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65 results for “Hydrogen production”
Effect of ion-specific water structures at metal surfaces on hydrogen production
<p>Here lies the tabulated data used to create the Figures for the Nature Communications manuscript NCOMMS-23-54843B titled "Effect of ion-specific water structures at metal surfaces on hydrogen production".</p>
Hydrogen production in microchannel reactors by process intensification
<p><strong>Hydrogen production in microchannel reactors by process intensification</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>In reactions under normal laboratory conditions, matter is neither created nor destroyed, and elements are not transformed into other elements. Therefore, equations depicting reactions must be balanced; that is, the same number of atoms of each kind must appear on opposite sides of the equation. The balanced equation for the iron-sulfur reaction shows that one iron atom can react with one sulfur atom to give one formula unit of iron sulfide. Chemists ordinarily work with weighable quantities of elements and compounds. For example, in the iron-sulfur equation the symbol Fe represents 55.845 grams of iron, S represents 32.066 grams of sulfur, and FeS represents 87.911 grams of iron sulfide. Because matter is not created or destroyed in a chemical reaction, the total mass of reactants is the same as the total mass of products. If some other amount of iron is used, say, one-tenth as much (5.585 grams), only one-tenth as much sulfur can be consumed (3.207 grams), and only one-tenth as much iron sulfide is produced (8.791 grams). If 32.066 grams of sulfur were initially present with 5.585 grams of iron, then 28.859 grams of sulfur would be left over when the reaction was complete. The ratio of reactants and products in a chemical reaction is called chemical stoichiometry. Stoichiometry depends on the fact that matter is conserved in chemical processes, and calculations giving mass relationships are based on the concept of the mole. One mole of any element or compound contains the same number of atoms or molecules, respectively, as one mole of any other element or compound. Energy plays a key role in chemical processes. According to the modern view of chemical reactions, bonds between atoms in the reactants must be broken, and the atoms or pieces of molecules are reassembled into products by forming new bonds. Energy is absorbed to break bonds, and energy is evolved as bonds are made. In some reactions the energy required to break bonds is larger than the energy evolved on making new bonds, and the net result is the absorption of energy. Such a reaction is said to be endothermic if the energy is in the form of heat. The opposite of endothermic is exothermic; in an exothermic reaction, energy as heat is evolved. The more general terms exoergic (energy evolved) and endoergic (energy required) are used when forms of energy other than heat are involved. A great many common reactions are exothermic. The formation of compounds from the constituent elements is almost always exothermic. Formation of water from molecular hydrogen and oxygen and the formation of a metal oxide such as calcium oxide from calcium metal and oxygen gas are examples. Among widely recognizable exothermic reactions is the combustion of fuels. Not all reactions are exothermic (or exoergic). A few compounds, such as nitric oxide and hydrazine, require energy input when they are formed from the elements. The decomposition of limestone to make lime is also an endothermic process; it is necessary to heat limestone to a high temperature for this reaction to occur. The decomposition of water into its elements by the process of electrolysis is another endoergic process. Electrical energy is used rather than heat energy to carry out this reaction. Generally, evolution of heat in a reaction favours the conversion of reactants to products. However, entropy is important in determining the favourability of a reaction. Entropy is a measure of the number of ways in which energy can be distributed in any system. Entropy accounts for the fact that not all energy available in a process can be manipulated to do work. A chemical reaction will favour the formation of products if the sum of the changes in entropy for the reaction system and its surroundings is positive. An example is burning methane. Methane has a low entropy. When methane burns, it produces ash as well as the high-entropy substances carbon dioxide gas and water vapour. The entropy of the reacting system increases during combustion. Just as important, the heat energy transferred by the combustion to its surroundings increases the entropy in the surroundings. The total of entropy changes for the substances in the reaction and the surroundings is positive, and the reaction is product-favoured.