Questions related to Catalyst Synthesis
For example, Cu/Zn/Al catalyst. 0.1M, NaOH soIution use for pH maintain. Desired pH achived without completing this NaOH solution. I wonder about rest of this solution is wastage?
I am looking for the oil for oil bath application.
My target temperature is 300 C so, I found this oil
PX0045-3 in the Sigma Aldrich, but I am not sure I can use it for oil bath application.
Can I use this? or if you have an available oil for the high temperature application, please let me know!
Silicon is can be used below 250 C I think.
Special ZSM-5 catalyst (synthesis and technical data) for converting C4+ olefines to light olefines.
I was wondering if anyone can share their experience regarding the calculation of required Salt and water(solvent) to prepare mixed metal oxide catalysts through the Co-precipitation method. For instance, CeZrO2 of 90:10 Ce/Zr molar ratio using Ce(NO3)3·6H2O and Zr(NO3)4·5H2O salts.
I typically start the calculations knowing the molar ratio of active components and the total weight of the catalyst
I suppose there are better approaches, for instance, calculating the required salts and solvents without having a specific weight of the end catalysts product in mind
I would like to make some modifications of my flavonoids for the sake to enhance the pharmaological activity.
Is it possible and practical ? And what kind of reagents will be more convenient?
Any suggestions or articles will be more valuable.
Please suggest a method to determine this practically. Please avoid mentioning the publications having the final results. The guidelines or procedure for measurement is required. Any related discussion or fruitful comments are warmly welcomed.
I would like to know which is a better approach,
Doing catalyst synthesis and characterization, performance testing of catalysts and then doing the kinetic and mechanistic study OR studying the reaction mechanistic via software tools like DFT before carrying out the catalyst synthesis and performance testing? I am asking the question in context with the steam reforming reaction over Ni-based bimetallic catalyst.
Yang Li, Yu X, Li H, et al. Detailed kinetic modeling of homogeneous H2S-CH4 oxidation under ultra rich condition for H-2 production[J]. Applied Energy, 2017, 208: 905–919.
In this document of preparing CS2 by thermal catalytic conversion of CH4 and H2S, the product will be forced air-cooled by quartz tube after coming out of the reactor to convert S from gaseous state to solid state. Will CS2 also change from gas to liquid? Can you continue to enter GC to detect the output?
I am trying to impregnate 10wt%Cu-10 wt%Fe on alumina pellets (1/8" in diameter, Alfa Aesar). The procedure I am following right now is mixing the alumina pellets and metal nitrate solutions (copper nitrate and iron (III) nitrate) with a weight of support to the volume of deionised water ratio of 1:5. The solution+support is mixed using a rotavapor for 3 hours and then the pellets are filtered out . Obviously, the filtration method will not ensure the required Cu-Fe loading on the alumina pellets. The problem is that when I mix and rotate the solution+pellets, the color of the solution changes from green to brown (I suspect some reaction of alumina with the metal nitrates). I tried to evaporating the metal precursor solution after impregnation using the rotavapor at 60°C of the water bath temperature (instead of the filtration step), but it led to the deposition of brown residue on the alumina pellets. What suggestions you will have to have an effective impregnation?
I am trying to make hard pellets of a NiO powder for Van Der Pauw conductivity measurements. Although I have a small steel iron pellet press (1.5cm diameter) and I go as high as 15,000.00 PSI, the pellets disintegrate as soon as I apply even a small pressure on them. I can't use a binder because it would change electronic conductivity, and I tried adding drops of ethanol or heating to 75 degrees °C but no luck. Any advice?
Could an electronegative support act as an electron sink to facilitate the oxidation of low-valence metal ions to higher valences?
If it could then Does electronegative support affect the catalyst efficiency in chemical water oxidation process?
In the case of water splitting the water oxidation (OER) is the bottleneck for the process and because of the harsh conditions of the WO reaction, molecular catalysts with high TOFs are not stable in the matrix and quickly decompose. On the other hand heterogeneous catalysts are more stable but they often do not have high TOF quantities. Now what is your opinion about the future catalyst type? Will the ideal catalysts fabricated by turning the molecular catalysts to heterogeneous catalysts ( by loading the molecular catalysts on the solid surfaces ) or it will be from the single atom heterogeneous catalyst type?
