%
Chemical Absorption with Amines	11%	22%	19%	18%	17%	14%
Pressure Swing Adsorption	36%	17%	17%	14%	13%	12%
Membrane Separation	10%	21%	24%	25%	29%	48%
Other Technologies	-	2%	2%	9%	8%	4%

Data collated from Task 37 Member Countries and https://www.ieabioenergy.com.

, where both the total number of upgrading facilities and technologies utilized are organized by year. Germany contains the largest number of upgrading sites of all polled countries, with 200 locations in 2017, compared to 532 locations in all fourteen countries combined [14]. The polled data shows a dramatic increase in the use of membrane separation versus traditional absorption methods over the past few years.

4.1. Physical Absorption via Water Washing

Although other technologies are gaining market share, water washing is still the most used technology for conditioning and improving biogas quality. Water is a low-cost solvent compared to many organic chemicals and is often more environmentally friendly as well [69,70]. Carbon dioxide is removed preferentially compared to methane because of its higher solubility in water. This is detailed in

Table 10. Solubility of Biogas Components in Water [71].

Gas Components	0 °C	25 °C
Hydrogen Sulfide	205	102
Carbon Dioxide	75	34
Methane	2.45	1.32

for 0 °C and 25 °C, where the solubility of methane is several orders of magnitude lower than carbon dioxide.

Henry’s Law states that the concentration of a gaseous compound in water is proportional to its vapor phase concentration and inversely proportional to system temperature. Absorption is most efficient at low temperatures and high pressures, allowing minimization of the process water needed during treatment [72]. Figure 2 presents a typical continuous flow water absorption process. During this treatment, the biogas is pressurized between 6 and 12 bar with temperatures up to 40 °C. Biogas is injected into the bottom of the absorption column while process water is injected at the top. Carbon dioxide and methane transfer from gas to liquid phase inside the absorption column according to solubility, flow rates, and system conditions [73,74,75,76]. In normal practices, the column is filled with a crush-resistant, high surface area packing material, allowing for a large contact area between gas and water to increase the transfer of gas into the liquid phase [69,73,76]. After contact the column’s liquid effluent stream consists of water, dissolved CO₂, and small amounts of CH₄, while the vapor stream is purified methane ready for further processing [68]. Methane stream purities of up to 95% are obtainable with this method [77].

Costs can be minimized by processing the used absorption water and recycling it back into the process, which is the most common configuration [64]. The effluent aqueous phase is transferred from the bottom of the column to a flash drum, where the pressure drops from 6–12 bar to 2–4 bar. Due to changing solubility, most of the CO₂ absorbed in the solution is released during the pressure drop. Water leaving the flash drum still contains enough CO₂ to prevent its use in absorption so it continues into a stripping column and is contacted with fresh air. The counter-current contact of the spent water and fresh air strips the remaining CO₂ out of the solution and allows the process water to be recycled [68,73,76]. Carbon dioxide exiting the desorption column, along with other trace gases, is deodorized by its passage through a filter and is in many cases released into the atmosphere, which increases the carbon footprint of the process due to greenhouse gas (GHG) emissions [78]. In comparison, the CO₂ can be captured, stored, or utilized to reduce GHG release and facilitate a reduced carbon footprint [79]. Data from pilot studies found an overall energy efficiency of 89.8% relative to the produced gas energy content when used for grid injection [12]. Continued studies, observed by Vilardi et al. [80] found that through simulations, water scrubbing had the largest exergy efficiency of 94.5% and a 99% methane recovery. In addition to the resulting exergy efficiencies of 91.1% and 90.8%, these two recovery percentages were found for membrane separation and amine scrubbing, respectively.

Alternatives for the utilization of CO₂ to reduce emissions into the atmosphere have been proposed and tested by several groups. Microalgae utilizes CO₂ as a carbon source for cell growth and is one of the most promising sequestration technologies. Capture efficiencies of >80% are easily obtained with some configurations removing >95% of released carbon dioxide [81,82,83].