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 14.1419</p> <p>0.00025 14.1567</p> <p>0.0005 14.1167</p> <p>0.00075 13.9733</p> <p>0.001 13.7817</p> <p>0.00125 13.5773</p> <p>0.0015 13.3834</p> <p>0.00175 13.2078</p> <p>0.002 13.0467</p> <p>0.00225 12.8884</p> <p>0.0025 12.7233</p> <p>0.00275 12.549</p> <p>0.003 12.3695</p> <p>0.00325 12.193</p> <p>0.0035 12.0273</p> <p>0.00375 11.8751</p> <p>0.004 11.7343</p> <p>0.00425 11.5992</p> <p>0.0045 11.4645</p> <p>0.00475 11.3284</p> <p>0.005 11.1919</p> <p>0.00525 11.0595</p> <p>0.0055 10.9352</p> <p>0.00575 10.8199</p> <p>0.006 10.7123</p> <p>0.00625 10.6092</p> <p>0.0065 10.5073</p> <p>0.00675 10.4052</p> <p>0.007 10.3035</p> <p>0.00725 10.2049</p> <p>0.0075 10.1114</p> <p>0.00775 10.0239</p> <p>0.008 9.94127</p> <p>0.00825 9.86107</p> <p>0.0085 9.78104</p> <p>0.00875 9.70044</p> <p>0.009 9.61993</p> <p>0.00925 9.54112</p> <p>0.0095 9.46564</p> <p>0.00975 9.39386</p> <p>0.01 9.32487</p> <p>0.01025 9.25686</p> <p>0.0105 9.1882</p> <p>0.01075 9.11849</p> <p>0.011 9.04832</p> <p>0.01125 8.97901</p> <p>0.0115 8.91153</p> <p>0.01175 8.84618</p> <p>0.012 8.78242</p> <p>0.01225 8.71871</p> <p>0.0125 8.65378</p> <p>0.01275 8.58747</p> <p>0.013 8.5204</p> <p>0.01325 8.45357</p> <p>0.0135 8.38782</p> <p>0.01375 8.3233</p> <p>0.014 8.25958</p> <p>0.01425 8.19529</p> <p>0.0145 8.12949</p> <p>0.01475 8.06216</p> <p>0.015 7.99387</p> <p>0.01525 7.92554</p> <p>0.0155 7.8578</p> <p>0.01575 7.79065</p> <p>0.016 7.72352</p> <p>0.01625 7.65551</p> <p>0.0165 7.58549</p> <p>0.01675 7.51373</p> <p>0.017 7.44118</p> <p>0.01725 7.36834</p> <p>0.0175 7.29539</p> <p>0.01775 7.22242</p> <p>0.018 7.1493</p> <p>0.01825 7.07505</p> <p>0.0185 6.999</p> <p>0.01875 6.92134</p> <p>0.019 6.84253</p> <p>0.01925 6.76289</p> <p>0.0195 6.683</p> <p>0.01975 6.60311</p> <p>0.02 6.5227</p> <p>0.02025 6.44094</p> <p>0.0205 6.35734</p> <p>0.02075 6.27217</p> <p>0.021 6.18588</p> <p>0.02125 6.09878</p> <p>0.0215 6.01121</p> <p>0.02175 5.92324</p> <p>0.022 5.8344</p> <p>0.02225 5.74426</p> <p>0.0225 5.65277</p> <p>0.02275 5.56008</p> <p>0.023 5.4663</p> <p>0.02325 5.37179</p> <p>0.0235 5.27682</p> <p>0.02375 5.18138</p> <p>0.024 5.08523</p> <p>0.02425 4.988</p> <p>0.0245 4.88969</p> <p>0.02475 4.79046</p> <p>0.025 4.69054</p> <p>0.02525 4.59019</p> <p>0.0255 4.48973</p> <p>0.02575 4.38924</p> <p>0.026 4.28848</p> <p>0.02625 4.18738</p> <p>0.0265 4.08615</p> <p>0.02675 3.98492</p> <p>0.027 3.88396</p> <p>0.02725 3.78374</p> <p>0.0275 3.68429</p> <p>0.02775 3.58597</p> <p>0.028 3.48836</p> <p>0.02825 3.38251</p> <p>0.0285 3.28598</p> <p>0.02875 3.18522</p> <p>0.029 3.08588</p> <p>0.02925 2.98803</p> <p>0.0295 2.89361</p> <p>0.02975 2.794388</p> <p>0.03 2.694288</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Catalytic reaction processes using microchannel technology for hydrogen production by steam reforming
<p><strong>Catalytic reaction processes using microchannel technology for hydrogen production by steam reforming</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>Two competing proposals have been made concerning the mechanism of catalytic reactions at surfaces, and it has not been possible to choose between them. Originally, Irving Langmuir, an American physical chemist, proposed chemisorption of both reacting species at the surface, followed by interaction between adjacent species and evaporation of the products. An alternative proposal involves interaction between an impinging molecule and species already adsorbed on the surface. Subsequent developments have suggested various modes of attachment of the adsorbed and adsorbing species. A major advance in the science of surface catalysis was the development of a method for determining the surface area of catalysts (and other materials) by measuring the multimolecular adsorption of nitrogen at liquid nitrogen temperatures or the adsorption of other gases close to their boiling points. It then became possible to calculate a quantity that represents the volume of gas necessary to form a monolayer on the accessible surface; furthermore, the area of the surface can be determined from the known dimensions of the adsorbed molecules. It has also been found possible to titrate (measure quantitatively) the area of surfaces by chemisorption of gases. Since heterogeneously catalyzed reactions occur on the surface of the catalyst, the rates of such reactions are proportional to the accessible surface area of the catalyst. Active catalysts are thus usually highly porous solids with total surface areas as high as several hundred square metres per gram. When measurements of surface areas became possible, it was seen at once that many constituents present in minor quantities in the main catalyst material, known as promoters, could act by extending the effective surface area of the catalyst. It also was shown, however, that a promoter might produce an increase in the quality of the surface for the given reaction. Acting in a reverse direction are minor constituents of the reacting system or unwanted products of the reaction, which by preferential adsorption on the reaction sites. Poisoning of a catalyst may also result from the poison adversely modifying the electronic properties of the catalyst.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 12.5259</p> <p>0.00025 12.5249</p> <p>0.0005 12.4628</p> <p>0.00075 12.2996</p> <p>0.001 12.0712</p> <p>0.00125 11.8221</p> <p>0.0015 11.596</p> <p>0.00175 11.4118</p> <p>0.002 11.2616</p> <p>0.00225 11.1177</p> <p>0.0025 10.9536</p> <p>0.00275 10.759</p> <p>0.003 10.5398</p> <p>0.00325 10.3175</p> <p>0.0035 10.1169</p> <p>0.00375 9.94876</p> <p>0.004 9.80787</p> <p>0.00425 9.67857</p> <p>0.0045 9.54646</p> <p>0.00475 9.40536</p> <p>0.005 9.25748</p> <p>0.00525 9.11421</p> <p>0.0055 8.98858</p> <p>0.00575 8.88572</p> <p>0.006 8.80178</p> <p>0.00625 8.72615</p> <p>0.0065 8.64819</p> <p>0.00675 8.5635</p> <p>0.007 8.47426</p> <p>0.00725 8.38872</p> <p>0.0075 8.31553</p> <p>0.00775 8.2578</p> <p>0.008 8.21239</p> <p>0.00825 8.17077</p> <p>0.0085 8.1251</p> <p>0.00875 8.07247</p> <p>0.009 8.01529</p> <p>0.00925 7.9603</p> <p>0.0095 7.91452</p> <p>0.00975 7.88049</p> <p>0.01 7.85474</p> <p>0.01025 7.83035</p> <p>0.0105 7.80092</p> <p>0.01075 7.76453</p> <p>0.011 7.72333</p> <p>0.01125 7.68313</p> <p>0.0115 7.65017</p> <p>0.01175 7.62633</p> <p>0.012 7.60882</p> <p>0.01225 7.59146</p> <p>0.0125 7.5688</p> <p>0.01275 7.53904</p> <p>0.013 7.50421</p> <p>0.01325 7.4698</p> <p>0.0135 7.4414</p> <p>0.01375 7.42087</p> <p>0.014 7.40548</p> <p>0.01425 