In your opinion, what’s the best strategy to approach the preparation of single atom site catalyst synthesis? Let’s suppose our substrate is zeolite or silica, and we want to impregnate Au/Ag on there edifice. Any suggestion will be appreciated.
Nitrooxy group (nitrate esters) is used in the preparation of vasodilators.
The use of silver nitrate to convert alkyl halides to nitrate esters is very common.
A. McKillop & M. E. Ford used mercury nitrate in organic media, but not repeated by someone else.
Can other nitrate salts be used to convert halides to nitrate esters?
Emami, Mut orgsynth.student
Typically xylene isomerization catalysts convert ethylbenzene (EB) to benzene. But for example, IFP's Oparsi plus catalyst convert EB to xylenes isomers.
It is a big help if anybody tells me what promoter can do this reaction.
I know hydrogenation metals like Pd can convert EB to naphthenes and acid sites of zeolite support are suitable for the conversion of naphthenes to xylene. But I think conventional catalysts have noble metals like Pd and they convert EB to benzene.
Good-day! Some researchers mention using Hydroquinone solution as a polymerization inhibitor in acrylic acid. How this solution can be prepared ?
What is the CAS number of the starting material involved. Thank you so much !!
Al incorporation into the SBA-15 structure can be done with limitations.
Upto what extent we can load Al into the SBA-15 structure, without creating an extra framework of alumina in the synthesized material?
As you know some MOFs are flexible and the way the flexible MOF behaves toward external stimuli such as temperature, pressure can affect their diameter (e.g., breathing) and many other physical properties.
How these changes can be related to the diffusion coefficient as it depends on catalyst diameter?
I need to know if it's possible to do the sabatier reaction to produce methane without catalyst, and the temperature that would require. The temperature must be higher (than with catalyst) due to the higher activation energy, right?
CO2 + 4H2 <-> CH4 + 2H2O
Recently, I was synthesized Zeolites Y with the mix of Ludox and NaAlO3. Is there any literature or good tip for me to modify Zeolites Y into Ultra-stable Zeolite Y? best regards.
I measured BET surface area and Electrochemically active surface area (EASA) of synthesized MnO2 nanomaterial. EASA was obtained by using Cyclic voltammetry at different scan rates (considering slope (Cdl) by plotting current (mA) vs. scan rates (mV/s)). the slope was obtained to be 0.0487 mF. Here, the carbon clothes (1 cm2) was used as a substrate for MnO2 nanomaterial, and considered Cs = 0.02 mF/cm2. EASA calculated from Cdl/Cs. The mass loading of the MnO2 on carbon cloth was about 0.00036 g/cm2.
1- First question is that "considering Cs=0.02 mF/cm2 as specific capacitance of an atomically smooth carbon meterials" is correct?
2- Second question is that : The BET surface area of MnO2 was obtained to be 17.5 m2/g. But EASA was obtained to be 0.0487 mF (slope), 2.435 cm2 (from Cdl/Cs), and 0.68 m2/g. Why there is high difference between obtained BET surface area (17.5 m2/g) and EASA (0.68 m2/g). Is there somethings wrong with the EASA result or it is correct?
I will be thankful if you could help me regarding two above questions.
I use a commercial Vulcan carbon as a support for multimetallic nanparticle catalyst. I notice in the EDS spectrum a peak of Si and another of S. I tend to think these are impurities in the carbon precusor itself and wonder what possible ways to clean the carbon from such impurities especially the sulphur which may poison the catalyst.
I am using Surfactants i.e CTAB, P-123 and F-127 in meso-structured materials synthesis. After synthesis i want to remove these surfacrtants by washing the materials with boiling EtOH for 6h. Is such kind of washing will be enough to remove surfactants because in my case calcination is not suitable for the as synthesized materials. So only washing will be enough to remove CTAB, P-123, F-127? kindly share your kind suggestions.