4.2. Physical Absorption Using Organic Solvents

This method is based on the absorption of unwanted components, CO₂ and H₂S, into non-reactive organic solvents [68,84]. In contrast to chemical absorption, this process describes the interaction between compounds and the organic solvent that is physical. Commonly, the most used organic solvents are mixtures of methanol and dimethyl ethers of polyethylene glycol (DEPG). Marketable chemicals are also available under the trade name of Genosorb^Ⓡ (Clariant), the commercialized Selexol^Ⓡ (DOW Chemicals) process [42,84,85,86]. The advantage of organic solvents over water washing is the increased solubility of CO₂. The Selexol^Ⓡ processes using DEPG can absorb three times more CO₂ than water, giving an advantage to biogas conditioning units with smaller process footprints. However, the high solubility of both CO₂ and H₂S in these solvents could also be viewed as a disadvantage in terms of energy consumption because of the high temperatures for solvent regeneration.

Energy consumption could be reduced by removing H₂S before applying organic solvents [64,84]. In this case, H₂S-free biogas is compressed (7–8 bars), cooled, and injected into the bottom of the absorption column visualized in Figure 3. The organic solvent is added in counter-current flow at approximately 20 °C. As with water/amine systems, temperature influences CO₂ solubility in the solvent and gas/liquid equilibrium. The column is filled with a random packing material (pall rings) to increase the contact surface between the solvent and biogas [68,72,73,76]. Once the organic solvent absorbs CO₂, the conditioned biogas, RNG, can be delivered into a gas network for distribution or other uses. The spent organic solvent exiting the bottom of the absorption column is introduced to a flash drum for CO₂ removal and further solvent reutilization. The pressure in the flashdrum depends on the methane losses, pressure on methane losses, pressure on the absorption column, and the methane concentration in the raw biogas. In the process of organic solvent regeneration, it is necessary to heat the solvent (40–80 °C) before entering the desorption column [72,86]. Process heat exchangers can provide some of the energy for this heating through the capture of the compressor’s wasted heat. Once heated, the solvent is injected into the upper part of the column at 1 bar. This column is also filled with random packing to increase the contact surface area between the solvent, and air, injected counter-currently as a stripping agent. Due to the non-corrosive characteristics of organic solvent, the piping does not have to be made of stainless steel. The low freezing point of organic solvents allows the system to operate at as low as −20 °C without the need for extra heating [72]. In colder climates, this lack of required heating for absorption combined with increased absorption efficiency at low temperatures provides significant benefits over water/amine systems.

4.3. Chemical Absorption Using Amine Solutions

The second most popular CO₂ removal method uses an amine reagent that binds chemically to carbon dioxide, thus removing it from the biogas. Water is used as the solvent with amine concentrations of 20–50% by weight depending on the chosen compounds [87]. In practice, common amines used for CO₂ removal are methyl diethanolamine (MDEA), diethanolamine (DEA), and monoethanolamine (MEA). Similarly to water absorption, CO₂ dissolves into solution, leaving a purified methane vapor stream. In contrast, however, further reactions with liquid amine convert the CO₂ to other compounds, dramatically increasing the liquid’s capacity for CO₂ removal. Absorption at low temperatures leads to more CO₂ dissolved in solution, while higher temperatures increase the reaction speed of CO₂ conversion. Chemical reactions in amine systems can be very complex with many intermediate steps. A simplified formula for the process can be seen in Equation (13) for the case of MEA, denoted as RNH₂. Reactions during absorption are exothermic, leading to a temperature increase of 20–65 °C. This may necessitate cooling of the liquid stream before it can be recycled for further use. As detailed earlier, another advantage of this technology is that amines selectively absorb sulfides and CO₂, allowing for the simultaneous removal of H₂S. Amine absorption is commonly used for upgrading fossil fuel-based natural gas as well [88].

$$\mathrm{R}\mathrm{N}{\mathrm{H}}_{2\left(\mathrm{a}\mathrm{q}\right)}+{\mathrm{C}\mathrm{O}}_2+{\mathrm{H}}_2\mathrm{O}\iff {\mathrm{H}}_3{\mathrm{O}}^{+}+\mathrm{N}\mathrm{R}{\mathrm{H}}_2{\mathrm{C}\mathrm{O}\mathrm{O}}^{-}$$