7.38911</p> <p>0.0145 7.36723</p> <p>0.01475 7.33882</p> <p>0.015 7.30582</p> <p>0.01525 7.27313</p> <p>0.0155 7.24519</p> <p>0.01575 7.22352</p> <p>0.016 7.20619</p> <p>0.01625 7.18805</p> <p>0.0165 7.16393</p> <p>0.01675 7.13321</p> <p>0.017 7.09884</p> <p>0.01725 7.06502</p> <p>0.0175 7.03546</p> <p>0.01775 7.01145</p> <p>0.018 6.99108</p> <p>0.01825 6.96922</p> <p>0.0185 6.94195</p> <p>0.01875 6.90861</p> <p>0.019 6.8712</p> <p>0.01925 6.83338</p> <p>0.0195 6.79882</p> <p>0.01975 6.76887</p> <p>0.02 6.74161</p> <p>0.02025 6.71249</p> <p>0.0205 6.67791</p> <p>0.02075 6.63756</p> <p>0.021 6.59338</p> <p>0.02125 6.54862</p> <p>0.0215 6.50642</p> <p>0.02175 6.46809</p> <p>0.022 6.43121</p> <p>0.02225 6.39171</p> <p>0.0225 6.34695</p> <p>0.02275 6.29666</p> <p>0.023 6.24214</p> <p>0.02325 6.18634</p> <p>0.0235 6.13241</p> <p>0.02375 6.0807</p> <p>0.024 6.02879</p> <p>0.02425 5.9737</p> <p>0.0245 5.9136</p> <p>0.02475 5.84831</p> <p>0.025 5.779</p> <p>0.02525 5.70789</p> <p>0.0255 5.63732</p> <p>0.02575 5.56765</p> <p>0.026 5.49729</p> <p>0.02625 5.42368</p> <p>0.0265 5.34518</p> <p>0.02675 5.26167</p> <p>0.027 5.17445</p> <p>0.02725 5.08554</p> <p>0.0275 4.99626</p> <p>0.02775 4.90677</p> <p>0.028 4.81571</p> <p>0.02825 4.7225</p> <p>0.0285 4.62433</p> <p>0.02875 4.52329</p> <p>0.029 4.40952</p> <p>0.02925 4.30083</p> <p>0.0295 4.20122</p> <p>0.02975 4.10465</p> <p>0.03 4.05785</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Heterogeneously catalyzed continuous flow reactors with highly insulating wall materials for the production of hydrogen by steam reforming
<p><strong>Heterogeneously catalyzed continuous flow reactors with highly insulating wall materials for the production of hydrogen by steam reforming</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>Catalysts may be classified generally according to their physical state, their chemical nature, or the nature of the reactions that they catalyze. Catalysts may be gases, liquids, or solids. In homogeneous catalysis, the catalyst is molecularly dispersed in the same phase (usually gaseous or liquid) as the reactants. In heterogeneous catalysis the reactants and the catalyst are in different phases, separated by a phase boundary. Most commonly, heterogeneous catalysts are solids, and the reactants are gases or liquids. When the catalyst and the reacting substances are present together in a single state of matter, usually as a gas or a liquid, it is customary to classify the reactions as cases of homogeneous catalysis. Oxides of nitrogen serve as catalysts for the oxidation of sulfur dioxide in the lead chamber process for producing sulfuric acid, an instance of homogeneous catalysis in which the catalyst and reactants are gases. Traces of water vapour catalyze some gas reactions, for example, the interaction of carbon monoxide and oxygen, which proceeds only slowly in dry conditions. Sulfuric acid used as a catalyst for the formation of diethyl ether from ethyl alcohol is an example of homogeneous catalysis in the liquid phase (when the products, water and ether, are continuously removed by distillation); by this method, considerable quantities of alcohol can be converted to ether with a single charge of sulfuric acid. The inversion of cane sugar and the hydrolysis of esters by acid solutions also are examples of homogeneous catalysis in the liquid phase.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 2.51969</p> <p>0.00025 2.52898</p> <p>0.0005 2.55637</p> <p>0.00075 2.59905</p> <p>0.001 2.65199</p> <p>0.00125 2.71215</p> <p>0.0015 2.779</p> <p>0.00175 2.85188</p> <p>0.002 2.929</p> <p>0.00225 3.007</p> <p>0.0025 3.08264</p> <p>0.00275 3.15412</p> <p>0.003 3.22107</p> <p>0.00325 3.28478</p> <p>0.0035 3.34725</p> <p>0.00375 3.40961</p> <p>0.004 3.47145</p> <p>0.00425 3.53115</p> <p>0.0045 3.58689</p> <p>0.00475 3.63782</p> <p>0.005 3.68446</p> <p>0.00525 3.72848</p> <p>0.0055 3.77185</p> <p>0.00575 3.81555</p> <p>0.006 3.85919</p> <p>0.00625 3.90117</p> <p>0.0065 3.93975</p> <p>0.00675 3.9745</p> <p>0.007 4.00595</p> <p>0.00725 4.03554</p> <p>0.0075 4.06508</p> <p>0.00775 4.09527</p> <p>0.008 4.1257</p> <p>0.00825 4.15508</p> <p>0.0085 4.18203</p> <p>0.00875 4.20586</p> <p>0.009 4.22692</p> <p>0.00925 4.24666</p> <p>0.0095 4.26675</p> <p>0.00975 4.28804</p> <p>0.01 4.31009</p> <p>0.01025 4.33162</p> <p>0.0105 4.35124</p> <p>0.01075 4.36833</p> <p>0.011 4.38322</p> <p>0.01125 4.39748</p> <p>0.0115 4.41272</p> <p>0.01175 4.42943</p> <p>0.012 4.44708</p> <p>0.01225 4.46422</p> <p>0.0125 4.47947</p> <p>0.01275 4.49245</p> <p>0.013 4.50367</p> <p>0.01325 4.51438</p> <p>0.0135 4.52587</p> <p>0.01375 4.53892</p> <p>0.014 4.55319</p> <p>0.01425 4.56709</p> <p>0.0145 4.57965</p> <p>0.01475 4.59029</p> <p>0.015 4.59928</p> <p>0.01525 4.60791</p> <p>0.0155 4.61738</p> <p>0.01575 4.62855</p> <p>0.016 4.64119</p> <p>0.01625 4.6539</p> <p>0.0165 4.665</p> <p>0.01675 4.67399</p> <p>0.017 4.68163</p> <p>0.01725 4.68922</p> <p>0.0175 4.69783</p> <p>0.01775 4.70789</p> <p>0.018 4.71927</p> <p>0.01825 4.73043</p> <p>0.0185 4.74005</p> <p>0.01875 4.74791</p> <p>0.019 4.75432</p> <p>0.01925 4.76037</p> <p>0.0195 4.7674</p> <p>0.01975 4.77614</p> <p>0.02 4.78619</p> <p>0.02025 4.79589</p> <p>0.0205 4.80412</p> <p>0.02075 4.81091</p> <p>0.021 4.81662</p> <p>0.02125 4.82204</p> <p>0.0215 4.8285</p> <p>0.02175 4.83678</p> <p>0.022 4.84603</p> <p>0.02225 4.85522</p> <p>0.0225 4.8636</p> <p>0.02275 4.87063</p> <p>0.023 4.87617</p> <p>0.02325 4.88134</p> <p>0.0235 4.88764</p> <p>0.02375 4.89563</p> <p>0.024 4.90453</p> <p>0.02425 4.91307</p> <p>0.0245 4.92044</p> <p>0.02475 4.92599</p> <p>0.025 4.92992</p> <p>0.02525 4.93332</p> <p>0.0255 4.93759</p> <p>0.02575 4.94309</p> <p>0.026 4.94878</p> <p>0.02625 4.95359</p> <p>0.0265 4.95679</p> <p>0.02675 4.95736</p> <p>0.027 4.95533</p> <p>0.02725 4.95189</p> <p>0.0275 4.94807</p> <p>0.02775 4.94582</p> <p>0.028 4.94248</p> <p>0.02825 4.9391</p> <p>0.0285 4.93625</p> <p>0.02875 4.93336</p> <p>0.029 4.93052</p> <p>0.02925 4.92708</p> <p>0.0295 4.92401</p> <p>0.02975 4.92139</p> <p>0.03 4.91781</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Heterogeneously catalyzed steam reforming reactors with highly insulating wall materials for hydrogen production