Kindly explain the major differences between the concept of catalyst inhibitors and catalyst poisons with suitable examples.
Thanks a lot.
I am getting dibenzylidene acetone with my product on doing separation by column. I do column at 1 to 2 % ethyl acetate /hexane. Any suggestion to remove dibenzylidene acetone
there are many parameters that effect to the formation of products in CO2 reduction such as catalyst, reductant.... Can you give me your opinion about this problem?. Thank you so much!
Dear Research Partners, How are you all so far? I have some questions for you please: Can a coffee husk based activated carbon be used for de colorization or de-pigmentation of herbal extracts in liquid form?....Is the process of preparing activated carbon from coffee husk an expensive process? Is there any paper or patent you know on the preparation of activated carbon from coffee husk for the same de pigmentation purpose? Hoping to hear from you ... Thanks very much
The reaction is CO methanation(i.e CO + 3H2 = CH4 + H2O). Since the input gases are CO2 and H2 at the surface of catalyst, the rate of former reaction is zero. As CO2 methanation and Reverse water-gas shift occurs along the radius of catalyst towards the center CO, H2O and CH4 are formed which will initiate the CO methanation reaction which was initially zero at the surface of the catalyst.
In hydrogenation process of phenylacetylene over Pd/C catalyst, when we calculate TON and TOF, we need to calculate the active site in the Pd/C catalyst.
Usually before hydrogenation phenylacetylene using a supported catalyst, catalyst purged with hydrogen at a certain time and temperature after that add phenylacetylene.
From the characterization analyses, it was found that the addition of the new functional group to the adsorbent decreased the rigidity of the material itself. However, the modified adsorbent are still giving the best performance during the regeneration and reusability study? Could anyone elaborate the findings, giving some theoretical evidence?
Siliceous zeolites or with low Si/Al are synthesized with easily, however, high Al-containing zeolite synthesis end up with mixed phases of amorphous silica-alumina with desired zeolite. Please suggest me some literature.
I want to convert phenol into cyclohexane via hydrodeoxygenation process. Most literatures suggest to use bifunctional HZSM-5 (acid catalyst) supported Pd catalyst (metal catalyst). However, I want to replace HZSM-5 with other material. I guess natural zeolite can be used to replace HZSM-5. However, I also have to consider the Bronsted acidity and porosity of natural zeolite. How can I tune those properties of natural zeolite? Reference will be very helpful.
Be able to synthesize M1 phase of MoVTeNb catalyst. Later, I'm planning to synthesis M1 phase of MoVTeNb catalyst supported on Silica.
I have no prior knowledge of synthesizing Hematite but now I need to make it.
Complete synthesis process of Hematite by any simple method is desired.
Hai, I am working with catalysis using metal nanoparticles (check my publication for details). Currently, I am studying the reduction of methyl orange using gold nanoparticles under continuous flow system. When studying the reduction kinetics, methyl orange is degrading to 90% at first but then the peak reappears after some time and the degradation is reduced to 50%. The catalyst is active. This I confirmed by washing the catalyst and reusing it for a fresh batch of methyl orange/BH solution. Can someone provide me with some insights to this problem?
Hi. I need to prepare metal supported alumina catalyst for my project. I found several methods in literature which can be applied including precipitation and impregnation methods as the most important ones but I do not know the exact difference between these two methods. Can anyone tell me the differences these two methods have in basic principles? Will the metal particles load in different places using these two methods?
Hi. I am synthesizing a Ag/TiO2-MCM-41 catalyst by using wet impregnation in a reflux system. I am using a AgNO3 solution as the Ag source, and I'm not sure if it is necessary to keep the solution protected from light during the synthesis, and/or also after it. Thanks in advance.
Note that, I have calcined my catalyst at 800 oC based on TGA result which became stable, with no weight loss after 800 oC.
The reaction temperature is 900 oC
We synthesized ZnO/ZrO2 catalyst in different content but we used same method which chemical precipitation. surprisingly all composites exhibites different morphology one of them is pencil-like other is star like etc. please help me is it possible and what is this reason?
What happen if I evaporate solvent at the same temperature which equal to rotary evaporator.