(13)

A description of the aminization process is shown in Figure 4. After initial conditioning, biogas enters through the column’s bottom and contacts the amine solution, flowing counter-current from the top at pressures of 1–2 bar. Molar feed ratios of amine to CO₂ vary from 2 to 7:1 to avoid reaction equilibrium restrictions and keep amine in excess [89]. Biogas containing purified methane exits the column’s top, while the amine solution with the captured CO₂ exits below. Within the stripper column, the liquid is rapidly depressurized in a flash unit where equilibrium changes release large amounts of CO₂ from the solution. The liquid is then distributed and passed over packing material, where it contacts clean vapor, stripping the remaining CO₂. A kettle boiler at the stripper’s bottom is used to heat the system to 120–150 °C, partially boiling the amine and water solution. The reboiler’s purpose includes: first, providing the heat of reaction required for the release of CO₂ bound with amine; and second, generating steam to reduce the partial pressure of CO₂ in the column [89]. Although limited by equilibrium, the high temperatures and low concentration of CO₂ in vapor push a majority of the carbon dioxide out of the liquid phase, allowing the liquid to be reused in further absorption. If a reboiler is used, provided heat at 90 °C or lower a vacuum-operated stripping column is required to pull CO₂ out of the solution. Effluent vapor from the stripper is cooled to condense any steam and amines; then it is sent back to the column while CO₂ remains in the vapor phase for release or capture [72].

Unlike water absorption systems, the pH of amine columns is high enough to retard bacterial growth. Therefore, any vapor/liquid contact method, such as packing, trays, or hybrid combinations may be utilized. The amine absorption system can be used for systems ranging from small scales such as biogas applications, to applications in the oil, gas, and chemical industries with units several meters in diameter [9].

Newer amine structures are being introduced and studied for the potential increase in CO₂ absorption such as benzylamine (BZA). Eskandari et al. studied BZA within hollow fiber membrane contactors (HFMCs) [90]. This system was tested against the more common amines, such as MEA and DEA. It was concluded that BZA had an increased absorption flux, comparatively, in many operating parameter variations, including amine concentration, sorbate partial pressure, phase velocities, temperature, and wettability. In addition to this study, BZA was utilized as a promoter in solutions of methyldiethanolamine (MDEA) and potassium carbonate (K₂CO₃), resulting in an increased absorption flux significantly [90].

In addition to amine solutions, other aqueous alkaline salts, such as calcium, potassium, and sodium hydroxides, can make a solvent that reacts chemically with CO₂ Sodium hydroxide has a higher absorption capacity for CO₂ compared to solvents such as monoethanolamine. For example, the theoretical amount of monoethanolamine required to capture 1 ton of CO₂ is 1.39 tons, while sodium hydroxide only demands 0.9 tons [91]. However, these systems are not commonly used to absorb CO₂ due to the difficulty of regenerating the solvents. This limits their use in acid gas removal to systems with low overall gas concentrations or small-scale temporary installations. The drawbacks of these methods include toxicity of the solvents to human beings and the environment, significant energy loads needed for regeneration of amines, initial cost of amine solvents, and amine losses due to evaporation [28]. The final content of methane in cleaned gas can reach up to 99% purity due to the high selectivity of amines for CO₂, with overall CH₄ losses as low as 0.1% [68]. As with water washing, the resulting gas must be dried before use in sensitive applications [72].

4.4. Pressure Swing Adsorption

PSA is a dry-contact method that separates gases based on the target compound’s molecular characteristics and the adsorbent material’s affinity. Utilizing the different interaction parameters of biogas compounds will allow for adsorption at different rates and concentrations on solid substrates. Equilibrium-based adsorbents have a higher affinity for holding CO₂ on their surface than CH_4, which results in an increased concentration of CH₄ in the vapor phase.