<p><strong>Heterogeneously catalyzed steam reforming reactors with highly insulating wall materials for hydrogen production</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>The design relates to a thermally coupled monolith reactor, used to thermally contact endothermic and exothermic reaction streams in adjacent channels. The geometry allows intimate thermal contact whilst keeping the streams from becoming mixed. The reactor body is constructed by modification of a substantially rigid and essentially nonporous monolith honeycomb. Prior to modification the monolith consists of a honeycombed body having a matrix of thin walls defining a multiplicity of discrete channels which pass through the body of the structure from one face to the opposing face. The monolith is modified in such a way as to produce a rigid body containing at least two discreet process flow paths which have a number of dividing walls in common. For the purpose of this design, a channel is defined as any individual passageway through the monolith body and a flow path is the group of channels used for a single reaction. The monolith body may be constructed from a number of materials using a range of techniques. Suitable materials include ceramics with a low coefficient of thermal expansion which are readily extrudable. These include, but are not limited to, mullite, corderite, alumina, and silica. Other materials include metals which may be extruded, welded, brazed, or diffusion bonded to make such structures. Using metals, it is sometimes useful to start with metal oxide powders, which are then bonded and reduced to the metallic state. Suitable metals include copper, aluminium, stainless steel, iron, titanium, and mixtures or alloys thereof.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 5.24167</p> <p>0.00025 5.35038</p> <p>0.0005 5.59568</p> <p>0.00075 5.86537</p> <p>0.001 6.11865</p> <p>0.00125 6.34243</p> <p>0.0015 6.53109</p> <p>0.00175 6.68219</p> <p>0.002 6.79554</p> <p>0.00225 6.87267</p> <p>0.0025 6.91642</p> <p>0.00275 6.93001</p> <p>0.003 6.91683</p> <p>0.00325 6.88071</p> <p>0.0035 6.82557</p> <p>0.00375 6.75504</p> <p>0.004 6.67218</p> <p>0.00425 6.58003</p> <p>0.0045 6.48092</p> <p>0.00475 6.37655</p> <p>0.005 6.26889</p> <p>0.00525 6.15969</p> <p>0.0055 6.05031</p> <p>0.00575 5.9419</p> <p>0.006 5.83551</p> <p>0.00625 5.73198</p> <p>0.0065 5.63166</p> <p>0.00675 5.53473</p> <p>0.007 5.44181</p> <p>0.00725 5.35303</p> <p>0.0075 5.26832</p> <p>0.00775 5.18794</p> <p>0.008 5.11205</p> <p>0.00825 5.0406</p> <p>0.0085 4.9734</p> <p>0.00875 4.91027</p> <p>0.009 4.85116</p> <p>0.00925 4.79592</p> <p>0.0095 4.74421</p> <p>0.00975 4.69592</p> <p>0.01 4.6509</p> <p>0.01025 4.60897</p> <p>0.0105 4.57006</p> <p>0.01075 4.53403</p> <p>0.011 4.50066</p> <p>0.01125 4.46966</p> <p>0.0115 4.44077</p> <p>0.01175 4.41409</p> <p>0.012 4.38962</p> <p>0.01225 4.36729</p> <p>0.0125 4.34699</p> <p>0.01275 4.32857</p> <p>0.013 4.31176</p> <p>0.01325 4.29635</p> <p>0.0135 4.28232</p> <p>0.01375 4.26966</p> <p>0.014 4.2583</p> <p>0.01425 4.24794</p> <p>0.0145 4.23865</p> <p>0.01475 4.23021</p> <p>0.015 4.22255</p> <p>0.01525 4.21587</p> <p>0.0155 4.21007</p> <p>0.01575 4.20509</p> <p>0.016 4.20091</p> <p>0.01625 4.1973</p> <p>0.0165 4.19387</p> <p>0.01675 4.19079</p> <p>0.017 4.1885</p> <p>0.01725 4.18682</p> <p>0.0175 4.18524</p> <p>0.01775 4.18388</p> <p>0.018 4.18298</p> <p>0.01825 4.18213</p> <p>0.0185 4.18136</p> <p>0.01875 4.18095</p> <p>0.019 4.1809</p> <p>0.01925 4.1808</p> <p>0.0195 4.18068</p> <p>0.01975 4.18095</p> <p>0.02 4.18151</p> <p>0.02025 4.18213</p> <p>0.0205 4.18266</p> <p>0.02075 4.18322</p> <p>0.021 4.18389</p> <p>0.02125 4.18446</p> <p>0.0215 4.18499</p> <p>0.02175 4.18578</p> <p>0.022 4.18649</p> <p>0.02225 4.18705</p> <p>0.0225 4.18769</p> <p>0.02275 4.18848</p> <p>0.023 4.18913</p> <p>0.02325 4.18948</p> <p>0.0235 4.18969</p> <p>0.02375 4.18992</p> <p>0.024 4.18989</p> <p>0.02425 4.18952</p> <p>0.0245 4.18926</p> <p>0.02475 4.18907</p> <p>0.025 4.18838</p> <p>0.02525 4.18717</p> <p>0.0255 4.18578</p> <p>0.02575 4.18424</p> <p>0.026 4.18227</p> <p>0.02625 4.17979</p> <p>0.0265 4.17704</p> <p>0.02675 4.17371</p> <p>0.027 4.16989</p> <p>0.02725 4.16595</p> <p>0.0275 4.16173</p> <p>0.02775 4.15674</p> <p>0.028 4.15105</p> <p>0.02825 4.14506</p> <p>0.0285 4.13866</p> <p>0.02875 4.13164</p> <p>0.029 4.12371</p> <p>0.02925 4.11536</p> <p>0.0295 4.1047</p> <p>0.02975 4.07045</p> <p>0.03 4.04272</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Microchannel steam reforming reactors with insulating wall materials for hydrogen production
