Evaluate a methane-conversion catalyst only within a defined reaction route and product target. A methane-conversion percentage by itself is not a ranking: steam reforming and dry reforming make syngas, oxidative coupling seeks C2 hydrocarbons, and direct-conversion routes may seek oxygenates such as methanol. For each candidate, normalize the feed, pressure, temperature, flow or space velocity, reactor configuration, and time on stream, then assess methane conversion together with product selectivity, yield, energy burden, and performance retention.
Start with the route and the product you actually need
“Methane conversion” describes the disappearance of methane from a reactor feed, not whether the process made the desired product efficiently. The first line of any comparison should therefore identify the reaction route and intended product.
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Steam reforming: syngas with a steam-dependent heat load
Steam reforming reacts methane with water to produce synthesis gas, principally hydrogen and carbon monoxide. The useful product description is not just methane conversion: report the hydrogen-to-carbon-monoxide ratio, carbon monoxide and hydrogen yields, residual steam or methane, and any downstream adjustment needed to reach the intended syngas composition.
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Dry reforming uses carbon dioxide as the oxidant and also produces syngas. It is endothermic, so a high reactor temperature can be an energy burden even when it improves conversion. The carbon-dioxide conversion must be reported alongside methane conversion because the two reactants can be consumed at different rates. Reviews of dry-reforming catalysts emphasize that useful conversion generally requires substantial heat input; temperature is therefore a process condition to account for, not a standalone score. See the assessments in Ranjekar and Yadav (2021) and “Catalyst design for dry reforming of methane” (2018).
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Partial oxidation and related syngas routes
Partial oxidation introduces oxygen and can reduce the external heat requirement, but oxygen concentration, co-feed ratio, pressure, and safety controls change the reaction balance. Compare a partial-oxidation catalyst only with other tests using a comparable oxygen-to-methane ratio and reactor configuration.
Oxidative coupling: C2 hydrocarbons, not syngas
Oxidative coupling of methane (OCM) aims to join methane-derived fragments into ethane and ethylene. The central metrics are methane conversion, C2 selectivity, and C2 yield. A catalyst can consume much of the methane while over-oxidizing it to carbon oxides, leaving a poor C2 yield.
Direct conversion to oxygenates
Direct-conversion approaches may target methanol or other oxygenates. Oxygenate selectivity, oxygenate yield, co-product formation, and product separation conditions become as important as methane conversion. A high conversion that produces mostly unwanted oxygenates or carbon oxides is not a successful catalyst for a methanol process.
Why methane conversion is difficult to interpret
Methane has a C–H bond dissociation energy of about 434 kJ/mol, a figure discussed by Cai and Hu in their 2019 review of methane and carbon-dioxide conversion (Energy Science & Engineering, first published 25 February 2019). Activating that bond often requires high temperature, a reactive oxidant, or a catalyst site that can stabilize reaction intermediates. The same conditions that activate methane can also promote secondary reactions, carbon deposition, sintering, or non-selective oxidation.
Consequently, a conversion value is meaningful only with its denominator and operating context. Record whether conversion is based on inlet and outlet methane concentrations, a carbon balance, or another method; state the analytical technique and balance closure when the study provides them. For a simple single-pass calculation, methane conversion is the fraction of inlet methane consumed, commonly expressed as a percentage. That percentage does not reveal residence time, product distribution, or how rapidly the catalyst is losing activity.
Normalize the test before comparing catalysts
Before deciding that one formulation is better, put every result on the same information grid. The following fields prevent most misleading comparisons.
| Dimension | What to record | Why it matters |
|---|---|---|
| Route and objective | Steam reforming, dry reforming, partial oxidation, OCM, or a direct oxygenate route; intended product | Conversion and selectivity are route-specific and cannot be ranked across different products. |
| Feed and conditions | CH4/oxidant ratio, diluent, impurities, pressure, temperature, total flow, and flow basis or space velocity | Residence time and reactant availability can change apparent conversion and deactivation. |
| Conversion | Methane conversion and, where relevant, co-reactant conversion such as CO2 conversion | A second reactant may be central to the material balance and process cost. |
| Product performance | Product selectivity and yield; H2/CO for syngas or C2 selectivity and yield for OCM | High methane conversion can coexist with poor desired-product yield. |
| Durability | Time on stream, conversion and selectivity drift, regeneration protocol, carbon or structural characterization, and poison exposure | Short initial activity is not evidence of long-term stability. |
| Practical burden | Operating temperature, heat duty, feed cleanup, oxidant handling, and documented pressure requirements | A high-performing catalyst may require more energy or impurity control than the process can afford. |
Use the same reactor type, catalyst mass basis, particle size range, flow convention, pressure, feed dilution, and analysis method whenever possible. If one paper reports gas hourly space velocity and another reports volumetric flow without catalyst volume or mass, label the comparison incomplete rather than treating the numbers as equivalent.