Neutral adsorbents have similar affinities for both gases and utilize pore size differences to change desorption rates, resulting in separation based on kinetics versus equilibrium [92,93]. Higher system pressure corresponds to high partial pressures, which drive high adsorption rates. Releasing this pressure causes desorption of gaseous compounds at different rates, allowing for physical separation. As an example, a methane stream containing 10% CO₂ was adsorbed on carbon molecular sieves (CMS) at 10 bar and 315 K. After approximately 15 min over 90% of the CO₂ had been adsorbed on the surface, but less than 5% of the CH₄ was adsorbed [94]. During blow-down, the methane was released first, followed by the desorption of CO₂. PSA systems are capable of producing high-purity gas streams but suffer from expensive capital cost requirements [13]. In addition, standard PSA configurations only recover 97% of the starting methane since it is lost to the waste stream when small amounts of CH₄ desorb with the CO₂ [95]. Adsorption of H₂S is irreversible on commonly used adsorbents, which reduces the usability of the system over time. To extend the life of the adsorbent and reduce operating costs, H₂S is separated from the raw gas prior to injection into the PSA system. Figure 5 presents a basic flow diagram of PSA systems in which treatment is divided into four overall steps (pressurization, adsorption, blow-down, and purge) performed in parallel to ensure continuous system operation. The main factors influencing PSA unit performance are injection pressure, purge pressure, type of adsorbent, cycle time, and interconnection of various columns [9,13,28,72,95,96]. PSA application advantages include compactness of the equipment, relatively low energy costs, a good safety record, and simplicity of operation.

Pressurization of clean biogas is performed between 4 and 10 atm during injection into a column containing adsorbate. The specific adsorbate used will depend on many factors, including concentrations of impurities in the biogas, desired treatment levels, cost restrictions, and end-use of the cleaned gas. Adsorption of clean biogas proceeds and temporarily traps gases such as CH₄, CO₂, N₂, O₂, and H₂. Equilibrium-based adsorbents are held under pressure until the system is close to equilibrium conditions. Impurities in the biogas will have adsorbed onto the surface material at higher concentrations than the gas phase, leading to an increase in gas phase methane purity. Kinetic-based adsorbents are held under pressure until the adsorbate is saturated with gas species. Methane does not adsorb with equilibrium-based adsorbents as strongly as carbon dioxide.

Blow-down begins by releasing the column pressure and allowing gases to exit. The methane, which is only weakly adsorbed, flows through the column and is collected at the top. The result from both equilibrium and kinetic adsorbents is an initial effluent gas very high in methane content, although some CO₂ is also released. As the system continues to depressurize, concentrations of CO₂ increase over time until its concentration in the effluent gas is higher than the level in the original biogas. To stop this from contaminating the first high-purity split, valves are used to divert flow when CO₂ concentrations begin to rise. This results in two separate gas collections from the original biogas stream: a high-purity CH₄ stream with some CO₂; and a high-concentration CO₂ stream with residual CH₄. The residual CH₄ gas stream contains significant amounts of methane, and though the concentration is low, it should be recycled back to the PSA entry. Further purification of one or both streams requires either multiple simultaneous adsorption columns or repeated treatment on the same column.

Purging involves flushing the column with nitrogen or other inert gases to remove any residual compounds still adsorbed after blow-down. Depending on the adsorbents utilized and the compounds collected, a heated gas stream may be needed to force desorption at the desired levels. A study by Ali Abd and Roslee Othman analyzed six separate adsorbents to compare differences in methane purity, and it was found that the carbon molecular sieve (CMS-3K) provided the highest biomethane recovery at 86.2% as well as the highest purity at 97.165% [97]. The selection of the adsorbent material plays a crucial role in the desired outcome of biogas upgrading and depends on the application and desired product.

4.5. Membrane Separation

Membrane technology is based on the selective permeability properties of a membrane, which allows the discriminatory separation of targeted gas components from a biogas matrix. A membrane is a dense filter that can separate the components in a gas or liquid at the molecular level. Membranes commonly used for upgrading biogas retain most of the methane while carbon dioxide and other trace, yet unwanted gases, penetrate through the membrane. There are two factors that affect the selection of membranes for the separation of gases: molecular size and solubility [98].