<p><strong>Microchannel steam reforming reactors with insulating wall materials for hydrogen production</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>In one form, the design includes a monolithic catalytic reactor with a primary flow path comprising a number of tubes which are lined with a catalyst. As chemical reactants are fed into the primary flow path the chemicals react, with the aid of the catalyst, to produce an exothermic reaction. In the same catalytic reactor is a secondary flow path, also comprising a number of tubes and also lined with a catalyst. In this secondary flow path, a different collection of chemical reactants are fed and, through the aid of the catalyst, will produce an endothermic reaction. The tubes of the primary and secondary flow paths are interspersed with one another within the monolith such that the heat generated from the exothermic reaction may conduct through the tube walls and serve as a heat source for the endothermic reaction. Furthermore, the microchannel steam reforming reactor design includes a method for enhancing one or more catalytic chemical reactions in terms of rate, product yield, energy and other parameters. Here, the initiating an exothermic reaction within one flow path of the monolithic reactor serves the dual purpose of creating a product yield as a result of that exothermic reaction and as a heat source. With the aid of this heat source, a second and endothermic reaction may be initiated in a secondary flow path which may absorb the heat from the exothermic reaction thereby enhancing product yield and making efficient use of available energy. To optimize the use of this heat, the reactions are controlled through one of many factors such as feed rate of the reactants, catalyst quality, reactant concentration and others. The flow paths may be co-current, countercurrent or other such variation as necessary to maximize heat transfer between the two reactions.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 8.97706</p> <p>0.00025 9.12983</p> <p>0.0005 9.45292</p> <p>0.00075 9.76459</p> <p>0.001 10.009</p> <p>0.00125 10.1761</p> <p>0.0015 10.2678</p> <p>0.00175 10.2901</p> <p>0.002 10.2514</p> <p>0.00225 10.1611</p> <p>0.0025 10.0284</p> <p>0.00275 9.86268</p> <p>0.003 9.67153</p> <p>0.00325 9.46156</p> <p>0.0035 9.23929</p> <p>0.00375 9.01005</p> <p>0.004 8.77805</p> <p>0.00425 8.54661</p> <p>0.0045 8.31863</p> <p>0.00475 8.09598</p> <p>0.005 7.87987</p> <p>0.00525 7.67157</p> <p>0.0055 7.47194</p> <p>0.00575 7.28144</p> <p>0.006 7.10033</p> <p>0.00625 6.92886</p> <p>0.0065 6.76695</p> <p>0.00675 6.61432</p> <p>0.007 6.47076</p> <p>0.00725 6.33601</p> <p>0.0075 6.20963</p> <p>0.00775 6.09103</p> <p>0.008 5.98024</p> <p>0.00825 5.87692</p> <p>0.0085 5.78047</p> <p>0.00875 5.6906</p> <p>0.009 5.60703</p> <p>0.00925 5.5293</p> <p>0.0095 5.45708</p> <p>0.00975 5.38993</p> <p>0.01 5.3273</p> <p>0.01025 5.26922</p> <p>0.0105 5.2156</p> <p>0.01075 5.1662</p> <p>0.011 5.12058</p> <p>0.01125 5.07842</p> <p>0.0115 5.03943</p> <p>0.01175 5.00345</p> <p>0.012 4.9703</p> <p>0.01225 4.93973</p> <p>0.0125 4.91161</p> <p>0.01275 4.88587</p> <p>0.013 4.86227</p> <p>0.01325 4.84055</p> <p>0.0135 4.82058</p> <p>0.01375 4.80242</p> <p>0.014 4.78598</p> <p>0.01425 4.77087</p> <p>0.0145 4.75708</p> <p>0.01475 4.74449</p> <p>0.015 4.73297</p> <p>0.01525 4.72248</p> <p>0.0155 4.71307</p> <p>0.01575 4.70472</p> <p>0.016 4.69726</p> <p>0.01625 4.69071</p> <p>0.0165 4.68471</p> <p>0.01675 4.67933</p> <p>0.017 4.67489</p> <p>0.01725 4.67115</p> <p>0.0175 4.66781</p> <p>0.01775 4.66491</p> <p>0.018 4.6626</p> <p>0.01825 4.66054</p> <p>0.0185 4.65865</p> <p>0.01875 4.65713</p> <p>0.019 4.65599</p> <p>0.01925 4.65505</p> <p>0.0195 4.6543</p> <p>0.01975 4.65386</p> <p>0.02 4.65375</p> <p>0.02025 4.65363</p> <p>0.0205 4.6535</p> <p>0.02075 4.6538</p> <p>0.021 4.65451</p> <p>0.02125 4.65516</p> <p>0.0215 4.65575</p> <p>0.02175 4.65657</p> <p>0.022 4.65718</p> <p>0.02225 4.65771</p> <p>0.0225 4.65857</p> <p>0.02275 4.65952</p> <p>0.023 4.66024</p> <p>0.02325 4.66071</p> <p>0.0235 4.66111</p> <p>0.02375 4.66146</p> <p>0.024 4.66145</p> <p>0.02425 4.66101</p> <p>0.0245 4.66041</p> <p>0.02475 4.65975</p> <p>0.025 4.65862</p> <p>0.02525 4.65679</p> <p>0.0255 4.65471</p> <p>0.02575 4.65255</p> <p>0.026 4.6498</p> <p>0.02625 4.64634</p> <p>0.0265 4.64254</p> <p>0.02675 4.63791</p> <p>0.027 4.63242</p> <p>0.02725 4.62651</p> <p>0.0275 4.62008</p> <p>0.02775 4.61266</p> <p>0.028 4.60415</p> <p>0.02825 4.59488</p> <p>0.0285 4.585</p> <p>0.02875 4.57438</p> <p>0.029 4.5624</p> <p>0.02925 4.54979</p> <p>0.0295 4.5335</p> <p>0.02975 4.47929</p> <p>0.03 4.43516</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Thermally coupled monolith reactors with enhanced heat and mass transfer for hydrogen production
<p><strong>Thermally coupled monolith reactors with enhanced heat and mass transfer for hydrogen production</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>The thermally coupled monolith reactor design comprises, in one form thereof, a monolith to which, at each end, the uppermost section of the dividing walls of alternate rows of channels has been ground or cut away. The top section of each of the created voids has been sealed with a suitable material from the end to a depth as to leave an opening in the outer wall, such that a distinct inlet or outlet is formed. A catalyst coating has been applied to the inner wall of the two sets of channels using a suitable technique, one of which is the well-known washcoat technique. Two manifolds, with suitable gaskets, are attached to open ends of the monolith. Furthermore, two addition manifolds, with suitable gaskets, are affixed to the two newly formed openings. The gasket material is chosen to afford a reasonable gas tight seal to prevent cross flow between the two channels. The catalyst coatings may need to be calcined and reduced in order to produce an active catalyst. More particularly, the design comprises, in one form, a monolith to which alternate channels have been sealed at opposing ends. A catalyst coating has been applied to the inner wall. A thin capillary like tube is passed through the inlet of the void and arranged such that it falls short of the sealed end. The opposing end is prepared in a similar manner. Process gas is passed through this tube to the far end of the monolith. The fluid exits the tube is directed back towards to inlet. As the fluid traverses the channel reaction occurs in the catalytically coated walls. Any heat which is required or generated by the process is transferred through the wall. However, even with this highly efficient transfer mechanism the gas will still absorb some heat energy and become hot. This heat energy can be conducted through the capillary inlet tube to preheat the incoming reactants. This arrangement alleviates the need for an external heat exchanger (although one can be used to provide further heating) and improvers the overall efficiency of the reactor.