Is rotary evaporator under pressure reduction necessary?
What I have read from some publications is that gamma-alumina can be synthesized from aluminium hydroxide through Boehmite formation as an intermediate compound. Is there any direct method to synthesize this compound?
So we can conclude that the catalyst has basic sites that relate to Bronsted Basic and Lewis Basic sites, or acidic sites that relate to Bronsted Acidic and Lewis Acidic sites.
I have synthesized a catalyst and I am applying it in catalysing biomass pyrolysis reaction to obtain bio-oil. The catalyst shows best performance when it is used at a concentration of 7% giving the maximum amount of bio-oil. We do not see any further increase in the amount of bio-oil even after increasing the catalyst concentration beyond 7%. Why is it so?
The acid value for my west cooking oil is 18.4 .So can I use base catalyst for biodiesel?
or can I use catalyst with 2 function acid and base ?
I want to increase the crystallinity of a water-insoluble phosphate by use of an autoclave.
In literature the phosphate/water dispersion was kept at 180 °C for one week. Cooling rate was not mentioned.
I wonder if it makes sense to slowly cool down the autoclave or if holding at high temperature is the important step.
I could find out by experiment, but that will take a long time, so any experience would be quite helpful.
From CO pulse titration, dispersion of Pt particles, volume of CO adsorbed, diameter of particles and metal surface area are found. I need the value to find the CO coverage on Pt/SBA-15.
Why when I increase the doping metal the TPD-NH3 show increasing in acidity then show me decrease at high consecration of the metal?
I am using Ce doped with activated carbon when I increas the consecration of Ce the acidity was increase then Show me decrease is there any explanation for this phenomena
After catalytic preparation of NVP through dehydration reaction, the product smells a bad odor. This also occurs for NMP production and the odor is like a dead fish odor! how to deodorize these products?
Thank you in advance for your help.
I am working on heterogeneous catalysis and i want to dope magnesium (Mg) on catalyst support can it be effective? if yes then can i use Magnesium hydroxide for wet impregnation method to get Mg ions on the catalyst support surface please guide me for the preparation of this catalyst.
In general, reaction of NiCl2.6H2O and dppp yield Ni(dppp)Cl2; whether NiCl2.6H2O can be replaced by anhydrous NiCl2 for the same reaction?
Any papers comparing activity, metal-support interactions and dispersion of the catalysts prepared by these varying methods?
there are many methods for synthesis of catalysts such as nitrate, co-precipitation, .... is the change of the synthesis method for an oxide affect and change it's band gap?
I have commercially available weakly acidic alumina provided by SIgma ALdrich. Can I use it instead of gamma alumina for catalyst loading?
I want to prepare metal oxide catalyst, which is CaO-ZnO/Al2O3.
So, which the best method for that; is it co-precipitation method or incipient wetness method? or you can suggest another method.
Thank you so much in advance.
Of course, colorless molecules are better choices for photocatalytic activity test, but I mean if we are still interested in using dyes because of simple, low-cost protocol for determining their concentration spectrophotometrically. As it is known, many dyes show hypo/bathochromically shifted absorption peaks after degradation test, possibly due to the presence of degradation products.
I wanna use Deposition Precipitation Method to load metal on the support. For example, I need 10%Metal loading on the support. Kindly guide me, in Deposition Precipitation Method, is it possible to have theoretical metal loading equal to actual metal loading?
I have to use FeCl3 as a catalyst for synthesis guanidine group from NH2 and CN group, but after this step I need to remove Fe from the reaction with HCl. Since my product is polar, I can not use aqueous HCl. also I tried with HCl 2M.Et2O, It is work but still I am losing a part my product and the yield is not good. Could you guide me to solve this problem? Thank you so much
The usual pH of the starting gel for the synthesis of phosphate-based materials such as aluminophosphates and SAPOs is slightly acidic to slightly alkaline (typically, starting pH = 4-8). Why this pH condition favors the synthesis of SAPO catalysts? And why is this condition different for aluminosilicate zeolites? I would be grateful if someone could explain it to me from the molecular point of view.