Polymer membranes can be classified as glassy, rubbery, or gel-like due to the increased freedom of movement that polymer chains can exhibit. In general, a higher freedom of movement means higher diffusivity of compounds but lower selectivity. For example, the permeability (low to high) of biogas components in a glassy polymer membrane is as follows: C₃H₈, CH₄, N₂, H₂S, CO₂, and H₂O. Preparing the membrane with a rubber polymer results in different permeability through the membrane: N₂, CH₄, CO₂, H₂S, C₃H₈, and H₂O. This trend can be seen in

Table 11. Permeability of Gases through Selected Membranes [100].

Membrane Type	Pure Gas CO2	Permeability [Barrier] CH4	Selectivity CO2/CH4
PDMS (Silicone Rubber)	464	136	3.4
Natural Rubber	13.7	2.9	4.7
Poly(4-methyl-1-pentane)	8.5	1.3	6.3
MatrimiⓇ (Polyimide)	6.5	0.19	34
P84 (Polyimide)	1.2	0.02	50
Kapton (Polyimide)	0.866	0.026	33.3

, which lists the permeability of CO₂ and CH₄ in various membranes. It can be observed that the water molecule is the smallest and most soluble; therefore, it is easily separated from methane by vitreous and polymeric gummy membranes, while carbon dioxide and hydrogen sulfide can be separated with glassy and gummy membranes [99].

In practice, carbon dioxide is better separated with vitreous membranes like cellulose acetate and polyimide, using size selectivity [101]. Hydrogen sulfide, which is a larger and more soluble compound than carbon dioxide, is best separated by gummy membranes, such as ether-amide co-polymers, using absorption selectivity [102,103]. Nitrogen can be separated from methane by vitreous membranes that use the difference in size or gummy membranes that use the differences in absorption strength, such as polyimide and perfluorinated polymers or rubber membranes like silicone rubber [100]. In both cases, the selectivity of these membranes is relatively small.

Finally, due to their solubility, propane and other hydrocarbons are best separated from methane using selective rubber absorption membranes like silicone rubber. The separation can be performed with dry processes (gas/gas separation) or wet (gas/liquid separation). The dry process uses specific polymer membrane materials capable of CO₂ and CH₄ separation made of cellulose acetate and polyimide [99]. The speed of permeability of the membranes depends on the absorption coefficients of the gases and material used for membrane synthesis. In turn, the absorption coefficient of a gas depends on the equilibrium concentration of gas in the membrane. By considering the diffusion and absorption coefficients of different gases, it can be observed over many polymer membranes that smaller molecules (such as CO₂) have a higher solubility and permeate more easily through the membrane compared to larger molecules like CH₄ [99]. As a result, CH₄ will be retained by the membrane while the CO₂ will permeate to the low-pressure side. Unfortunately, the membranes are rarely 100% selective, and some of the CH₄ (10–15%) is also transported to the low-pressure side [100].

A typical and simplified design of a membrane-based biogas enhancement unit is shown in Figure 6. In practice, raw biogas is initially cleaned by eliminating contaminants such as H₂S, water, VOCs, and other trace gases to avoid corrosion-related problems. Water is eliminated by condensation prior to compression, while H₂S is usually separated using activated carbon. Once water and H₂S have been removed, the biogas is compressed to 6–20 bars, achieving the driving force necessary for the membrane separation. The cleaned gas is then passed through a standard commercial separator to remove residual compressor oil and sent to membrane separation. Specific pressures for separation depend on operational requirements, including processing time, membrane types, purity requirements, and ambient temperature [28,68,72].

There are three very common membrane designs on the market. The first design shown in Figure 6 does not include internal biogas circulation, and therefore exhibits a lower energy consumption for compression. However, the loss of methane is higher without reprocessing of the off-gas. Application of this system requires the use of very selective membranes to minimize methane losses. Cost savings associated with reduced compression costs need to be carefully balanced against higher membrane costs. Methane in the residual gas could be used (e.g., co-generation in a boiler or CHP engine) to improve the overall efficiency of the system.