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 10.8203</p> <p>0.00025 10.9546</p> <p>0.0005 11.2153</p> <p>0.00075 11.4215</p> <p>0.001 11.5345</p> <p>0.00125 11.5606</p> <p>0.0015 11.5129</p> <p>0.00175 11.4049</p> <p>0.002 11.2484</p> <p>0.00225 11.0544</p> <p>0.0025 10.8331</p> <p>0.00275 10.5932</p> <p>0.003 10.3414</p> <p>0.00325 10.0835</p> <p>0.0035 9.82406</p> <p>0.00375 9.56646</p> <p>0.004 9.31349</p> <p>0.00425 9.06713</p> <p>0.0045 8.82918</p> <p>0.00475 8.60082</p> <p>0.005 8.3823</p> <p>0.00525 8.17379</p> <p>0.0055 7.97561</p> <p>0.00575 7.78777</p> <p>0.006 7.61007</p> <p>0.00625 7.44219</p> <p>0.0065 7.28392</p> <p>0.00675 7.13507</p> <p>0.007 6.99548</p> <p>0.00725 6.86493</p> <p>0.0075 6.74275</p> <p>0.00775 6.62832</p> <p>0.008 6.52152</p> <p>0.00825 6.42164</p> <p>0.0085 6.32835</p> <p>0.00875 6.24151</p> <p>0.009 6.16052</p> <p>0.00925 6.08491</p> <p>0.0095 6.01452</p> <p>0.00975 5.94897</p> <p>0.01 5.88786</p> <p>0.01025 5.83131</p> <p>0.0105 5.7787</p> <p>0.01075 5.72978</p> <p>0.011 5.68436</p> <p>0.01125 5.64228</p> <p>0.0115 5.60333</p> <p>0.01175 5.56712</p> <p>0.012 5.53346</p> <p>0.01225 5.5021</p> <p>0.0125 5.47301</p> <p>0.01275 5.44619</p> <p>0.013 5.42156</p> <p>0.01325 5.3988</p> <p>0.0135 5.37773</p> <p>0.01375 5.35853</p> <p>0.014 5.34102</p> <p>0.01425 5.32469</p> <p>0.0145 5.30957</p> <p>0.01475 5.29573</p> <p>0.015 5.28316</p> <p>0.01525 5.27177</p> <p>0.0155 5.26118</p> <p>0.01575 5.25136</p> <p>0.016 5.24246</p> <p>0.01625 5.23449</p> <p>0.0165 5.22729</p> <p>0.01675 5.22085</p> <p>0.017 5.21505</p> <p>0.01725 5.20996</p> <p>0.0175 5.20538</p> <p>0.01775 5.20125</p> <p>0.018 5.19797</p> <p>0.01825 5.195</p> <p>0.0185 5.19226</p> <p>0.01875 5.19015</p> <p>0.019 5.1885</p> <p>0.01925 5.18698</p> <p>0.0195 5.18558</p> <p>0.01975 5.18461</p> <p>0.02 5.18412</p> <p>0.02025 5.18363</p> <p>0.0205 5.18302</p> <p>0.02075 5.18277</p> <p>0.021 5.18289</p> <p>0.02125 5.1829</p> <p>0.0215 5.18274</p> <p>0.02175 5.18262</p> <p>0.022 5.18211</p> <p>0.02225 5.18139</p> <p>0.0225 5.1809</p> <p>0.02275 5.18047</p> <p>0.023 5.17976</p> <p>0.02325 5.17871</p> <p>0.0235 5.17765</p> <p>0.02375 5.17665</p> <p>0.024 5.17509</p> <p>0.02425 5.17287</p> <p>0.0245 5.17047</p> <p>0.02475 5.1679</p> <p>0.025 5.1648</p> <p>0.02525 5.16115</p> <p>0.0255 5.15706</p> <p>0.02575 5.15234</p> <p>0.026 5.14688</p> <p>0.02625 5.14071</p> <p>0.0265 5.13396</p> <p>0.02675 5.12621</p> <p>0.027 5.11737</p> <p>0.02725 5.10778</p> <p>0.0275 5.09726</p> <p>0.02775 5.08542</p> <p>0.028 5.07222</p> <p>0.02825 5.05787</p> <p>0.0285 5.04248</p> <p>0.02875 5.02603</p> <p>0.029 5.00788</p> <p>0.02925 4.98897</p> <p>0.0295 4.9649</p> <p>0.02975 4.88466</p> <p>0.03 4.81923</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Autothermal steam reforming reactors with thermally conductive walls for hydrogen production
<p><strong>Autothermal steam reforming reactors with thermally conductive walls for hydrogen production</strong></p> <p>Junjie Chen</p> <p>Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com</p> <p> </p> <p>It is necessary to provide a reactor where the catalytically active components are immobilized on adjacent sides of the monolith dividing walls such that heat transfer can occur via purely conduction through the wall from one catalytic process to the second catalytic process. It is also necessary to provide a reactor where the monolith body is demountable from the inlet and outlet manifolds such that catalyst replacement and recovery of spent catalyst can be easily performed. It is also necessary to provide a reactor where the heat transfer characteristics are decoupled from the reactant or product fluid velocities such that the system can operate with moderate gas velocities and with low pressure drops. It is also necessary to provide a reactor of low thermal inertia and high heat load such that rapid start up and fast response to load transients can be achieved. The design comprises, in one form thereof, a chemical processing method to thermally contact an endothermic and an exothermic reaction without mixing the two streams, utilizing a thermally coupled monolith reactor. A ceramic or metal monolith is modified to produce a structure containing at least two sets of discrete flow channels and which are separated by a number of common walls. Manifolds are arranged such that one reaction mixture flows through one set of channels and a different reaction mixture flows through the second. Catalytic material, which is active for the relevant reaction, is coated onto the inner walls of each of the sets of channels. The two reactions are chosen such that one is exothermic and one is endothermic, such that the energy required by the endothermic process is supplied directly through the dividing wall from the exothermic process occurring on the opposing side. This method of heat transfer completely decouples the gas phase hydrodynamics from the heat transfer process.