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Steam Reforming - Science topic
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A typical reforming section in a large-scale Haber-Bosch process (Figure 1) comprises two reactors. A mixture of methane (CH4) and steam (H2O) is fed into a primary reformer to produce syngas via steam reforming (SMR). The gas product is then fed into a secondary reformer where it is mixed with air before going through a second steam reforming process. The air introduced into the secondary reformer (ATR) provides not only a suitable amount of nitrogen for ammonia synthesis but also some oxygen to exothermally oxidize part of the feed stream, thus decreasing the energy requirements of the steam reforming section of this reformer.
An alternative reforming process is proposed in Figure 2. Unlike the conventional approach, the first reactor is used to catalytically oxidize the methane feedstock at low temperatures using a sub-stoichiometric amount of air (CPOX) and consuming 100% of the oxygen. In the secondary reformer, a steam reforming process is performed to increase the amount of H2 produced.
Based on thermodynamic grounds, these two processes are expected to produce the same reformate; however, the use of low-temperature catalytic partial oxidation in the first reformer may lead to smaller reactor sizes as well as the reduction of potential fire hazards as flammable mixtures will not be exposed to high temperatures.
Is there any other foreseeable advantage of the alternative reforming approach?

I need a PET + Solvent mixture to feed it to a fixed bed reactor for steam reforming.
I would like your expertise and guidance regarding a challenging Computational Fluid Dynamics (CFD) problem I currently have. The project involves species transport in Ansys Fluent, focusing on simulating a steam methane reforming process.
The issue I am encountering pertains to the Chemkin files that I have uploaded into the Ansys Fluent software. Unfortunately, I am encountering persistent errors, and it seems the software is not properly considering the uploaded Chemkin files. I have thoroughly reviewed the inputs, but the problem persists. Despite my best efforts, I have been unable to resolve this issue.
Furthermore, in this simulation, a key aspect involves maintaining a wall at an elevated temperature of 2000 degrees Celsius. The objective is to facilitate heat transfer to the methane and steam feed mixture to initiate the steam methane reforming reaction.
Regrettably, I have observed that the heat is not effectively transferring to the feed mixture, resulting in the absence of the desired chemical reaction. This poses a significant setback to the project, as the core objective is to study the reaction kinetics and product distribution in this specific environment.
Your support in this matter would be immensely important to my research progress.
Thank you in advance for considering my request. I am eager to learn from your expertise and am open to any suggestions or instructions you may have.
Sincerely,
Sudeep N S
Hi all,
To set things clearly: I am a PhD student working on the process implications of electryfing the ammonia production by replacing conventional SMR with Water Electrolysis. A part of my preliminary work is to assess the difference in theoretical minimum energy consumption. To do so, I have calculated a first approximation by summing up the reactions (SMR, Water gas shift, Haber-Bosch,...) and calculating the enthalpy of the resulting "total" reaction. I have done this for the "Water Electrolysis + Haber-Bosch scenario" and validated the minimum with values from the literature.
However, for the conventional "SMR + Haber-Bosch scenario", values from the literature are different. To be more specific, here is the energy minimum calculated in the following conference paper:
(...) the theoretical minimum of energy consumption for the process itself (represented by LHV of methane) is 22.2 GJ/t NH3 (...)
Conference Paper 2. Kirova-Yordanova Z, Energy Integration and Cogeneration i...
So here is my question: Why use the LHV of methane (instead the enthalpy of reactions) to calculate the energy minimum ? I feel like this is incorrect as I do not take into account the synthesis of methane.
Thanks in advance for any answers,
Antoine
How to solve x, y, and z on Matlab or excel?
I have tried many times but all times get negative values for x and y (using equation 7-13). If you have any idea or MATLAB code to solve these equations, then please let me know.
fuel composition is CH4=97%; CO2=1.5%; N2=1.5%
Air Composition is O2 =32%; N2=79%.
Dear all,
I have planned to do kinetic studies of Dry (CO2) Reforming of Methane experimentally and theoretically for my developed Ni/CeX-Zr1-XO2. I went through some published papers, and they have shown the final kinetics equation based on different kinetic models, which is very difficult for me to understand and perform for my experiment. May I get help from any one of you in this regard or anybody willing to research collaboration with me in these regard?
Thank you in advance for your kind consideration and any valuable supports!
I've been tasked to design a PSA to produce 99.9% pure hydrogen via steam reforming. The inlet feed into the PSA consists of hydrogen, carbon monoxide, carbon dioxide and nitrogen. Can anyone please help me on how i would go about designing a PSA.
Thanks
I want to convert flow rate unit Cubic centimeters per minute to KPa. What would be the conversion for 60 SCCM of H2 in KPa.?
Thank you
In general, syngas from gasification or steam reforming, etc, can generate H2, CO, CO2, and/or CH4.
However, many papers compared only H2/CO.