The second design in Figure 7 contains the air–liquid membrane Medal^TM and is used in most biogas upgrading operations. The permeate (gas passing through the membrane) from the first membrane stage is removed from the system, while permeate from the second stage is recirculated to minimize methane losses in off-gas. Reprocessing this second gas stream leads to increased energy consumption compared to Figure 6 but gives much better total methane recovery.

The third design, Figure 8, uses Evonik Sepuran^Ⓡ membranes. The retained product (the gas that does not pass through the membrane) during the first stage is purified in the second stage, as in design two, to obtain a gas product with a purity of more than 97% methane. Additionally, permeate from Stage 1 is introduced into a third stage to minimize the concentration of CH₄ in the residual gas as well as the gas circulating towards the compressor. The permeate that flows from the second and third stages is combined for recycling into the compressor. In a membrane unit, the majority of the remaining water after compression is separated from the RNG as part of a CO₂ stream. Therefore, a gas dryer is not commonly needed to further decrease the dew point.

The content of CH₄ in the upgraded biogas is commonly 95% but can reach over 98% under certain optimized conditions [72]. Wet membrane technology combines the advantages of membranes with absorption technologies. The difference between dry and humid processes is related to the hydrophobic properties of the micro-porous membranes used in the latter. Practically, the installed membrane separates the gas and liquid while gas molecules spread through the membrane and are absorbed by the counter-current liquid medium. The liquid solution can be regenerated at high temperature, while the CO₂ released is pure and can be used in other industrial applications. The main drawbacks of this technology are the high cost of membranes and their fragility. These membrane configurations provide biogas purification at an estimated cost of 0.3 kWh per cubic meter of RNG [46].

Further estimates predict the lifespan of membranes for biogas purification, in these configurations, vary between 5 and 10 years [72]. A study on multi-step membrane processes from Zito et al. found an increase in methane recovery due to higher selectivity as well as a saving in membrane area [104]. Analysis was made from 2 to 10 step paths with a significant reduction in membrane area between 2 and 5 steps. This method recovered a methane purity of 98% with a purer CO₂ permeate of 97.9%, reducing methane losses [104].

5. Conclusions

At present, RNG is emerging as a promising solution to reduce greenhouse gas emissions, enhance energy security, and support the transition to a sustainable future. This paper reviewed the current technologies for biogas conditioning and upgrading, discussing the methods used to transform raw biogas into high-quality RNG that meets pipeline standards and can be used interchangeably with conventional natural gas. The core technologies for biogas upgrading—scrubbing, sorption, pressure swing adsorption, and membrane separation—have made massive advancements in recent years. Despite this, several challenges remain. These processes alone are not at a level to produce the purity and cost metrics that will bring this alternative fuel to further readiness. The energy requirements of upgrading processes, the initial capital investment, and other operational costs are significant obstacles that need to be addressed to fully realize the potential of RNG. Addressing these challenges requires continued research and development to enhance the efficiency and cost-effectiveness of existing technologies.

Each technology discussed in this paper illuminates one or more avenues into generating biogas with methods for cleaning impurities, and these operations can be tailored to fit the requirements of various applications. Not every technology will fit in every instance of RNG production, therefore it is important to understand how they function so that they can be used in conjunction with new and already implemented systems. Furthermore, exploring the potential of emerging technologies, in Part II of this assessment, such as hybrid systems (i.e., that combine multiple upgrading methods), cryogenic separation, in situ methane enrichment, and the integration of renewable energy sources for process power, offer potential pathways to mitigate inherent issues of the current RNG landscape while opening new avenues forward in research and development. Other methods for upgrading (i.e., industrial lung, supersonic separation, chemical hydrogenation, hydrate formation, biological processes, etc.) should be expanded, and these advancements can significantly impact greater RNG adoption. Government policies and regulatory frameworks are essential in promoting the implementation and expansion of RNG technologies. Financial incentives like feed-in tariffs, renewable energy credits, and carbon pricing can provide the necessary economic incentives for investing in RNG. Additionally, aligning regulations across different regions can enhance the development of a global RNG market, encouraging international cooperation and the sharing of technological advancements.