</p> <p>Streamwise distance (meter), Heterogeneous reaction rate along the length of the reactor (mole per square meter per second)</p> <p>0 12.1245</p> <p>0.00025 12.2056</p> <p>0.0005 12.3371</p> <p>0.00075 12.3931</p> <p>0.001 12.3704</p> <p>0.00125 12.2891</p> <p>0.0015 12.1645</p> <p>0.00175 12.0076</p> <p>0.002 11.8272</p> <p>0.00225 11.63</p> <p>0.0025 11.4214</p> <p>0.00275 11.2059</p> <p>0.003 10.987</p> <p>0.00325 10.7674</p> <p>0.0035 10.5496</p> <p>0.00375 10.3354</p> <p>0.004 10.1263</p> <p>0.00425 9.9232</p> <p>0.0045 9.72691</p> <p>0.00475 9.53772</p> <p>0.005 9.35585</p> <p>0.00525 9.18161</p> <p>0.0055 9.01491</p> <p>0.00575 8.85575</p> <p>0.006 8.70412</p> <p>0.00625 8.55976</p> <p>0.0065 8.42235</p> <p>0.00675 8.29183</p> <p>0.007 8.16813</p> <p>0.00725 8.05097</p> <p>0.0075 7.94006</p> <p>0.00775 7.83509</p> <p>0.008 7.73603</p> <p>0.00825 7.64259</p> <p>0.0085 7.55447</p> <p>0.00875 7.47149</p> <p>0.009 7.39325</p> <p>0.00925 7.31962</p> <p>0.0095 7.25041</p> <p>0.00975 7.18541</p> <p>0.01 7.12413</p> <p>0.01025 7.06625</p> <p>0.0105 7.01189</p> <p>0.01075 6.96101</p> <p>0.011 6.91331</p> <p>0.01125 6.86823</p> <p>0.0115 6.82574</p> <p>0.01175 6.78591</p> <p>0.012 6.74833</p> <p>0.01225 6.7128</p> <p>0.0125 6.67938</p> <p>0.01275 6.648</p> <p>0.013 6.61842</p> <p>0.01325 6.5905</p> <p>0.0135 6.56401</p> <p>0.01375 6.53896</p> <p>0.014 6.51549</p> <p>0.01425 6.49316</p> <p>0.0145 6.47196</p> <p>0.01475 6.45184</p> <p>0.015 6.43277</p> <p>0.01525 6.41475</p> <p>0.0155 6.39735</p> <p>0.01575 6.38068</p> <p>0.016 6.36501</p> <p>0.01625 6.35036</p> <p>0.0165 6.33607</p> <p>0.01675 6.32215</p> <p>0.017 6.30899</p> <p>0.01725 6.29632</p> <p>0.0175 6.28384</p> <p>0.01775 6.27168</p> <p>0.018 6.2601</p> <p>0.01825 6.24866</p> <p>0.0185 6.23744</p> <p>0.01875 6.22675</p> <p>0.019 6.21628</p> <p>0.01925 6.20588</p> <p>0.0195 6.19553</p> <p>0.01975 6.18524</p> <p>0.02 6.17518</p> <p>0.02025 6.16499</p> <p>0.0205 6.1546</p> <p>0.02075 6.1444</p> <p>0.021 6.13426</p> <p>0.02125 6.12398</p> <p>0.0215 6.11344</p> <p>0.02175 6.10277</p> <p>0.022 6.09166</p> <p>0.02225 6.08022</p> <p>0.0225 6.06884</p> <p>0.02275 6.05715</p> <p>0.023 6.04483</p> <p>0.02325 6.03193</p> <p>0.0235 6.01875</p> <p>0.02375 6.00527</p> <p>0.024 5.99094</p> <p>0.02425 5.97588</p> <p>0.0245 5.96041</p> <p>0.02475 5.94431</p> <p>0.025 5.92737</p> <p>0.02525 5.90954</p> <p>0.0255 5.89105</p> <p>0.02575 5.87191</p> <p>0.026 5.85159</p> <p>0.02625 5.83007</p> <p>0.0265 5.80776</p> <p>0.02675 5.78416</p> <p>0.027 5.7593</p> <p>0.02725 5.73344</p> <p>0.0275 5.70642</p> <p>0.02775 5.67803</p> <p>0.028 5.64823</p> <p>0.02825 5.61725</p> <p>0.0285 5.58477</p> <p>0.02875 5.55098</p> <p>0.029 5.52507</p> <p>0.02925 5.49861</p> <p>0.0295 5.46342</p> <p>0.02975 5.43244</p> <p>0.03 5.40902</p> <p>Contributor: Junjie Chen, ORCID: 0000-0001-5055-4309, E-mail address: komcjj@gmail.com, Department of Energy and Power Engineering, School of Mechanical and Power Engineering, Henan Polytechnic University, 2000 Century Avenue, Jiaozuo, Henan, 454000, P.R. China</p>
Dataset of paper "Hydrogen production from urea in human urine using segregated systems"
<p>Dataset of paper "Hydrogen production from urea in human urine using segregated systems"</p> <ul> <li>Fig. 2. Isotherm experimental data for adsorption of urea onto activated carbon at different temperatures.</li> <li>Table 2. Langmuir and Freundlich Equations fitting parameters for the isotherms of adsorption of urea on activated carbon.</li> <li>Fig. 3. Kinetic study of the adsorption of urea onto activated carbon.</li> <li>Table 1. Comparison of adsorption capacity of urea onto studied activated carbon with literature carbon-based materials.</li> <li>Fig. 4. A: Outlet gases concentration as a function of temperature during the thermal treatment of urea adsorbed on activated carbon. B: Carbon dioxide concentration as a function of temperature during thermal treatment of fresh and saturated activated carbon.</li> <li>Fig. 5. Adsorption capacity of urea with regenerated carbon after five consecutive adsorption/desorption cycles</li> <li>Fig. 6. Hydrogen and ammonia production from thermal treatment and catalytic treatment of urea adsorbed on activated carbon</li> <li>Table 3. Efficiencies assumed for the preliminary energy balance calculation of the designed process.</li> <li>Fig. 7. Distribution of energy requirements to produce hydrogen from urea present in human urine.</li> <li>Fig. 8. Summary of the energy analysis for the installation of the process in the city of Lleida, Spain.</li> <li>Fig. 9. Sensitivity analysis of the effect of urea adsorption capacity and ammonia decomposition temperature on the net energy production of the designed process.</li> <li>Table 4. Energy balance summary.</li> </ul>
Techno-economic evaluation and resource assessment of hydrogen production through offshore wind farms: A European perspective - Supplementary material
<p>This is the additional material provided with the journal article "Techno-economic evaluation and resource assessment of hydrogen production through offshore wind farms: A European perspective" published in Renewable and Sustainable Energy Reviews (<a href="https://doi.org/10.1016/j.rser.2023.113699">https://doi.org/10.1016/j.rser.2023.113699</a>).</p> <p>Datasets are provided as NetCDF files for European maps and CSVfor Economically Attractive Resource curves.</p> <p>European and National plots are provided as PDF files.</p>
A fresh thermodynamic outlook of hydrogen production by water splitting from an exergy-based perspective
<p>The upload files is the origin data and calculation procedure for the article titled "A fresh thermodynamic outlook of hydrogen production by water splitting from an exergy-based perspective".</p>