Therefore, I want to know the reason why H2/CO2 is not used.
Is there a characteristic or importance of H2/CO?
Thank you so much!
Hi,
We all know that the catalysts provide an alternative (lower energy) pathway for a reaction to occur. For example, the gas reforming reactions (say steam reforming of methane) are highly endothermic and the use of catalysts economize the reaction. But how does all this actually take place? I just want an explanation that can help me realize this phenomenon.
In absence of catalyst the gas molecules can collide at very high temperatures (>1000 oC) to form the products, but in presence of catalyst the same reaction is taking place at 600 oC. How this happens?
Dear all ,
I want to use Rapidox 7100 Multigas Analyser to analyze the reactants and products of the dry CH4 reforming reaction . But the instrument is not responding, I am working at a total flow rate of 60ml/min( CO2:CH4:N2, 5:5 :50 ml/min), can there be a flow rate problem? If not, if a colleague works with the same instrument, please clarify especially the connection of the gas inlet.
thanks
Hydrogen plant has a turndown ratio of 40% and after reaching this stage, extra H2 is being produced than the required. So it is being vented.
Is there any way to stop this venting and use it as a fuel somewhere like boilers by mixing it with current fuel-natural gas?
Im currently designing an adiabatic pre reformer? I cant find any reference regarding the rate of reactions and also kinetics for the pre reformer design.
In order to simulate one process of SOFC with internal methane reforming, in the Reformer some reaction take a place like: CO+H2O = CO2+H2, C+CO2 = 2 CO, C+H2O = CO+H2, CO+3 H2 = CH4+H2O, C+2 H2 = CH4 and each of this reactions have an equilibrium temperature, which tells me the direction of the reaction.
I need to know, what is the relationship between the equilibrium temperature and the mass flux of the fuel, which enter the reformer. In my case, I use the exhaust gases generated in the Anode to supply the Reformer with energy after mixing with the natural gas. It will be very helpful if there is a Formel or scientific paper which gives the relationship between the equilibrium temperature in the reformer and the mass flux of the fuel entering the reformer.
The most current research focused on hydrogen production, storage, and use, considers the following distribution of commercial hydrogen production technologies as the standard for the global hydrogen production matrix:
48% methane steam reforming
30% oil/naphtha reforming
18% coal gasification
4% water electrolysis
However, this information is more than 30 years old and comes from the statistics of the world hydrogen production from 1988 presented by (Roesler, R. and Zittel, W. 1994). I have tried, unsuccessfully, to update these numbers to today's reality.
Finally, I would like to know your opinion on this topic. Do you consider it to be worthwhile to update this information, and if so, do you have any information on where these data could be found?
Attached you may find a paper by Gaudernack from 1998 where Roesler is cited.
In ethanol steam reforming , how to calculate the heat of the different unit operation in aspen plus, provided with different NIO/ethanol molar ratios and the carbon yield?
Hydrogen is an eco-friendly fuel in part because when it burns, the result is water. However, there are no convenient suitable natural sources for pure hydrogen. Today, hydrogen is obtained by steam reforming (or "cracking") hydrocarbons, such as natural gas. This process, though, requires fossil fuels and creates carbon byproducts, which makes it less suited for sustainable production.
Steam electrolysis, by contrast, needs only water and electricity to split water molecules, thereby generating hydrogen and oxygen. The electricity can come from any source, including wind, solar, nuclear and other emission-free sources. Being able to do electrolysis efficiently at as low a temperature as possible minimizes the energy needed.
I have both the mass and energy balances from Aspen plus; I was thinking of specifying the residence time and then calculating the volume from that but I can't find the typical values for residence time in industrial reformers.
hi anybody, what is circular variable dependency in comsol and how can i overcome it? im working on modeling and simulating of methane steam reforming in membrane reactor and i use a kinetic that its expressions are circularly depended to each other , this is a 2-D steady model. i wonder if you help me thanks
I'm designing a primary reformer(tubular top fired methane steam reformer) for a ammonia production plant. I have issue in deciding the mounting method of tubes and standard gaps between tubes and furnace wall. It will be great if you can help me with resources
How can we overcome the sintering of nanoparticles, happens at the surface, in the synthesis of Pd-based intermetallic compound as a catalyst on Methanol Steam Reforming process? In face, the most challenging part of synthesizing an intermetallic compound is the annealing section where the mixture should go through a comparably moderate heating so that we could reach the ordered compound known as intermetallic, not an unordered alloy (solid solution).
You may want to consider ZnPd (intermetallic) as the case study. Recommending some applicable papers is profoundly appreciated.
Thank you in advance.
Main Liquid products are Glycerol water acetic acid acrolein acetone methanol and ethanol.
Is there any way to avoid ion exchange column for such components detection ?