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What the published examples do—and do not—show
The reviewed literature contains useful reference points, but it does not establish a universal catalyst ranking. These examples come from different routes and study conditions.
| Study example | Route and objective | Feed and conditions reported | Conversion reported | Product performance | Durability information | Practical burden |
|---|---|---|---|---|---|---|
| 7% Ni–1% Au/Al2O3 | Steam reforming; syngas production | Specific feed ratio, pressure, flow basis, and test duration are not stated in the cited review summary | 84% methane conversion | Not stated in the cited summary; hydrogen and carbon-monoxide distribution must be obtained from the underlying study | Not stated in the cited summary | Steam-reforming heat and steam requirements are not quantified in the cited summary |
| 10% Ni/ZrOx–MnOx/SiO2 | Dry reforming; syngas from methane and carbon dioxide | 500 °C; other feed, pressure, flow, and duration details are not stated in the cited summary | 17.9% methane conversion and 23.1% carbon-dioxide conversion | Syngas composition and H2/CO ratio are not stated in the cited summary | Not stated in the cited summary | Dry reforming is endothermic; the 500 °C result is a condition in this study, not a universal optimum |
The 84% and 17.9% figures must not be read as a head-to-head result. They describe different reactions, feeds, and likely reactor conditions. The 10% nickel dry-reforming example also reports 23.1% CO2 conversion, which is essential context rather than an optional extra number. Both examples are summarized in Chen et al., “Catalytic Conversion of Methane at Low Temperatures: A Critical Review” (first published 11 October 2019; volume publication 2020).
Temperature: compare useful output per unit of heat, not the lowest number
A lower operating temperature can reduce furnace duty and materials stress, but it may also lower conversion, slow reaction rates, or shift products toward unwanted species. A higher temperature can improve methane activation while accelerating carbon formation, sintering, or methane cracking. Report the temperature together with conversion, selectivity, yield, feed composition, pressure, and space velocity.
Build a temperature-response curve
When data allow, test several temperatures after the catalyst reaches a defined steady state at each point. Hold feed composition, total flow, pressure, catalyst mass, and analysis method constant. Plot methane conversion and each major product selectivity against temperature; a single “best temperature” can hide a sharp selectivity loss or a durability penalty.
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Endothermic reforming can create temperature gradients between the furnace, reactor wall, gas phase, and catalyst bed. Record how temperature was measured and where the thermocouple was positioned. Apparent improvements caused by external heating or a different reactor geometry should not be attributed automatically to intrinsic catalyst activity.
Include the feed-cleanup and energy context
Steam generation, carbon-dioxide conditioning, oxygen production, preheating, and recycle compression can dominate the process energy balance. A catalyst that operates at a lower temperature but requires a purified feed or large oxidant excess may not reduce total energy use. Only claim an energy advantage when the study reports the relevant heat and separation requirements.
Conversion, selectivity, and yield must be read together
For a single desired product, yield is generally the fraction of inlet methane that appears as that product, while selectivity describes the product share among converted methane or carbon, depending on the study’s stated convention. Always reproduce the denominator used by the authors. Different conventions can make two apparently similar percentages non-comparable.
Syngas routes
For steam and dry reforming, record methane conversion, co-reactant conversion, hydrogen yield, carbon-monoxide yield, and the H2/CO ratio. A catalyst may give high methane conversion but an H2/CO ratio unsuitable for the downstream Fischer–Tropsch, methanol, or hydrogen process. Carbon dioxide conversion in dry reforming also affects the net carbon balance and recycle load.
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OCM routes
OCM requires a three-part result: methane conversion, C2 selectivity, and C2 yield. Cai and Hu’s literature review reports maximum conventional oxygen-based OCM C2 yields of 16–27% with selectivity of 72–82%. The same review reports a maximum C2 yield of up to 6% for CO2-OCM, with comparable selectivity. These are literature summary ranges, not guarantees for a new catalyst or a single formulation. They should not be assigned to an individual catalyst without checking the underlying paper.
Direct oxygenate routes
For methanol or another oxygenate, list oxygenate selectivity and yield separately from methane conversion, then identify water formation, over-oxidation products, and the product-recovery step. A catalyst that produces a trace amount of methanol at high selectivity may have a different commercial implication from one with high conversion but substantial carbon-oxide formation.
Durability is a measured trajectory, not a label
Define durability as performance retained over a specified time under specified feed and operating conditions. A credible durability result shows conversion and selectivity versus time on stream, identifies temperature and flow throughout the run, and explains any regeneration or restart procedure.
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Track the right signals
- Plot methane conversion and every critical product selectivity from the beginning to the end of the run.
- Record co-reactant conversion where it controls the process balance.
- State whether the catalyst was stabilized before data collection and how long stabilization lasted.
- Report carbon deposition measurements, such as post-run carbon quantity or microscopy, when available.
- Check for active-phase sintering, support transformation, oxidation-state changes, and loss of surface area.