Data for "Transparent Porous Conductive Substrates for Gas-Phase Photoelectrochemical Hydrogen Production"
<p>Data archive for "Transparent Porous Conductive Substrates for Gas-Phase Photoelectrochemical Hydrogen Production"</p> <p>DOI: 10.1002/adma.202208740</p>
Dataset of paper "Solar photoelectrocatalytic oxidation of urea in water coupled to green hydrogen production"
<p>Dataset of paper "Solar photoelectrocatalytic oxidation of urea in water coupled to green hydrogen production"</p> <ul> <li>Material characterization for TiO<sub>2</sub> and WO<sub>3</sub> electrodes. </li> <li>Photoelectrochemical characterization for TiO<sub>2</sub> and WO<sub>3</sub>. </li> <li>One compartment cell characterization.</li> <li>Urea oxidation experiments for TiO<sub>2</sub> and WO<sub>3</sub> electrodes.</li> <li>Urea oxidation and products using one compartment cell.</li> <li>Production of NO<sub>2</sub><sup>-</sup> during urea oxidation.</li> <li>Evolution of NO<sub>3</sub><sup>−</sup> oxidation in time and conversion to NH<sub>4</sub><sup>+</sup>.</li> <li>Two compartment cell characterization.</li> <li>Urea oxidation and products using two-compartment cell.</li> </ul>
Minimizing emissions from grid-based hydrogen production in the United States: Raw Data
<p>This repository contains all GenX model input and results data relevant to the paper 'Minimizing emissions from grid-based hydrogen production in the United States.' Data for each modeled scenario is contained within a folder in the main directory, using the naming convention [Clean Energy Matching Regime]_[Model Year]_[Electrolyzer Zone]_[Electrolyzer Capacity]_[Hydrogen Sales Revenue]kg_[Additional Descriptors]. Clean energy matching regime tags include `BaseCase' (the No Policy regime), `100AM' (the 100% Annual Matching regime), `100WM' (the 100% Weekly Matching regime), `100CFE' (the 100% Hourly Matching regime), and `100SRME' (the Net-Zero SRME regime). The `BaseCase_2030_noload' folder contains the baseline system without any added electrolysis demand. The `Scripts' folder contains plotting scripts and copies of all figures used in this work. The `SRME Iterations' folder contains intermediate runs used to calculate short-run marginal emissions time-series for each SRME case. Each case folder in the main repository contains `Inputs' and `Settings' folders, which contain GenX inputs and are described further in the GenX GitHub repository: <a href="https://github.com/GenXProject/GenX">https://github.com/GenXProject/GenX</a>. All model outputs are contained in the `Results' folder and are also described in detail in the GenX documentation. Cases should be run using the version of GenX included in this repository, from a folder within the main GenX folder named '2030'.</p>
Rational design of optimal bimetallic and trimetallic nickel-based single-atom alloys for bio-oil upgrading toward hydrogen production
<p>Supplementary Data for the "Rational design of optimal <em>bimetallic</em> and <em>trimetallic</em> nickel-based single-atom alloys for bio-oil upgrading toward hydrogen production".</p>
Experimental source data for "A photosensitiser-polyoxometalate dyad that enables the decoupling of light- and dark-reactions for delayed on-demand solar hydrogen production"
<p>Experimental data for the manuscript "A photosensitiser-polyoxometalate dyad that enables the decoupling of light- and dark-reactions for delayed on-demand solar hydrogen production"</p>
Products for "Hydrogen sulfide and metal-enriched atmosphere for a Jupiter-mass exoplanet"
<p>Data and model for JWST transit observation of HD 189733b using NIRCam (GO 1633, PI: Drake Deming) from paper "Hydrogen sulfide and metal-enriched<br>atmosphere for a Jupiter-mass exoplanet" (Fu et al. 2024).</p>
Solar Hydrogen Production By Photoelectrochemical Water Splitting "Freilandversuch"
Open the record for dataset details and reuse information.
Input data and code related to "Utilizing curtailed wind and solar power to scale up electrolytic hydrogen production in Europe"
<p>Datasets and code for the submitted article: "Utilizing curtailed wind and solar power to scale up electrolytic hydrogen production in Europe" </p> <p>by Alissa Ganter<sup>1,2</sup>, Tyler H. Ruggles<sup>2</sup>, Paolo Gabrielli<sup>1</sup>, Giovanni Sansavini<sup>1,*</sup>, Ken Caldeira<sup>2</sup></p> <p><sup>1</sup> Institute of Energy and Process Engineering, ETH Zurich, 8092 Zurich, Switzerland</p> <p><sup>2</sup> Department of Global Ecology, Carnegie Institution for Science, Stanford, CA, USA</p> <p><sup>*</sup> Corresponding author: email - sansavig@ethz.ch</p> <p>All rights lie with the authors. Refer to the README.docx for a description of the datasets and their usage in the article.</p>
Dataset "Combining biomass gasification and LOHC mixed gas hydrogenation for high purity hydrogen production and storage"
Open the record for dataset details and reuse information.
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Allen Brain Atlas
Allen Brain Atlas is an Allen Institute collection of brain map atlases, datasets, APIs, and analysis tools covering mouse, human, and non-human primate brain resources.
Annotated Behaviour and Observability Dataset (ABODe)
ABODe is a University of Edinburgh DataShare dataset for behavior classification in group-housed mice using home-cage video, identities, bounding boxes, ground-plate positions, and annotator labels.
DANDI Archive for NWB datasets
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International Brain Laboratory public data
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OpenNeuro
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