I have run preliminary reaction for Methane dry reforming at 1:1 ratio of CH4:CO2 at 500 oC and 600 oC, the conversion was as following:
500 oC CH4= 14% CO2= 20%
600 oC CH4= 36% CO2= 46%.
For the Design of Experiments (DOE) Shall I start from 500 oC.
Thank you
In oxidation growth processes, parabolic kinetics occurs when the mass gain or oxide growth on a sample is proportional to the square root of time.
In my case I only have experimental data correlating the average thickness of the oxide growth with square root of time and as a result, I am trying to convert it from [m2/s] to [g2cm-4s-1] in order to compare with other studies wherein their focus was mass gain.
Thank you
I am running dry reforming on Ni-based catalyst. During the reaction Huge amount of carbon formed below the quarts, However, this coke formation doesn't deactivate the catalyst. If I want to quantify the carbon shall I consider the carbon on the catalyst or both (below the quartz wool. I could easily separate the layer of carbon formed below the catalyst bed.
Thank you
Carbon formed on the catalyst used for dry reforming. From the attached SEM image can I know the type of carbon. Thank you
I have a Two Stage Coal Gasifier. The Oxidation and Reduction zones are in the Annular Boiler. We would like to measure the bed temperature at difference heights of the annular boiler. we have concerns about drilling through the annular boiler plates as that might compromise the strength on the plates. What other options can I consider as means of measuring the temperatures at different zones.
Regards
Lawrence
What would be the most accurate method to calculate the LHV of a fuel (heterogeneity of IW and MSW) in a incineration power plant. If hydrocarbon contents, and other relevant elements are unknown (question of a real-life practice)
For instance, could the property of a steam, boiler efficiency, etc. be used in a reversed calculation. And how could it be done?
Does anybody have experience with the online detection of carbon formation in a reforming process? We would like to determine if any carbon is formed during operation. One of the ideas is to use mass balance over the reactor. Does anybody have experience with this, may it be accurate enough?
Can anybody reccomend literature on this? So far all literature I know discusses the analysis of the catalyst itself outside the reactor via XRD or similar techniques.
Actually, I am working on steam reforming of hydrocarbons field. As we know, lots of carbon generate over catalyst surface during reaction time. Before the reaction, I used binder such as bentonite to make catalyst extrude. So, the bentonite surface area will include with actual catalyst surface area. I want to know that how can I know the surface area of the catalyst after reaction.
Considering an initial mixture of steam and methane with steam to carbon ratio of 2, based on the methane steam reforming and water gas shift reactions, how can I compute the mixture composition after 10% pre-reforming, where the shift reaction is at equilibrium?
Actually, I know the procedure for determining the mole fractions at equilibrium considering the two reactions, but I don't understand the role of the word ''10%'' pre-reforming in the problem !!
Thanks in advance.
it is possible to minimize coke formation by using non acidic catalyst
We performed a Raman-TPO (up to 600 ºC) experiment with a spent catalyst, deactivated by coke in a bio-oil steam reforming process, and the Raman spectra were recorded during the combustion process. However, we see an increasing G band width and D/G ratio and a decrease in G band position during the process, which is not in line with Robertson ('Diamond-like amorphous carbon', 2002). Do our results have any sense? I will fully appreciate any provided help, thanks a lot.
I would appreciate it if there are any appropriate scientific references paper in which the authors are working on a small scale anaerobic digester combined with steam reforming followed by Fischer Tropsch reactor.
A set of experiment for steam reforming were carried out using NiO at 800C varying the time, after reforming experiment the NiO reduced to Ni with adsorbed C.
Hence, I want to evaluate the amount of Carbon deposited in the NiO catalyst.
The goal of gasification/ steam reformation is the complete transformation of feedstock carbon content into gases (syngas) with high heating values. The Boudouard reaction is a very important process to achieve this goal by transforming solid residue carbon content and non-combustible carbon dioxide into a usable gas - carbon monoxide and increasing the heating value of the produced syngas.
i working for methane steam reforming simulation.
i want calculate the heat transfer coefficient in catalyst bed.
and i want compare to some one's coefficient.
Currently I am studying 'Methane Steam Limitations and Reforming II. Diffusional Reactor Simulation'
What is the optimum steam to carbon ratio for steam reforming of naptha C11H24, and how do you get the balance in the desulfurizer for removing 22 ppm by weight of sulphur contained in the liquid naptha? I used a ratio of 6.5 and my balancing gets off tune in the primary reformer.
The pipe is horizontal and is rotating about its central axis. The pipe resistivity is very low (range 10^8 ohms). A very high current will be required in general to generate heat fluxes in the range of 2kw at least.
Is it feasible to go ahead with this kind of a set up.
Conventional heaters will restrict the access to various sections of the pipe and I would like to access all the parts of the outer pipe surface in order to measure local temperatures.
The flow rate will be in laminar range and the pipe is partially filled with water.