- Describe regeneration conditions separately from normal operation; recovered activity after burning off carbon is not the same as uninterrupted stability.
Why nickel needs special scrutiny
Nickel is widely used for reforming because it combines high activity with relatively low cost. It is also vulnerable to carbon-related deactivation, especially under dry-reforming conditions. Cai and Hu summarize the issue directly: “The majority of catalysts are based on Ni due to its high activity and low cost, whereas these catalysts usually undergo deactivation processes mainly due to carbon deposition.” Alloying and support or promoter strategies are active research approaches for limiting carbon formation and improving structural stability. The review of alloying effects in steam and dry reforming by Torimoto and Sekine provides context at Catalysis Science & Technology (first published 15 March 2022).
Distinguish deactivation mechanisms
Carbon deposition can block active sites or plug pores; sintering can reduce the number of exposed active ensembles; poisoning can bind irreversibly to those sites. A falling conversion accompanied by increasing carbon suggests a different intervention from a fall associated with metal-particle growth. Do not call a catalyst “stable” when the study reports only one initial activity point.
Test realistic impurities
Biogas-derived methane can contain hydrogen sulfide. Sulfur resistance is therefore a catalyst-design concern, not a minor analytical detail. State the H2S concentration, exposure time, whether the poison was removed, and whether activity recovered after regeneration. Cai and Hu discuss impurity concerns for methane-conversion feeds at their 2019 review.
Independent reader supportYour contribution helps us test, update, and keep practical guides available for everyone.A step-by-step evaluation workflow
- Write the process specification. Name the feed source, target product, acceptable impurity level, pressure range, throughput basis, and whether single-pass or recycled operation is intended.
- Select route-specific success metrics. Use syngas composition for reforming, C2 selectivity and yield for OCM, or oxygenate yield and selectivity for a direct-conversion route.
- Create a condition sheet. Capture methane and oxidant composition, diluents, pressure, temperature profile, catalyst mass and particle size, flow or space velocity, reactor dimensions, and analytical method.
- Check material balances. Compare inlet and outlet carbon, hydrogen, oxygen, and—when relevant—carbon dioxide. Investigate unexplained balance gaps before accepting a high conversion claim.
- Measure a temperature series. Use identical feed and flow settings at each temperature and wait for a defined steady state. Record both activity and selectivity.
- Run time-on-stream tests. Predefine the duration, sampling interval, acceptable conversion drift, and selectivity drift. Include a post-run catalyst characterization plan.
- Challenge the catalyst. Introduce relevant impurities such as H2S at a documented concentration when the intended feed contains them. Test start-up, shutdown, and any planned regeneration separately.
- Compare on a like-for-like basis. Prefer tests with the same route, feed, pressure, reactor configuration, flow basis, catalyst loading, and duration. Mark every remaining difference in the comparison table.
- Translate laboratory results into process burden. Estimate heating, steam, oxygen or carbon-dioxide conditioning, recycle, separation, and replacement costs only from reported or independently verified data; do not infer them from conversion alone.
- Make a qualified decision. Select the formulation that meets the product and lifetime requirement at an acceptable energy and impurity burden, not the one with the largest isolated conversion percentage.
Common comparison errors and how to correct them
Ranking across different reaction routes
Comparing an 84% steam-reforming conversion with a 17.9% dry-reforming conversion as though they were competing grades is invalid. Correct the error by grouping results by route and product, then comparing only normalized studies within a group.
Reporting temperature without residence time
Two reactors at the same temperature can have different contact times because of catalyst volume, flow rate, dilution, or pressure. Always report space velocity or enough information to calculate it.
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In multi-product chemistry, conversion can rise while desired-product yield falls. Add selectivity and yield beside conversion and identify the denominator.
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Calling a short run durable
An initial steady value does not establish lifetime. Ask for time-on-stream data, drift, regeneration history, and post-test characterization.
Ignoring analytical and balance uncertainty
Small conversion differences may be less significant than gas-analysis uncertainty or an incomplete carbon balance. Require calibration details, replicate measurements, and balance closure where the decision depends on a narrow performance margin.
Assuming a promoter solves every failure mode
Alloying or a modified support may suppress carbon in one feed while changing selectivity, reducibility, or sulfur response in another. Judge the modification by the complete condition sheet and durability trajectory, not by its composition alone.
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A concise claim should contain the route, product, conditions, performance, and duration in one sentence. For example: “Under the reported dry-reforming feed at 500 °C, formulation X reached Y% methane conversion and Z% carbon-dioxide conversion; syngas composition and long-term drift were not reported.” This wording tells a reader exactly what is known and prevents a laboratory value from becoming an unsupported commercial benchmark.
When evidence comes from a review rather than a controlled comparison, identify it as a literature example. The available reviews do not define one universal durability protocol or a current commercial benchmark covering every methane-conversion route. A credible evaluation therefore preserves the boundaries of each experiment instead of forcing unlike results into a single league table.
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